JP2568769B2 - Absorption refrigerator - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an absorption refrigerator used for cooling and heating, and more particularly to an arrangement of heat transfer tubes of an absorber and an evaporator and a dispersion plate installed in a heat transfer tube group.

[0002]

2. Description of the Related Art In general, an absorption refrigerator has an evaporator, an absorber,
Low-temperature regenerator, high-temperature regenerator, and a pump connecting them,
It consists of a heat exchanger. FIG. 9 is a principle system diagram. Water is passed through the tubes of the tube group in the evaporator,
Water is sprayed outside the pipe as a refrigerant, and the water in the pipe is cooled by the latent heat of evaporation, and is supplied to a cooler or the like as cold water.
The water vapor evaporated by the evaporator flows into the absorber, and is absorbed by an absorbing solution (such as a lithium bromide solution) sprayed on the outer surface of the tube group in the absorber, and the absorbed heat generated at this time is cooling water passing through the tube. Cooled by. The concentration of the absorbing liquid that has absorbed the water vapor in the absorber decreases, and the absorbing power decreases. Then, after preheating this through a heat exchanger, it is sent to a high-temperature regenerator and a low-temperature regenerator and concentrated by heating. As a heat source of the high-temperature regenerator, heat obtained by burning gas, oil, or the like is generally used. Steam generated by the high-temperature regenerator is used as the heat source of the low-temperature regenerator. The steam generated in the low-temperature regenerator and the high-temperature regenerator is finally cooled and condensed by the cooling water in the condenser. The condensed water is supplied to an evaporator as an evaporation medium.

[0003] Among the components of the absorption refrigerator, particularly important in terms of the performance as an absorption refrigerator are an absorber and an evaporator.

[0004] As described above, the evaporator evaporates an evaporating medium such as water to cool a cooling medium such as water by the latent heat. The evaporator mainly includes a heat transfer tube group in a staggered or lattice arrangement and a spraying device for spraying an evaporation medium on the surface thereof. Generally, water is flowed as a cooling medium into the heat transfer tube, and water sprayed on the outer surface of the heat transfer tube is
Since the inside of the system is kept at a low pressure, the water evaporates and its latent heat cools the water flowing in the heat transfer tube and is used for cooling or the like. The vapor generated in this evaporator is guided to the absorber as described above. The absorber, like the evaporator, is mainly composed of a group of heat transfer tubes arranged in a staggered or lattice arrangement and a spraying device for spraying the absorbing liquid on the surface thereof. In general, a lithium bromide solution is used as the absorbing liquid, and is sprayed on the outer surface of the heat transfer tube. The vapor pressure of lithium bromide is much lower than that of water, and the vapor flowing into the absorber from the evaporator is absorbed by the absorbent based on the difference in vapor pressure. At this time, since the temperature of the absorbing liquid increases due to the heat of absorption, a cooling medium such as water is flown in the heat transfer pipe to cool the pipe.

In order to improve the performance of the absorption refrigerator, it is necessary to increase the effective pressure difference between the vapor pressure of the evaporation medium in the evaporator and the vapor pressure of the absorption liquid in the absorber from the above-mentioned principle of the absorption cycle operation. There is. For this purpose, first, the flow resistance (pressure loss) of the steam in the tube group of the absorber and the evaporator is reduced, and the pressure difference available for absorbing the evaporation in the absorber is increased. . The second is to improve absorption heat transfer characteristics in the absorber. There are three main ways to do this. One measure, which is not directly related to the present invention, is to form fins on the surface of the heat transfer tube as described in JP-A-63-6363 in order to improve the absorption heat transfer characteristics of a single heat transfer tube. The purpose is to increase the holding area of the absorbing liquid while increasing the heat area. Another measure is to prevent accumulation of non-condensable gases, such as air, which provide heat transfer resistance on the steam side. Another measure is to supply and distribute the absorbing liquid evenly to each heat transfer tube in the absorber to eliminate useless heat transfer tubes that are not used for absorption.

The prior art of these performance improvement measures includes:
As described in Japanese Patent No. 1187335, in the evaporator, the upstream portion of the steam is arranged in a heat transfer tube array having a narrow pitch lattice arrangement, and the downstream portion having a large steam flow is arranged in a staggered arrangement having a wide pitch. There is a method in which the flow resistance of steam in the tube bank is made uniform by forming a staggered array with a large pitch in the upstream portion of the steam and a group of heat transfer tubes in a grid array with a narrow pitch in the downstream portion of the steam. Further, as described in Japanese Patent Application Laid-Open No. Sho 62-155482, there is a method in which non-condensable gas is prevented from being accumulated and air is extracted by providing a partition plate parallel to a tube row in a heat transfer tube group of an absorber.

[0007]

In the above prior art, the heat transfer tube group of the absorber and the evaporator is of an integral structure, and all the vapor must pass through the heat transfer tube group uniformly. In the evaporator, the steam generated at the upstream of the steam flows across the heat transfer tube group to the steam outlet. In the absorber, the gas flows uniformly across the heat transfer tube group from the steam inlet to the steam downstream. That is, the passage distance of the steam through the heat transfer tube group is equal to the depth of the heat transfer tube group in the vapor outflow direction in the evaporator and in the steam inflow direction in the absorber, and the flow resistance of the steam is generated accordingly. This not only causes an increase in pressure loss in the heat transfer tube group and causes a decrease in the performance of the absorption refrigerator, but also limits the depth of the heat transfer tube group, and consequently limits the overall configuration of the absorption refrigerator. Resulting in. Furthermore, in the absorber, the heat transfer tubes near the steam inlet have a large amount of steam supply, so the amount of absorption and heat transfer per unit heat transfer area increases, and the amount of absorption decreases toward the back of the heat transfer tube group. Will cause an imbalance. This does not mean that the heat transfer tubes downstream of the steam in the absorber are effectively used, and hinders the performance improvement of the absorber.

Further, in the absorber, a low-pressure portion is formed in the heat transfer tube group having an integral structure due to the flow resistance of steam, and even if a partition plate is provided, non-condensable gas stays there, and the absorption heat transfer Significantly degrade performance. On the other hand, the supply of the absorbing liquid in the absorber is performed by spraying or dripping from the top of the heat transfer tube group and gradually flowing downward while dripping the heat transfer tube group. In the case of horizontal orientation, for example, the dropping absorption liquid is flooded with steam, and the supply amount of the absorption liquid is significantly reduced in some of the heat transfer tubes below the heat transfer tube group, so that the absorption heat transfer performance is reduced. A similar problem relates to the application of the evaporation medium of the evaporator.

Both of the above problems are closely related to the arrangement of the heat transfer tubes in the absorber or evaporator, that is, the structure of the heat transfer tube group. The present invention has been made based on the idea that reduction of pressure loss (flow resistance of steam) in the heat transfer tube group leads to solving all problems. First, the flow resistance of steam in the heat transfer tube group is reduced. And increase the pressure difference available for absorbing steam in the absorber, thereby making the pressure distribution in the tube group uniform, suppressing the accumulation of non-condensable gas, and further reducing non-condensable gas. It is an object of the present invention to form a low-pressure region near a bleeding port for bleeding to enable efficient bleeding of non-condensable gas.

[0010]

SUMMARY OF THE INVENTION In order to reduce the flow resistance of steam in a heat transfer tube group in an absorber, the absorber is transferred to the absorber instead of a conventional integrated tube group structure. A pipe in which a plurality of tube group blocks separated by a steam flow path in a cross section viewed from the longitudinal direction of the heat pipe are divided, and a width of the steam flow path in a cross section viewed from the longitudinal direction of the heat transfer pipe is such that the heat transfer pipes are densely arranged. An absorber having a tube arrangement in which the interval is larger than the maximum value of the interval between adjacent heat transfer tubes in the group block and a plurality of tube group blocks are surrounded by the steam flow path . The yo Ri Specifically, surrounded by the steam channel of the plurality of tube bundle block in the cross section viewed absorber from the heat transfer tube longitudinal direction maximum value greater spacing than the spacing between adjacent heat transfer tube in the block, and A tube group block in which heat transfer tubes are densely arranged in a cross section viewed from the surface of the steam flowing into the absorber, wherein the tube block is divided by a steam flow path having an interval larger than a maximum value of an interval between adjacent heat transfer tubes in the block. Make an absorber with groups. Depending on the shape of the absorber and the steam flow rate, the heat transfer tubes belonging to one tube group block are arranged so that the number of rows in the direction perpendicular to the steam inflow direction is 20 or less.

Further, in the absorber, in order to suppress the non-condensable gas from staying in the heat transfer tube group and to facilitate the bleeding of the gas, the tube group block has a maximum distance between adjacent heat transfer tubes in the block. In an absorber having a tube group divided by a steam path with a larger interval, the tube group block closest to the absorbent outlet or the non-condensable gas extraction port has a heat transfer tube as compared to the other tube group blocks. The number should be large or the heat transfer tube pitch should be narrow.

[0012] In order to reduce the flow resistance of steam in the heat transfer tube group in the evaporator, the evaporator is not a conventional one-piece tube group structure like the absorber, but rather from the longitudinal direction of the heat transfer tube. thereby divided into a plurality of tube bundle blocks separated by steam flow path in the observed cross-section, the width of the steam path in a cross section as seen from the heat transfer tube longitudinal direction, of the tube bundle in blocks densely arranged heat transfer tube An evaporator having a tube arrangement in which the interval is larger than the maximum value of the interval between the adjacent heat transfer tubes and a plurality of tube group blocks are surrounded by the steam flow path . The yo Ri Specifically, surrounded by the steam channel of the plurality of tube bundle block in the cross section viewed evaporator from the heat transfer tube longitudinal direction maximum value greater spacing than the spacing between adjacent heat transfer tube in the block, and A pipe group block in which heat transfer tubes are densely arranged in a cross section as viewed from a steam outflow surface from the evaporator is divided by a steam flow path having an interval larger than a maximum value of an interval between adjacent heat transfer tubes in the block. Evaporator with group. Depending on the evaporator shape and steam flow rate,
The number of rows in the direction perpendicular to the steam inflow direction of the heat transfer tubes belonging to one pipe group block is arranged to be 20 rows or less.

In order to make the dispersion of the absorbing liquid in the absorber and / or the dispersion of the evaporating medium in the evaporator uniform even in the lower part of the tube group, a dispersion plate for simultaneously passing the liquid and the gas through the heat transfer tube group. Is placed horizontally. This dispersion plate is more effective in an absorber or evaporator having a plurality of tube bank blocks if it is installed horizontally in the vapor flow path.

[0014]

According to the present invention, the steam in the absorber or evaporator mainly flows through the steam flow path and spreads throughout the absorber or evaporator. The flow resistance of the steam in the steam flow path is much smaller than the flow resistance in the tube group block in which the heat transfer tubes are densely arranged, and is negligible. The vapor evaporated in the tube group block of the evaporator flows into the steam flow path through the shortest distance in the tube group in the tube group block. Similarly, the steam in the tube group block of the absorber flows from the steam flow path through the shortest distance in the tube group in the tube group block and is absorbed into the tube group block. In a conventional tube bundle having an integral structure, the passage distance in the tube bundle when steam flows in and out corresponds to the depth of the tube bank in the steam flow direction. Therefore, in the present invention, since the passage distance of the steam in the tube bank can be shortened, the flow resistance of the steam at that time can be greatly reduced. Since the pressure loss in the tube group can be reduced, the pressure distribution in the absorber or the evaporator can be made uniform, and the amount of steam absorbed in each heat transfer tube in the absorber can also be made uniform.

This uniform pressure distribution can prevent the non-condensable gas from staying in the tube bank block. Further, the non-condensable gas is discharged near the bleed port or with the absorbing liquid. In this case, a low-pressure region can be easily formed by increasing the number of tubes or narrowing the pitch of the heat transfer tubes in the tube block near the discharge port compared to other tube blocks, and non-condensing. The volatile gas is sucked there, and it is possible to extract air with high efficiency.

The dispersion plate, which is disposed in the heat transfer tube group and allows liquid and gas to pass at the same time, receives the absorbing liquid or the evaporating medium flowing down from above into the absorber or evaporator without obstructing the vapor flow. Redistribute. Thus, the absorbing liquid or the evaporating medium can be uniformly supplied to the heat transfer tube in the lower part of the vessel. This effect is achieved by arranging the dispersion plate horizontally in the vapor flow path in the absorber or evaporator having a plurality of tube bank blocks because the absorbing liquid or the evaporating medium is flooded in the vapor flow path. Is even more effective.

[0017]

1 (1) and (2) are schematic cross-sectional views of two embodiments of an absorber of an absorption refrigerator according to the present invention as viewed from the longitudinal direction of a heat transfer tube. 1 is a heat transfer tube, 2 is a tube group block, 3 is a steam flow path, 4 is an inflow portion of steam (steam) flowing from an evaporator, 5 is an absorbent dispersion device, 6 is an absorbent, and 7 is an absorbent outlet. (This also serves as a bleed port in this embodiment). FIG. 1A shows an embodiment in which the steam generated in the evaporator flows in the horizontal direction through the steam inflow section 4. The vapor inflow section 4 may be provided with an eliminator or the like in order to prevent the absorption liquid from scattering, but may have an opening where nothing is provided. Four tube group blocks in which the heat transfer tubes 1 are densely arranged are formed in the absorber, and each tube group block is surrounded by the steam flow path 3. The steam flowing from the evaporator through the steam inflow section 4 spreads throughout the absorber through the steam flow path 3 and is absorbed by the absorbing liquid dispersed on the outer surface of each heat transfer tube. . At this time, the absorbing liquid is heated by the absorption heat, but is cooled by the cooling water flowing in the heat transfer tube. The absorbing liquid drops from the upper heat transfer pipe to the lower heat transfer pipe, and flows out of the absorber through the absorbing liquid discharge port 7. The absorbent outlet 7 may be provided with a bleeding port for non-condensable gas such as air, or the ejector may discharge the non-condensable gas and the absorbent simultaneously. FIG. 1 (2) shows that the vapor generated in the evaporator passes through the vapor inflow section 4 and flows vertically from the upper part of the absorber. Similarly, in some embodiments, steam may flow vertically from the bottom to the top of the absorber.

Next, the principle of the present invention will be described with reference to the results of a numerical analysis of the basic arrangement of tube banks in the absorber. In this numerical analysis, we solve the conservation laws of mass and momentum for the flow,
The amount of steam absorption in the heat transfer tube bank is calculated based on the empirical formula. The details of this analysis model can be found in the Proceeding of the
Second International Symposium on Condensers andco
ndensation (1990), pp.235-244. FIG. 2 shows the results of numerical analysis 3
It is a figure which shows the cross section seen from the longitudinal direction of the heat transfer tube of the heat transfer tube group of the kind of absorber. All three types of absorbers have the same volume (0.75 m in height, 0.33 m in depth, 2.0 in the heat transfer tube longitudinal direction).
m), and the number of arranged heat transfer tubes is also equal to 336.
The steam flows in from the left side. In each case, the arrangement of the heat transfer tubes (diameter 15.88 mm) is a staggered arrangement.
The "rectangular" arrangement of (a) is a conventional tube bank of integral construction,
The horizontal tube pitch is 23.3 mm in the heat transfer tube arrangement area 8,
The tubes are arranged at a vertical pipe pitch of 26.7 mm.
The “comb-type” arrangement of (b) is an arrangement in which the tube block divided by the steam flow path is in contact with the inner wall surface of the absorber,
The pipe pitch in the horizontal direction is 17.0 mm, and the pipe pitch in the vertical direction is 19.5 mm. The "block type" arrangement shown in (c) is an arrangement in which the tube group blocks are all surrounded by steam flow paths, and the horizontal pipe pitch is 17.0 mm and the vertical pipe pitch is 19.5 mm. FIG. 3 shows a numerical analysis result of the pressure distribution of steam at the pressure plotting position 9 shown in FIG. 2 for these tube groups. According to the analysis results, the pressure loss (difference between the pressure at the steam inlet and the pressure at the lowest pressure point) is clearly higher in the array divided into tube bundle blocks than in the “rectangular” array of the monolithic structure. It can be seen that the pressure distribution at the vapor inlet of the absorber is low, and the pressure difference between the evaporator and the evaporator is large with the same number of heat transfer tubes. This tendency is even greater for the "block-type" array than for the "comb-type" array.

FIGS. 4 (1) and 4 (2) show FIGS. 1 (1) and 1 (2).
FIG. 3 shows schematic diagrams of cross sections of the same absorber viewed from the longitudinal direction of the heat transfer tube. 1 has a tube group block 2 surrounded by a steam flow path 3, while a tube group block 10 in contact with an absorbent outlet or a bleed port 7 has a smaller number of heat transfer tubes than other tube group blocks. Therefore, the pressure near the bleed port 7 is reduced. In this way, non-condensable gas such as air in the absorber can be efficiently extracted, and the heat transfer characteristics are improved.

FIGS. 5 (1) and 5 (2) also show FIGS. 1 (1) and 1 (2).
FIG. 3 shows schematic diagrams of cross sections of the same absorber viewed from the longitudinal direction of the heat transfer tube. As in FIG. 1, a dispersion plate 11 having a tube group block 2 surrounded by a steam flow path 3 and allowing the vapor and the liquid to pass at the same time is installed in the steam flow path, and the absorbing liquid is redistributed. As a result, the absorbing liquid is distributed to all the heat transfer tubes, so that the steam can be efficiently absorbed.

FIGS. 6A and 6B show such a dispersion plate 1.
FIG. 2 is a cross-sectional view showing each of two examples 1; FIG. 1A shows a short cylinder 112 through which a gas passes through the perforated plate 111 and is projected upward. The liquid accumulated on the perforated plate 111 is dropped from the holes of the perforated plate 111. FIG. 2B shows a short cylinder 113 having a relatively large diameter penetrating the plate 114 and projecting upward.
The gas overflows into the inside of the cylinder 113 and flows down in a wet state on the inner wall of the cylinder 113, and the gas flows through the center of the cylinder 113.

FIGS. 7 (1) and 7 (2) are schematic views showing two embodiments of the evaporator of the absorption refrigerator according to the present invention, as viewed from the longitudinal direction of the heat transfer tube. Four tube group blocks 2 in which heat transfer tubes 1 are densely arranged are formed in the evaporator, and each tube group block is surrounded by a steam flow path 3. From the upper part of the tube group, an evaporating medium 13 such as water is sprinkled from the evaporating medium sprinkling device 12 onto the outer surface of the heat transfer tube and evaporated. The evaporated vapor flows out from the vapor outflow section 14 through the vapor flow path 3 to the absorber.
The evaporating medium that has reached the lower portion of the evaporator without being completely evaporated exits the evaporator through the evaporating medium outlet 15.

FIGS. 8 (1) and 8 (2) show FIGS. 7 (1) and 7 (2).
And a schematic diagram of a cross section of the same evaporator as viewed from the longitudinal direction of the heat transfer tube. 7 and a dispersion plate 11 (similar to (1) or (2) in FIG. 6), which has a tube group block 2 surrounded by a steam flow path 3 and simultaneously passes steam and liquid through the steam flow path. ) And redistribute the liquid. Thereby, water as an evaporation medium is distributed to all the heat transfer tubes, and the heat transfer characteristics are improved.

[0024]

According to the present invention, the flow resistance of steam in the absorber or evaporator of the absorption refrigerator can be reduced, and a high-performance absorption refrigerator can be provided. Also, in the absorber, the pressure distribution in the entire absorber can be made uniform by forming a block tube group, and non-condensation can be achieved by artificially reducing the pressure only in the vicinity of the bleeding port as shown in FIG. Effluent gas can be efficiently extracted, and the absorption heat transfer characteristics in the absorber can be improved. In addition, by installing a dispersion plate of liquid that does not affect the vapor flow in the tube group of the absorber or evaporator, the absorbing liquid or the evaporating medium liquid is evenly sprayed on the heat transfer tube at the bottom of the tube group. The heat transfer characteristic can be further improved without generating a useless pipe such that the liquid is not supplied. As described above, the present invention can provide a high-performance absorption refrigerator, and can exhibit a refrigerating capacity higher than that of the conventional technology with a small device.

[Brief description of the drawings]

FIG. 1 is a schematic cross-sectional view in the longitudinal direction of a heat transfer tube of an absorber of an absorption refrigerator according to one embodiment of the present invention;

FIG. 2 is a schematic view of a cross section of an absorber according to the prior art used for numerical analysis and the present invention,

FIG. 3 is a diagram showing a pressure distribution by numerical analysis of the tube group shown in FIG. 2;

FIG. 4 is a schematic cross-sectional view in the longitudinal direction of a heat transfer tube of an absorber of an absorption refrigerator according to another embodiment of the present invention;

FIG. 5 is a schematic cross-sectional view of an absorber according to still another embodiment of the absorption refrigerator of the present invention;

FIG. 6 is a schematic sectional partial view of a dispersion plate used in the present invention,

FIG. 7 is a schematic cross-sectional view in the longitudinal direction of a heat transfer tube of an evaporator of an absorption refrigerator according to one embodiment of the present invention;

FIG. 8 is a schematic sectional view of an evaporator according to another embodiment of the absorption refrigerator of the present invention,

FIG. 9 is a conceptual diagram of the entire system of the absorption refrigerator.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 ... Heat transfer tube 2 ... Tube group block 3 ... Steam flow path 4 ... Inflow part of the steam which flows in from an evaporator 5 ... Absorbing liquid spraying device 6 ... Absorbing liquid 7 ... Absorbing liquid discharge port or bleeding port 8 ... Heat transfer tube arrangement area 9: Pressure plotting position 10: Tube group block adjacent to absorption liquid outlet or bleeding port 7: Dispersion plate for passing vapor and liquid simultaneously 12: Evaporation medium dispersing device 13: Evaporation medium 14: Vapor outlet 15: Evaporation medium Vent

 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Fumio Takahashi 1168 Moriyamacho, Hitachi City, Ibaraki Prefecture Inside Energy Laboratory, Hitachi, Ltd. (56) References JP-A-4-309764 (JP, A) Jpn.

Claims (9)

(57) [Claims] 1. An absorption refrigerator having an evaporator for evaporating liquid on the surfaces of a plurality of heat transfer tubes to generate steam, and an absorber for absorbing steam flowing from the evaporator with the absorbent on the surfaces of the plurality of heat transfer tubes. in, absorber, in a cross section as viewed from the heat transfer tube longitudinal direction, a plurality of tube bundle territory was densely arranged heat transfer tube
Area and the maximum distance between adjacent heat transfer tubes in each tube bank area
Also has a large spacing steam flow path, and the heat transfer tubes are densely arranged
Each of the plurality of tube bank regions is surrounded by the steam flow path.
Absorption refrigerating machine, characterized in that there. 2. An absorption refrigerator having an evaporator for evaporating liquid on the surfaces of a plurality of heat transfer tubes to generate steam and an absorber for absorbing the steam flowing from the evaporator with the absorbent on the surfaces of the plurality of heat transfer tubes. In the absorber, in the cross section viewed from the longitudinal direction of the heat transfer tubes, the steam having a larger interval than the maximum value of the interval between the plurality of tube group regions in which the heat transfer tubes are densely arranged and the adjacent heat transfer tube in each tube group region. Having a flow path, each of the plurality of tube group areas where heat transfer tubes are densely arranged are surrounded by the steam flow path.
And the cross section seen from the vapor inflow side to the absorber
Thus, each of the plurality of tube bank regions where heat transfer tubes are densely arranged is
While the distance is greater than the maximum distance between adjacent heat transfer tubes in the area
An absorption refrigerator characterized by being divided by a separate steam flow path . 3. A steam flow of a heat transfer tube belonging to one tube bank region.
The number of columns in a direction perpendicular to the input direction is 20 or less.
The absorption refrigerator described . 4. A method of evaporating liquid on the surfaces of a plurality of heat transfer tubes to evaporate.
Vaporizing evaporator and the vapor flowing from the evaporator
It has an absorber to absorb with the absorption liquid on the surface of several heat transfer tubes
Absorption refrigerator, the absorber is viewed from the longitudinal direction of the heat transfer tube.
Tube section with densely arranged heat transfer tubes and each tube
Spacing greater than the maximum spacing between adjacent heat transfer tubes in the group area
And a plurality of the steam flow paths, wherein the heat transfer tubes are densely arranged.
Each of the tube bundle regions is separated by the steam flow path; and
The tube group closest to the absorbent outlet or bleed port in the absorber
The number of heat transfer tubes is larger or the heat transfer is larger
An absorption refrigerator characterized by a narrow pipe pitch . 5. In the tube bundle area in an absorber or
Dispersion that allows liquid and gas to pass simultaneously through the vapor flow path
The absorption refrigerator according to any one of claims 1 to 4, wherein a plate is arranged . 6. A method for evaporating a liquid on the surface of a plurality of heat transfer tubes to evaporate.
Vaporizing evaporator and the vapor flowing from the evaporator
It has an absorber to absorb with the absorption liquid on the surface of several heat transfer tubes
In the absorption refrigerator, the evaporator is located in the longitudinal direction of the heat transfer tube.
In the cross section seen, multiple tube groups with densely arranged heat transfer tubes
Area and the maximum distance between adjacent heat transfer tubes in each tube bank area
Also has a large spacing steam flow path, and the heat transfer tubes are densely arranged
Each of the plurality of tube bank regions is surrounded by the steam flow path.
An absorption refrigerator. 7. An absorption refrigerator having an evaporator for evaporating liquid on the surfaces of a plurality of heat transfer tubes to generate steam and an absorber for absorbing the steam flowing from the evaporator with the absorbent on the surfaces of the plurality of heat transfer tubes. in the evaporator, in the cross section seen from the heat transfer tube longitudinal direction, a plurality of tube bundle territory was densely arranged heat transfer tube
Area and the maximum distance between adjacent heat transfer tubes in each tube bank area
Also has a large spacing steam flow path, and the heat transfer tubes are densely arranged
Each of the plurality of tube bank regions is surrounded by the steam flow path.
And the cross section seen from the vapor outflow surface from the evaporator
Thus, each of the plurality of tube bank regions where heat transfer tubes are densely arranged is
While the distance is greater than the maximum distance between adjacent heat transfer tubes in the area
An absorption refrigerator characterized by being divided by a separate steam flow path . 8. A steam flow of a heat transfer tube belonging to one tube bank region.
8. The number of columns in a direction perpendicular to the exit direction is 20 or less.
The absorption refrigerator described . 9. In the tube bank area in an evaporator or
Dispersion that allows liquid and gas to pass simultaneously through the vapor flow path
The absorption refrigerator according to any one of claims 6 to 8, wherein a plate is arranged .