JP2005337565A - Absorption refrigerator - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an absorption refrigerator with an absorber using a small and highly efficient ejector. <P>SOLUTION: The absorption refrigerator comprises an evaporator 9, the absorber 1, a condenser 8, regenerators 6, 7, solution heat exchangers 3, 5, a pump 19, and pipes connecting theses together. The absorber 1 has the ejector 11 using absorbed liquid enriched by the regenerators 6, 7 as a drive source for sucking refrigerant vapor in the evaporator 9 and absorbing it into the absorbed liquid. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to an absorption refrigerator.

  As a prior art regarding an absorption refrigerator using a shell and tube type absorber using a falling liquid film, for example, the one described in JP-A-6-347122 (Patent Document 1) can be cited. This absorption refrigerator includes an evaporator, a water heater, an absorber, a condenser, a high temperature regenerator, a low temperature regenerator, a solution heat exchanger, a solution pump, a refrigerant pump, a hot water three-way valve, and a piping system that operatively couples them. It is composed of A shell and tube type heat exchanger that performs heat exchange between the fluid flowing in the tube and the fluid flowing on the shell side is used in the heat exchanger portion of the water-cooled absorber. The refrigerant vapor evaporated in the evaporator flows into the absorber, where it is absorbed by the aqueous lithium bromide solution sprayed onto the absorber heat transfer tube.

  Moreover, as a prior art regarding the absorption refrigerator using the spray type absorber by a nozzle, the thing as described in Unexamined-Japanese-Patent No. 11-270921 (patent document 2) is mentioned, for example. This absorption refrigerator includes an evaporator that evaporates the refrigerant, an absorber that absorbs the refrigerant vapor evaporated in the evaporator into an absorbing liquid, a high-temperature regenerator that regenerates the absorbing liquid that has absorbed the refrigerant in the absorber, and a low-temperature A regenerator, a condenser for condensing refrigerant vapor generated by regeneration in the high temperature regenerator and the low temperature regenerator, and a steam passage connecting the low temperature regenerator and the condenser. And the absorption solution cooled by the solution cooling part is sprayed from the sprayer provided in the absorber main body of the absorber, and the refrigerant vapor evaporated in the heat transfer tube is absorbed into the absorption solution.

JP-A-6-347122

Japanese Patent Laid-Open No. 11-270921

  Since the absorber of patent document 1 is a shell & tube system which performs heat exchange between the fluid flowing in the tube and the fluid flowing on the shell side, the heat transfer performance greatly depends on the thickness of the liquid film and the flow speed. In addition, it is inevitable to simultaneously perform the heat and mass transfer process during the absorption process. Therefore, in the absorber of patent document 1, since a highly efficient heat exchanger, such as a plate fin, cannot be used, it is difficult to improve heat transfer performance, and the apparatus has been enlarged.

  On the other hand, the absorber of patent document 2 sprays the absorption liquid which it cooled and supercooled previously in the free space in an absorber for the purpose of isolate | separating the said two movement processes with a nozzle. The system absorbs refrigerant vapor generated in the evaporator. In the absorber of this patent document 2, since the absorbing liquid is sprayed by the nozzle, there is an advantage that the gas-liquid interface between the liquid droplet and the refrigerant vapor is increased. The only factor causing the absorption action was mass transfer due to the difference in the saturated concentration of the absorption liquid as in the case of a conventional absorber using a falling film. Further, in the absorber of Patent Document 2, since the absorbing liquid can be cooled only for the purpose of bringing the absorbing liquid into a supercooled state at the nozzle inlet, the refrigerant vapor is absorbed more than the conventional absorber using the falling liquid film. The ability was small. Therefore, the performance of the absorber cannot be secured unless the solution at the outlet of the absorber is recirculated, leading to an increase in the size and complexity of the absorber.

  An object of the present invention is to provide an absorption refrigerator capable of increasing the efficiency and size of an absorber.

  In order to achieve the above object, the present invention provides an absorption refrigerator comprising an evaporator, an absorber, a condenser, a regenerator, a solution heat exchanger, pumps, and piping connecting them, and the absorber is The present invention is configured to include an ejector that uses the absorption liquid concentrated in the regenerator as a drive source and sucks the refrigerant vapor inside the evaporator and absorbs it into the absorption liquid.

  In order to achieve the above object, the present invention provides an absorption refrigerator comprising an evaporator, an absorber, a condenser, a regenerator, a solution heat exchanger, pumps, and piping connecting them. The apparatus includes an ejector that uses the absorption liquid concentrated in the regenerator as a driving source and sucks the refrigerant vapor inside the evaporator and absorbs it into the absorption liquid. The ejector uses a two-phase flow laval nozzle as a nozzle part. It is in the configuration.

A more preferable specific configuration of the present invention is as follows.
(1) Absorbing liquid having a saturation pressure lower than the evaporator pressure is used as the drive source of the ejector.
(2) A cooling heat exchanger is disposed on the outlet side of the ejector.
(3) A heating heat exchanger is disposed on the inlet side of the absorbing liquid of the ejector.
(4) A solution pump for increasing the pressure of the absorbing liquid is disposed on the inlet side of the ejector.
(5) A plurality of the ejectors are provided in series.
(6) The absorber is configured by arranging the ejector inside the evaporator space.
(7) In the absorber, the ejector is disposed in close contact with or adjacent to the side surface of the evaporator, and an opening serving as a passage for intake steam is provided on the wall surface.

  ADVANTAGE OF THE INVENTION According to this invention, it is possible to implement | achieve the absorption refrigerator which can raise the efficiency and size reduction of an absorber.

  Hereinafter, a plurality of embodiments of the present invention will be described with reference to the drawings. The same reference numerals in the drawings of the respective embodiments indicate the same or equivalent.

  The absorption refrigerator according to the first embodiment of the present invention will be described with reference to FIGS.

  First, the overall configuration of the absorption refrigerator according to the present embodiment will be described with reference to FIGS. 1 and 2. FIG. 1 is a block diagram of a double effect absorption refrigerator according to a first embodiment of the present invention, and FIG. 2 is a block diagram of the main part of the absorber of FIG.

As shown in FIG. 1, the absorption refrigerator of the present embodiment includes a mixed absorber 1, a low temperature heat exchanger 3, a high temperature solution heat exchanger 5, a high temperature regenerator 6, a low temperature regenerator 7, a condenser 8, and evaporation. 2 is a parallel flow type H ₂ O / LiBr-based gas-fired double-effect absorption refrigerator composed of a vessel 9. In addition, in FIG. 1, the arrow has shown the flow direction of absorption liquid, a refrigerant | coolant, and cooling. Further, the present invention is applicable to absorption refrigerators such as a series flow and a reverse flow.

  In this absorption refrigerator, the dilute solution from the absorber 1 is sent to the low-temperature solution heat exchanger 3 by the solution circulation pump 2 and is divided after leaving the low-temperature solution heat exchanger 3. One of the dilute solutions is sent to the high-temperature solution heat exchanger 5 and then sent to the high-temperature regenerator 6, and the other dilute solution that has been diverted is sent to the low-temperature regenerator 7. It is composed. The rare solution sent to the high temperature regenerator 6 is heated by the burner 6A in the high temperature regenerator 6 and separated into refrigerant vapor and concentrated solution. The rare solution sent to the low temperature regenerator 7 is heated by the refrigerant vapor generated in the high temperature regenerator 6 and separated into the refrigerant vapor and the concentrated solution. The concentrated solution thus concentrated is returned to the absorber 1 through the high temperature solution heat exchanger 5 and the low temperature solution heat exchanger 3 again.

  The refrigerant drain condensed by heating the low temperature regenerator 7 is guided to the condenser 8, and the refrigerant vapor generated in the low temperature regenerator 7 is guided to the condenser 8, and these are condensed in the condenser 8. The condensed refrigerant condensed in this way is returned to the evaporator 9.

  The evaporator 9 is for evaporating the liquid refrigerant. A tank part that stores liquid refrigerant is formed at the bottom of the evaporator 9, and a refrigerant pump 91 that sucks the stored liquid refrigerant is connected to the tank part. The refrigerant pump 91 is installed in a refrigerant spray pipe 92 that communicates the tank portion with the upper part of the evaporator 9. The liquid refrigerant stored in the tank part is supplied to the upper part in the evaporator 9 through the refrigerant spray pipe 92 by the operation of the refrigerant pump 91 and sprayed from the upper part in the evaporator 9. Below that, a cold water pipe 93 to which water is supplied by a cold water pump (not shown) is provided. The sprayed refrigerant is evaporated in the evaporator 9, and the water in the cold water pipe 93 is cooled by the heat of evaporation. The cooled water is used as cooling water for cooling. Further, the evaporated refrigerant vapor is sucked into the absorber 1.

  The absorber 1 is provided adjacent to the evaporator 9 in order to absorb and dilute the refrigerant vapor into the concentrated solution. The absorber 1 includes a solution pump 18, a cooling heat exchanger 16, a first stage ejector 11, a first stage cooling heat exchanger 17, a first stage solution pump 19, a second stage ejector 11A, and a second stage cooling. The heat exchanger 17A and the second stage solution pump 19A are connected in series. In this embodiment, in order to reduce the size and increase the efficiency of the absorber 1, the absorber 1 is constituted by a two-stage ejector in which a first-stage ejector 11 and a second-stage ejector 11A are connected in series.

  In FIG. 2, the first stage ejector 11 includes a first stage nozzle part 12, a first stage suction part 13, a first stage mixing part 14, and a first stage diffuser part 15. The second stage ejector 11A includes a second stage nozzle part 12A, a second stage suction part 13A, a second stage mixing part 14A, and a second stage diffuser part 15A. The first-stage nozzle portion 12 and the second-stage nozzle portion 12A are composed of tapered nozzles.

  Reference numeral 10 denotes a flow of the absorption liquid concentrated in the regenerators 6 and 7, reference numerals 20 and 20A denote a flow of the absorption liquid cooled by the cooling heat exchanger 16 and the cooling heat exchanger 16A and brought into a supercooled state, 30 , 30A is the flow of the refrigerant vapor generated in the evaporator 9, 40 and 40A are the two-phase flow of the absorption liquid and the refrigerant vapor, and 50 and 50A are the absorption liquid at the outlet of the first stage diffuser section 15 and the second stage diffuser section 15A. , 60 and 60A are the flow of the absorption liquid at the outlet of the first stage cooling heat exchanger 17 and the second stage cooling heat exchanger 17A, and 70 and 70A are the first stage solution pump 19 and the second stage solution pump. The flow of the absorption liquid on the outlet side of 19A is shown.

  The operation of the absorber 1 will be described with reference to FIGS.

  The absorbent in the stream 10 that is concentrated in the high-temperature regenerator 6 and the low-temperature regenerator 7 and returned to the absorber 1 is pressurized by the solution pump 18 and further cooled by the cooling heat exchanger 16 to be in a supercooled state. The absorption liquid in the supercooled flow 20 is sprayed into the venturi from the nozzle portion 12 of the first stage ejector 11 using the flow 20 as a driving flow. As a result, the refrigerant vapor is sucked from the evaporator 9 as a flow 30 and mixed with the sprayed absorption liquid to generate a gas-liquid two-phase flow 40. Thereafter, the gas-liquid two-phase flow 40 flows through the first-stage mixing unit 14 and the first-stage diffuser unit 15, and while the pressure is recovered, the saturation concentration difference of the supercooled absorption liquid and the compression action of the first-stage ejector 11 As a result, the refrigerant vapor is absorbed by the absorbent and flows out as a flow 50. Further, since the first-stage cooling heat exchanger 17 is installed on the outlet side of the first-stage ejector 11, the supercooled absorption is achieved by cooling the absorbent with the first-stage cooling heat exchanger 17. Refrigerant vapor that could not be absorbed by the absorption effect due to the saturation concentration difference of the liquid and the compression action of the first stage ejector 11 is again absorbed by the saturation concentration difference of the absorption liquid in the first stage cooling heat exchanger 17 and flows. It is discharged as 60. Therefore, the efficiency of the absorber 1 can be further increased. The cooling method for the first stage cooling heat exchanger 17 may be either a water cooling type or an air cooling type.

  The absorption liquid in the stream 60 having a reduced concentration is boosted by the first stage solution pump 19. The pressure-absorbing liquid 70 in the flow 70 is sprayed into the venturi from the second stage nozzle portion 12A using the flow 70 as a driving flow. As a result, refrigerant vapor is sucked from the evaporator 9 as a flow 30A and mixed with the sprayed absorption liquid to generate a gas-liquid two-phase flow 40A. Thereafter, the gas-liquid two-phase flow 40A flows through the second-stage mixing section 14A, the second-stage diffuser section 15A, and the second-stage cooling heat exchanger 17A, and the refrigerant vapor is absorbed by the absorbing liquid while the pressure is recovered. By cooling with the second stage cooling heat exchanger 17A, the refrigerant vapor is further absorbed by the absorption liquid, resulting in a flow 50A having a further reduced concentration. The dilute solution in the flow 50A is pressurized by the second stage solution pump 19A and flows out to the low temperature solution heat exchanger 3. Note that the first stage diffuser unit 15 and the second stage diffuser unit 15A may be omitted depending on usage conditions.

  According to the absorber 1, the absorption action is caused by the suction effect by the momentum in addition to the conventional mass transfer due to the saturation concentration difference, and is absorbed by the stage mixing unit 14, 14 A / diffuser unit 15, 15 A in the ejectors 11, 11 A. Excellent effects such as being able to recover the pressure of the liquid and the refrigerant vapor and being able to also serve as an extraction device that absorbs the non-condensable gas of the absorber 1 by the suction effect of the venturi can be obtained. More specifically, the first point is that the absorption action is due to the entrainment effect of the jet in addition to the conventional thermal effect and the compression action by the stage mixing portions 14, 14A and the diffuser portions 15, 15A in the ejectors 11, 11A. The effect is also due. This makes it possible to achieve higher efficiency of the absorber 1 than in the prior art. The second point is that since the free space is not provided in the absorber 1, the absorber 1 can be significantly reduced in size. The third point is that, unlike the absorbers of the prior art, the refrigerant vapor is forcibly sucked, so that the extraction device that absorbs the non-condensable gas of the absorber that has greatly influenced the performance of the absorber in the past can also be used. It is possible.

  Further, the absorber 1 of the present embodiment is greatly different from the conventional shell and tube type absorber in addition to the above-mentioned difference, that the heat and mass transfer process in the absorption process can be separated, and the ejector nozzle part For example, by creating a fine jet, the area of the gas-liquid interface can be increased, so that the absorption phenomenon can be promoted.

  Moreover, since the refrigerant | coolant vapor | steam absorption amount increases by providing the ejector 11 and 11A in multiple steps in series, the absorption liquid 10A concentrated by the regenerators 6 and 7 and the absorption liquid 70A of the exit of the absorber 1 are included. The performance of the absorption refrigerator is improved by increasing the concentration range.

  A cycle simulation of such an absorption refrigerator will be described with reference to FIGS.

In the cycle simulation, the heat balance of each heat exchanger was calculated separately for the amount of change in enthalpy inside and outside the heat transfer tube and the amount of heat transfer obtained using the logarithm average temperature difference. Incidentally, COP representing the efficiency of the refrigerator as the following equation (1) was calculated by the ratio of the high-temperature regenerator heat quantity Q _HG refrigerating capacity Q _E and higher heating value basis.
COP = Q _E / Q _HG (1)
Table 1 shows the capacity of the absorption refrigerator, the cold water / cooling water conditions, and the solution temperature / pressure at the venturi inlet, which were the targets of the simulation.

  Moreover, the experimental result regarding the absorption performance of a venturi is as showing in FIG. The reason why the refrigeration capacity was set to 2.0 usRT in the simulation is that the solution circulation amount of the experimental venturi was equivalent to 2.0 usRT, and was adjusted accordingly. The venturi performance curve is obtained by measuring the inlet and outlet concentration widths (for one stage) using the inlet concentration as a parameter under the same inlet temperature and pressure conditions as in the simulation. The calculation of the venturi part of the cycle simulation is based on this performance curve.

  Changes in the COP and the cycle state when the inlet concentration of the absorber 1 is used as a parameter are as shown in FIG. As is apparent from FIG. 4, the COP when the absorber 1 of this embodiment is used is improved by about 10% to 15% compared to the conventional cycle, and the tendency is that the improvement rate decreases as the inlet concentration of the absorber 1 decreases. Can be seen to be higher. This is because the sensible heat loss inside the cycle can be reduced because the temperature of the high-temperature regenerator 6 is lowered by reducing the inlet concentration of the absorber 1. In the case of the conventional falling film type absorber, the absorption action is small in the low concentration absorbent of the 50% level, so the cycle must be configured so that the concentration of the concentrated solution is in the 60% level. In the case of the absorber 1 of the present embodiment, the heat / mass transfer process is separated, and the absorption action is caused by the suction effect by the momentum in addition to the mass transfer by the saturation concentration difference. It is possible to configure the cycle at a lower concentration than the cycle. As a result, the COP can be improved and the possibility of crystallization and corrosion of the solution can be reduced.

  Table 2 compares the volume of the absorber 1 of this example with that of the conventional falling liquid film type absorber. The volume of the absorber 1 of the present embodiment is indicated by the total value of two venturis, heat exchangers, and solution pumps because the first stage ejector 11 and the second stage ejector 11A are provided in two stages in series. . In addition, since there is no comparison object of the conventional 2.0usRT absorber, it is compared with the absorber for 30usRT and the volume ratio per unit refrigeration capacity.

  As can be seen from Table 2, the volume of the present embodiment can be about 50% of the conventional falling film absorber, which can greatly contribute to downsizing.

  As described above, in this embodiment, the absorbing liquid concentrated in the regenerators 6 and 7 is cooled at the inlet of the absorber 1, so that the absorbing liquid having a saturation pressure lower than the evaporator pressure is used as the driving flow. The ejectors 11 and 11A are used as the absorber 1. The ejectors 11 and 11A are composed of nozzle sections 12 and 12A, suction sections 13 and 13A, mixing sections 14 and 14A, and diffuser sections 15 and 15A. The ejectors 11 and 11A are low-pressure and high-speed that are driven by the nozzle sections 12 and 12A. It is a device that creates a jet, sucks and sucks suction fluid by the entrainment action of the jet in the suction sections 13 and 13A, and gradually recovers the pressure through the mixing sections 14 and 14A and the diffuser sections 15 and 15A. A method of applying the ejectors 11 and 11A to the absorber 1 is as follows. The drive flow of the ejectors 11 and 11A is an absorption liquid which is concentrated in the regenerators 6 and 7 and then brought into a supercooled state, and the suction flow is a refrigerant vapor generated in the evaporator 9. By injecting the absorption liquid into the suction sections 13 and 13A as a high-speed spray flow from the nozzle sections 12 and 12A, the refrigerant vapor generated in the evaporator 9 is caused by the saturation pressure difference with the absorption liquid and the entrainment action of the jet flow. Sucked. By performing this continuously, the evaporator 9 maintains a constant pressure and exhibits a refrigerating capacity. The refrigerant vapor sucked by the suction sections 13 and 13A and absorbed into the two-phase flow absorbs the refrigerant vapor while recovering the pressure by the mixing sections 14 and 14A / diffuser sections 15 and 15A. This completes the absorption process. In this way, the absorber 1 can be highly efficient and downsized.

  In this embodiment, since the two-stage ejectors 11 and 11A are provided, the performance of the absorber 1 can be further improved, but even with only one-stage ejector, compared to the conventional example. High efficiency and downsizing can be achieved. In the case of a single-stage ejector, the performance of the absorber will be lower than in the case of a two-stage ejector, but this is advantageous in terms of miniaturization.

  Next, a second embodiment of the present invention will be described with reference to FIG. FIG. 5 is a block diagram of the main part of the absorber 1 in the absorption refrigerator according to the second embodiment of the present invention.

  In the second embodiment, the first-stage nozzle portion 12 and the second-stage nozzle portion 12A of the first embodiment are tapered nozzles, whereas the two-phase flow laval nozzle is used, and the absorbing liquid flowing into the ejector However, the other points are basically the same as the first embodiment. Although only the first stage ejector 11 is shown in FIG. 5, the second stage ejector 11 </ b> A has the same configuration as the first stage ejector 11.

  The two-phase flow laval nozzle 12 includes a tapered portion 12a, a throat portion 12b, and a divergent portion 12c. Since the tapered portion 12a is a liquid single-phase subsonic flow, the flow passage cross-sectional area is reduced and the pressure is reduced and accelerated. In the throat portion 12b, when the absorption liquid pressure becomes equal to or lower than the saturation pressure, the liquid is boiled under reduced pressure to become a gas-liquid two-phase flow, and the flow reaches the speed of sound. The divergent portion 12c is further depressurized and accelerated as the flow passage cross-sectional area increases due to the supersonic flow. By using this two-phase flow Laval nozzle 12, the pressure of the jet of absorbing liquid at the nozzle outlet is lower than that when using a tapered nozzle, the flow velocity is increased, and the droplets are refined. The refrigerant vapor can be sucked by the entrainment effect of the jet more than the case. When the two-phase flow Laval nozzle 12 is used, the jet flow from the nozzle is a supersonic flow, but a shock wave (shock) is generated in the mixing unit 14 because it is reduced to a subsonic flow, and the refrigerant vapor and the absorption liquid As the pressure increases, the absorption capacity increases (the absorption liquid can be supersaturated).

  In both the first and second embodiments, the ejector is used as an absorber. However, the difference between the two is the dominant factor for the absorbing liquid to suck the refrigerant vapor. That is, the first embodiment is predominantly sucked by the saturation pressure difference between the driving liquid absorption liquid and the refrigerant vapor generated in the evaporator, whereas the second embodiment is the absorption liquid saturation pressure difference. The entrainment action by the flow velocity of the driving flow sprayed by the nozzle is a dominant factor rather than the suction by the nozzle.

  Next, a third embodiment of the present invention will be described with reference to FIG. FIG. 6 is a block diagram of the main part of the absorber 1 in the absorption refrigerator according to the third embodiment of the present invention.

  This third embodiment is different from the second embodiment in that a heating heat exchanger 16 'for raising the temperature of the absorbent is used instead of the cooling heat exchanger 16, and the other points are different. Is basically the same as the second embodiment.

  The performance of the Laval nozzle greatly affects the enthalpy difference between the absorption liquid at the Laval nozzle inlet and outlet, and the nozzle performance improves as the enthalpy difference increases. Therefore, in this third embodiment, the temperature of the absorbing liquid is increased at the ejector inlet to increase the enthalpy difference and improve the nozzle efficiency. Since the performance of the ejector is greatly affected by the jet flow from the nozzle, the performance of the ejector is improved by improving the nozzle performance as in the third embodiment.

  Next, a fourth embodiment of the present invention will be described with reference to FIG. FIG. 7 is a block diagram of the main part of the absorber 1 in the absorption refrigerator according to the fourth embodiment of the present invention.

  The fourth embodiment differs from the first embodiment in that a cooling heat exchanger 16A is provided on the inlet side of the second stage ejector 11A, and other points are basically the same as those of the first embodiment. Are the same. The effect similar to that of the cooling heat exchanger 16 can be achieved by the second stage ejector 11A by the cooling heat exchanger 16A.

  Next, a fifth embodiment of the present invention will be described with reference to FIG. FIG. 8 is a block diagram of the main part of the absorber 1 in the absorption refrigerator according to the fifth embodiment of the present invention.

  The fifth embodiment is different from the third embodiment in that a heating heat exchanger 16'A is provided on the inlet side of the second stage ejector 11A, and other points are basically the same as those in the third embodiment. Are the same. This heating heat exchanger 16'A can achieve the same effect as that of the heating heat exchanger 16 'with the second stage ejector 11A.

  Next, a sixth embodiment of the present invention will be described with reference to FIG. FIG. 9 is a block diagram of the main part of the absorber 1 in the absorption refrigerator according to the sixth embodiment of the present invention.

  The sixth embodiment is different from the first embodiment in that the ejector 11 is disposed in the evaporator 9, and the other points are basically the same as the first embodiment. By disposing the ejector 11 in the evaporator 9, the pressure loss of the suction part 13 of the ejector 11 can be remarkably reduced as compared with the first embodiment, and the performance of the absorber can be improved. . In addition, the ejector 11 is provided in only one stage, the cold water pipe 93 is formed in a cylindrical shape, and the ejector 11 is disposed in the cold water pipe 93, whereby the absorber 1 can be further reduced in size.

  Next, a seventh embodiment of the present invention will be described with reference to FIG. FIG. 10 is a main part configuration diagram of the absorber 1 in the absorption refrigerator according to the seventh embodiment of the present invention.

  The seventh embodiment is different from the sixth embodiment in that the ejector 11 is disposed in close contact with or adjacent to the side surface of the evaporator 9 and an opening serving as a passage for intake steam is provided. This is basically the same as the first embodiment. With the configuration of the seventh embodiment, the pressure loss of the suction portion 13 of the ejector 11 can be significantly reduced as compared with the first embodiment, and the performance of the absorber can be improved.

It is a block diagram of the double effect absorption refrigerator which is 1st Example of this invention. It is a principal part block diagram of the absorber of 1st Example. It is a characteristic view which shows the relationship between the absorber nozzle entrance density | concentration of 1st Example, and a density | concentration difference. It is a characteristic view which shows the relationship between the absorber nozzle inlet_port | entrance density | concentration of 1st Example, and COP. It is a principal part block diagram of the absorber in the absorption refrigerator of 2nd Example of this invention. It is a principal part block diagram of the absorber in the absorption refrigerator of 3rd Example of this invention. It is a principal part block diagram of the absorber in the absorption refrigerator of 4th Example of this invention. It is a principal part block diagram of the absorber in the absorption refrigerator of 5th Example of this invention. It is a principal part block diagram of the absorber in the absorption refrigerator of 6th Example of this invention. It is a principal part block diagram of the absorber in the absorption refrigerator of 7th Example of this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 ... Absorber, 3 ... Low temperature solution heat exchanger, 5 ... High temperature solution heat exchanger, 6 ... High temperature regenerator, 6A ... Burner, 7 ... Low temperature regenerator, 8 ... Condenser, 9 ... Evaporator, 11th 1st stage ejector, 11A ... 2nd stage ejector, 12 ... 1st stage nozzle part, 12A ... 2nd stage nozzle part, 13 ... 1st stage suction part, 13A ... 2nd stage suction part, 14 ... 1st stage mixing part , 14A ... 2nd stage mixing part, 15 ... 1st stage diffuser part, 15A ... 2nd stage diffuser part, 16, 16A ... Heat exchanger for cooling, 16 ', 16'A ... Heat exchanger for heating, 17 ... First stage cooling heat exchanger, 17A ... Second stage cooling heat exchanger, 18 ... Solution pump, 19 ... First stage solution pump, 19A ... Second stage solution pump, 91 ... Refrigerant pump, 92 ... Refrigerant spray Piping, 93 ... cold water pipe.

Claims (9)

In an absorption refrigerator comprising an evaporator, an absorber, a condenser, a regenerator, a solution heat exchanger, pumps, and piping connecting them,
The absorption refrigerator includes an ejector that uses the absorption liquid concentrated in the regenerator as a drive source and sucks the refrigerant vapor inside the evaporator and absorbs it into the absorption liquid.   2. The absorption refrigerator according to claim 1, wherein an absorption liquid having a saturation pressure lower than an evaporator pressure is used as a drive source of the ejector.   2. The absorption refrigerator according to claim 1, wherein a cooling heat exchanger is disposed on the outlet side of the ejector. In an absorption refrigerator comprising an evaporator, an absorber, a condenser, a regenerator, a solution heat exchanger, pumps, and piping connecting them,
The absorber includes an ejector that uses the absorption liquid concentrated in the regenerator as a drive source and sucks the refrigerant vapor inside the evaporator and absorbs it into the absorption liquid.
The ejector uses a two-phase flow laval nozzle as a nozzle part.   5. The absorption refrigerator according to claim 4, wherein a heating heat exchanger is disposed on the inlet side of the absorption liquid of the ejector.   5. The absorption refrigerator according to claim 1, wherein a solution pump for increasing the pressure of the absorption liquid is disposed on the inlet side of the ejector.   The absorption refrigerator according to claim 1 or 4, wherein the ejector is provided in a plurality of stages in series.   The absorption refrigerator according to claim 1 or 4, wherein the absorber is configured by arranging the ejector in a space of the evaporator. 5. The absorption refrigerator according to claim 1 or 4, wherein the absorber has an ejector disposed in close contact with or adjacent to a side surface of the evaporator and an opening serving as a passage for intake steam is provided on a wall surface. .

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