KR100522197B1 - High desorber - Google Patents

Abstract

The present invention relates to a high temperature regenerator used in absorption chillers and absorption chillers, more specifically, to increase the flame temperature by applying a pre-mixed surface combustion method, a plurality of heat transfer unit consisting of a plurality of associated heat pipe bundles in series ( Up and down) or in parallel (left and right) is arranged to maximize the heat transfer area, it is characterized in that it is possible to increase the efficiency due to improved heat transfer and fuel consumption and to reduce the size of the high temperature regenerator itself.

Description

High Temperature Regenerator {HIGH DESORBER}

The present invention relates to a high temperature regenerator used in absorption chillers and absorption chillers, in particular, to minimize the combustion space by applying a pre-mixed surface combustion method, and select a plurality of heat transfer unit consisting of a plurality of associated heat pipe bundles in series or parallel The present invention relates to a high temperature regenerator that realizes miniaturization and high efficiency.

Generally, the absorption chiller uses water as a refrigerant and lithium bromide as an absorbent, and is a device for making cold water using a combustion device or a high temperature fluid as a heating source, and the high temperature regenerator is housed in the absorption chiller or absorption cold / hot water It is a heating apparatus that continuously regenerates a thin absorbent liquid (lithium bromide aqueous solution) into a concentrated absorbent liquid.

1 is a view showing the configuration of a general absorption chiller.

As shown, the absorption chiller is an absorber (3), a high temperature regenerator (7) and a burner (71) provided therein, a low temperature regenerator (6), a condenser (5), an evaporator (2), a low temperature solution heat exchanger (8). ), A high temperature solution heat exchanger (9), an absorption liquid circulation pump (32), a refrigerant pump (23) and piping.

The absorber 3 and the evaporator 2 integrally form the lower body 1, and the cryogenic regenerator 6 and the condenser 5 integrally form the upper body 4, and on the lower body 1 The upper body 4 is located, and the low temperature solution heat exchanger 8 and the high temperature solution heat exchanger 9 are positioned below the lower body 4.

Briefly describing the operation of the absorption type refrigerator having the above-described configuration, the absorbent liquid falls from the tray 31 on the upper side of the absorber 3 onto the cooling water heat pipe 33 in the absorber 3 and passes between the eliminators 34. Absorbs and collects at the bottom of the absorber (3).

At this time, the absorbent liquid is much thinner than before it flows into the tray 31, and the concentration is about 58%. The absorbed liquid of the collected rare liquid (dilute concentration) is absorbed by the absorbent liquid circulation pump 32 in the absorber 3 and the low temperature solution heat exchanger 8 ) And the high temperature solution heat exchanger (9) is heat exchanged to a high temperature of about 120 ~ 130 ℃ to rise to the high temperature regenerator (7), when heated further by the heat source in the high temperature regenerator (7) Absorption liquid at the concentration) evaporates, and the concentration rises.

On the other hand, the intermediate liquid (medium liquid absorbing liquid) whose concentration is increased by about 61% is passed through the high temperature solution heat exchanger 9 and the temperature is lowered to about 84 ° C., thereby rising to the low temperature regenerator 6.

 The absorber is transported from the absorber 3 to the high temperature regenerator 7 by the earth output of the absorption liquid circulation pump 32, but from the high temperature regenerator 7 to the low temperature regenerator 6 due to the pressure difference between the high temperature regenerator and the low temperature regenerator. do.

That is, since the pressure of the high temperature regenerator 7 is about 700 to 710 mmHg, and the temperature of the low temperature regenerator 6 is about 56 mmHg, the absorbent liquid whose concentration is increased in the high temperature regenerator 7 by this pressure difference is the low temperature regenerator. Is transported to (6).

In the low temperature regenerator (6), the hot liquid vapor separated from the high temperature regenerator (7) and turned into steam passes through the heat transfer pipe (14) in the low temperature regenerator (6), thereby heating the intermediate liquid once more, thereby increasing the concentration of the intermediate liquid. Concentrate to approximately 63% absorption liquid.

At this time, the concentration of the absorbent liquid is the strongest, and in the cryogenic regenerator 6, the concentrate (the concentrated absorbent liquid) passes through the low temperature solution heat exchanger 8 and the absorber (3) is lowered again at a lower temperature of about 52 to 55 ° C. In this case, the absorption liquid flows to the absorber due to the height difference between the low temperature regenerator 6 and the absorber 3 and the pressure difference between the low temperature regenerator 6 and the absorber 3.

Through this process, the absorbent liquid absorbs the refrigerant again and continues to circulate in the same manner.

In addition, the refrigerant evaporates in the evaporator 2 to make the water in the cold water heat pipe 22 into cold cold water. The refrigerant in the form of vapor is absorbed by the absorbent liquid and mixed with the absorbent liquid to the high temperature regenerator 7 and transported. When heated by the heat source at (7), the refrigerant vapor separated from the absorbing liquid at the upper part of the high temperature regenerator 7 and evaporated goes to the low temperature regenerator 6 along the refrigerant vapor pipe.

Then, the refrigerant vapor moved to the low temperature regenerator (6) flows to the heat transfer tube (14) in the low temperature regenerator (6) to heat the intermediate liquid once more.

The refrigerant vapor passing through the low temperature regenerator 6 is condensed with water, which is a refrigerant at the same time as the absorption liquid is heated in the low temperature regenerator, and the condensed refrigerant moves to the condenser 5 and is recovered to the evaporator 2. Refrigerant vapor remaining without condensation is condensed by the cooling water of the condenser (5).

The refrigerant in the condenser is recovered to the evaporator 2 and circulated in the same order as above.

Figure 2a is a partial cutaway perspective view showing a conventional high temperature regenerator, Figure 2b is a longitudinal cross-sectional view of Figure 2a, Figure 2c is a cross-sectional view A-A of Figure 2a, Figure 2d is a B-B cross-sectional view of Figure 2a.

As shown in the drawing, the conventional high temperature regenerator 7 includes a burner 71, a combustion chamber 74, an associated heat transfer tube 76, a connection space 75 connecting the combustion chamber and the heat transfer tube, an exhaust port 77 and an outer cylinder 78. Is done.

The burner 71 is connected to a fuel supply unit 72 for controlling and supplying fuel gas and an air supply unit 73 for controlling and supplying air, and one side is connected to an outer cylinder 78 of the high temperature regenerator.

The combustion chamber 74 is connected to the burner 71, one side is connected to the connection space (75).

The associated heat transfer pipes 76 are located at the upper portion of the combustion chamber 74 and are connected to the connection space 75, and one side is connected to the outer cylinder 78.

The exhaust port 77 is connected to the outer cylinder 78 of the high temperature regenerator and includes one side of the associated heat transfer tube 76.

The outer cylinder 78 includes a rare liquid inlet 701, an intermediate liquid outlet 702, and a refrigerant vapor outlet 703, and an eliminator 704 is connected to the refrigerant vapor outlet.

Looking at the operation of the high temperature regenerator having the above configuration in detail as follows.

The fuel gas supplied from the fuel supply unit 72 and the air supplied from the air supply unit 73 pass through the burner 71 and are respectively supplied to the combustion chamber 74.

The fuel gas and air supplied to the combustion chamber 74 are mixed in the combustion chamber, and combustion starts by ignition of the burner 71.

Once combustion is started, the fuel gas and air continue the combustion process without further ignition by the combustion exothermic reaction, and the mixing and combustion of the fuel gas and air occur simultaneously in the combustion chamber 74.

This method is called diffusion combustion, and the area where combustion proceeds is called flame. Diffusion combustion type flame requires a certain space for mixing fuel gas and air. The flame is relatively large and requires a combustion chamber of a certain space to form a stable flame.

On the other hand, the high-temperature combustion gas after the combustion is completed in the combustion chamber 72 passes a portion of heat to the combustion chamber inner wall and the connection space inner wall while passing through the combustion chamber and the connection space 75, and enters the associated heat transfer tube 76.

The hot combustion gas then transfers much of the heat inside the associated heat pipe to the inside wall of the heat pipe, and enters the exhaust port 77 and is discharged outward.

On the other hand, the rare liquid enters into the liquid chamber through the rare liquid inlet 701 connected to one side of the outer cylinder 78, and is heated by receiving heat from the inner wall of the combustion chamber, the inner wall of the connection space, and the inner wall of the associated heat pipe, and then into the refrigerant vapor and the intermediate liquid. Are separated.

Then, the separated refrigerant vapor and the intermediate liquid respectively exit to the refrigerant vapor outlet 703 and the intermediate liquid outlet 702 communicated with one side of the outer cylinder.

Therefore, the conventional high temperature regenerator burns while the fuel gas and air are mixed inside the combustion chamber, and the combustion chamber has a relatively large constant space so that the combustion chamber can form a proper flame and a stable flame. The heat transfer portion, which is a bundle of heat transfer tubes, is disposed on the combustion chamber to have an appropriate hot regenerator length, and connects the combustion chamber and the heat transfer portion to the connection space.

However, the above-described high temperature regenerator has the following problems.

First, while the combustion chamber has a significantly lower heat transfer effect than the heat transfer unit, while the size of the combustion chamber is larger than that of the heat transfer unit, the size of the high temperature regenerator increases in the structure, thereby increasing the inefficiency of the installation area.

Second, the heat transfer effect is affected not only by the heat transfer area of the heat transfer part, but also by the heat transfer length of the heat transfer part, but the heat transfer effect is better as the heat transfer length is longer even in the same heat transfer area. Shorter than the length of the combustion chamber.

Due to the limitation of the length of the heat transfer tube, the inefficiency of the heat transfer effect is increased.

Third, in the above structure, combustion occurs sequentially as fuel gas and air flow from the burner side to the connection space, and thus combustion reaction heat is sequentially generated in the combustion chamber.

However, the temperature of the flame (diffusion flame) which burns sequentially is lower than the maximum temperature of the flame (premixed flame) which burns intensively.

In other words, the effect of heat transfer is affected by the temperature difference and the larger the temperature difference is, the higher the flame structure is formed in the above-described structure, since the maximum temperature of the flame is lower than the temperature of the flame intensively burned, the combustion gas and The temperature difference of the absorbent liquid is reduced, which reduces the efficiency of the heat transfer effect.

Therefore, as mentioned above, the existing high temperature regenerator has inefficiencies in size and heat transfer performance.

Therefore, the present invention has been made to solve the above problems, the present invention is a heat transfer means comprising one or more heat transfer unit having an associated heat transfer tube bundle is arranged in series or parallel structure heat efficiency according to the increase in the length of the heat transfer tube The aim is to maximize.

In addition, the present invention aims to improve the heat transfer effect by increasing the maximum temperature of the flame to become a premixed flame during combustion.

In order to achieve the above object, the present invention combusts fuel flowing through a fuel supply unit and an air supply unit, and transfers the fuel to an associated heat exchanger tube. In the high temperature regenerator provided,

The high temperature regenerator and premixing means for mixing the fuel supplied; A combustion unit connected to one side of a surface combustion plate provided in the premixing means; A heat transfer means connected to the combustion unit and having at least one heat transfer unit including a plurality of associated heat transfer tubes through which combustion gas passes; It provides a high temperature regenerator comprising a heat transfer connecting portion for connecting the heat transfer unit.

Through the above configuration, the high temperature regenerator according to the present invention further improves performance by arranging heat transfer tubes in a space that can be reduced without reducing the size, or by arranging heat transfer tubes only in a portion of the space that can be reduced, thereby improving performance and size. At the same time, it can be reduced.

Hereinafter, exemplary embodiments of the present invention will be described with reference to the accompanying drawings.

In addition, the present embodiment is not intended to limit the scope of the present invention but is merely presented as an example, and there may be various embodiments implemented through the technical idea.

Figure 3a is a perspective view showing a high temperature regenerator according to the present invention, Figure 3b is a longitudinal sectional view of Figure 3a, Figure 3c is a sectional view AA of Figure 3b, Figure 3d is a sectional view BB of Figure 3b, Figure 3e is a fuel mixing means 3F is a cross sectional view of FIG. 3E.

As shown, the high temperature regenerator 100 of the present invention is a pre-mixing means 101 for mixing the air and fuel introduced roughly, the combustion unit 201 in communication with the pre-mixing means 101 to burn the mixed fuel ), A heat transfer means 301 having a plurality of heat transfer parts in communication with the combustion unit 201 and moving the combustion gas and heat, and a heat transfer connection portion connecting the heat transfer parts to each other so that the combustion gas moves the heat transfer means sequentially. 302, a liquid chamber 402, which is a space for temporarily storing the leachate, and an outer cylinder 401 for allowing the above-mentioned components to be embedded.

Specifically, the premixing means 101 is in communication with the fuel supply unit 102 in which fuel gas is controlled and supplied, and is connected to the air supply unit 103 in which air is controlled and supplied.

In addition, the interior of the pre-mixing means 101 may be divided into a mixing unit 108 for mixing fuel and air, and a uniform distribution unit 106 to have a uniform pressure and speed of the flow of the mixed fuel.

At this time, the mixing unit 108 is provided with a diffusion mixing plate 104 for mixing the air and fuel supplied, the uniform distribution unit 106 is spaced apart from the diffusion mixing plate 104 by a predetermined distance and mixed fuel A porous plate 105 in which a plurality of holes are formed to maintain a uniform pressure and speed, and a surface burner plate 107 which ejects the mixed fuel at a position spaced apart from the porous plate 105 by contact with the combustion unit 201. ) Is provided.

The combustion unit 201 communicates with the premixing means 101 on one side and forms a predetermined space for forming a flame of the mixed gas.

On the other hand, it is connected to the combustion unit 201 in communication with the pre-mixing means 101, the heat transfer means 301 is provided with at least one heat transfer unit consisting of a bundle of associated heat transfer tube passing the combustion gas therein, The heat transfer connector 302 is provided to connect the plurality of heat transfer units to sequentially move the combustion gas.

At this time, the plurality of heat transfer means 301 is arranged in a vertical (up and down) direction, the combustion gas can be moved sequentially, in the present invention, the heat transfer means is a combustion unit 201 to move the combustion gas in sequence ) And a second heat transfer part 301b communicating with the first heat transfer part 301b and formed above the first heat transfer part 301a.

The first heat transfer part 301a and the second heat transfer part 301b communicate with each other through the heat transfer connection part 302, and each heat transfer part is composed of a plurality of associated heat pipe bundles.

The outer cylinder 401 includes the combustion unit 201, the heat transfer means 301, the heat transfer connection portion 302 therein at a predetermined interval, the absorbent liquid concentrate outlet 404, the absorbent liquid solution inlet 403, the refrigerant It is made to be connected in communication with the steam outlet (405).

In addition, the liquid chamber 402 is composed of a predetermined space between the combustion unit 201, the heat transfer means 301, the heat transfer connection portion 302 and the outer cylinder 401.

The operation of the present invention having the above configuration will be described with reference to FIGS. 3A to 3F.

The fuel gas supplied from the fuel supply unit 102 and the air supplied from the air supply unit 103 are mixed into the mixed fuel in the mixing unit 108 including the diffusion mixing plate 104, and the mixed fuel is a porous plate. The uniform distribution part 106 including the 105 has a uniform pressure and velocity flow, and is ejected to the combustion part 201 through the surface burning plate 107.

Then, the mixed fuel of the combustion unit 201 by the ignition by the pre-mixing means 101 is burned in a flame of 50 ~ 150 mm length in the surface burner plate 107, the combustion gas of the high temperature combustion is completed, the first heat transfer unit After heat exchange in the interior 301a, the heat transfer part 302 enters the heat transfer connection part 302 at about 357 ~ 365 ° C, and after heat exchange in the second heat transfer part 301b, it is discharged outward through the exhaust part 501 at 185 ~ 189 ° C. do.

Meanwhile, the rare liquid enters into the liquid chamber through the rare liquid inlet 403 communicated with one side of the outer cylinder 401, and receives the heat from the combustion unit 201, the heat transfer means 301, and the heat transfer connection unit 302, and heats it. The refrigerant vapor and the intermediate liquid are separated, and the separated refrigerant vapor and the intermediate liquid exit to the refrigerant vapor outlet 405 and the intermediate liquid outlet 404 respectively connected to one side of the outer cylinder 401.

The structure of the present invention has the following effects.

First, since the associated heating element can be arranged in the vertical direction, even if the heat transfer tube having the same heat transfer area as the conventional high temperature regenerator, the width is reduced.

Therefore, in the above structure, the size of the high temperature regenerator becomes small, and in particular, the width becomes smaller, thereby realizing a compact high temperature regenerator and a slim type high temperature regenerator and reducing the installation area.

Second, even if it has a heat exchanger tube of the same heat transfer area as a conventional high temperature regenerator, heat transfer means can be arrange | positioned in series with respect to combustion gas, and heat transfer length can be made longer than the length of a high temperature regenerator.

Therefore, the effect of heat transfer improvement is brought.

Third, since combustion starts on the surface burner plate and is instantaneously completed in a narrow combustion section space, the temperature of the flame is higher than the flame temperature of the conventional high temperature regenerator, so that the temperature difference between the flame and the absorbing liquid can be increased.

Therefore, the effect of heat transfer improvement is brought.

Figure 4a is a perspective view showing an embodiment of a high temperature regenerator according to the present invention, Figure 4b is a longitudinal cross-sectional view of Figure 4a, Figure 4c is a cross-sectional view A-A of Figure 4b, Figure 4d is a cross-sectional view B-B of Figure 4b.

As shown, the cross section of the combustion gas flow path of the first heat transfer unit 301a is larger than the cross section of the combustion gas flow path of the second heat transfer unit.

Because the combustion gas temperature in the first heat transfer unit 301a enters 1150 ° C. and goes out at 365 ° C., and in the second heat transfer unit 301b enters 365 ° C. and exits at 190 ° C., the first heat transfer part and the second heat transfer. Even if the same flue gas mass flow rate passes through the part, the density of the flue gas varies depending on the temperature, and thus the velocity of the flue gas is different.

That is, when the first heat transfer part 301a and the second heat transfer part 301b have the same flow path area, the velocity of the combustion gas is increased in the first heat transfer unit having a high temperature, and combustion is performed in the second heat transfer unit having a low temperature. The speed of the gas is slowed down. If the speed of the combustion gas is faster than necessary in the first heat transfer unit, the pressure difference is more than necessary.

Therefore, the flow path area of the first heat transfer part is larger than the flow path area of the second heat transfer part in order to lower the moving speed of the combustion gas in the first heat transfer part 301a than the moving speed of the combustion gas in the second heat transfer part 301b. do.

Theoretically calculating this is as follows.

P V = m R T (1) in the state equation of an ideal gas

Where P is absolute pressure, V is volume, m is mass, R is gas constant, and T is absolute temperature.

On the other hand, since the inlet and outlet pressures of the first heat transfer part and the second heat transfer part are much larger than the differential pressure, the absolute pressure P can be regarded as constant, and the gas constant R has almost no combustion gas components in the first heat transfer part and the second heat transfer part. Since it can be considered as the same, it can be seen as a constant, the absolute temperature T uses the average temperature of the inlet and outlet temperature of the first heat transfer section and the second heat transfer section for approximate calculation.

Therefore, differentiating (1) with respect to time is as follows.

P dV / dt = dm / dt R T (2)

Where dV / dt represents volume flow rate and dm / dt represents mass flow rate, respectively.

The mass flow rate dm / dt becomes constant because all the combustion gas from the first heat transfer unit enters the second heat transfer unit.

However, the volume flow rate dV / dt is not constant because the volume and density change with temperature, and this is divided by the velocity v and the flow path area A as follows.

P v A = dm / dt R T (3)

Since the flow path area A must be determined to make the velocity v constant, the velocity v is considered to be constant.

A ∝ T (4)

That is, in order to make the velocity of combustion gas constant, what is necessary is just to design so that the flow path area ratio of a 1st heat exchange part and a 2nd heat transfer part may be equal to an average absolute temperature ratio.

At this time, it is preferable that the ratio of the cross-sectional area of the flow path of the first heat transfer part and the second heat transfer part is 1.4: 1 to 2.8: 1.

5A is a perspective view showing a high temperature regenerator in which heat transfer means are vertically arranged in three stages, and FIG. 5B is a cross-sectional view of FIG. 5A.

Since the flow path of the combustion gas is longer, as shown in the drawing, the heat transfer means 301 may be arranged in three stages or more, resulting in an effect of improving heat transfer.

That is, the first, second, and third heat transfer parts 301a, 301b, and 301c are sequentially installed vertically, and the first and second heat transfer parts are connected to each other by the first heat connection part 302a. The third heat transfer part is connected via the second heat connection part 302b.

At this time, in order to reduce the size of the high temperature regenerator, in particular, in order to reduce the width and not increase the height, the height of the associated heat exchanger tube is made smaller and the number thereof is increased, thereby securing the overall heat transfer area.

6A is a perspective view showing a high temperature regenerator in which heat transfer means are arranged vertically and horizontally, and FIG. 6B is a cross-sectional view of FIG. 6A.

In the above embodiment, the first, second, third, and fourth heat transfer parts 301a, 301b, 301c, and 301d are sequentially installed vertically and horizontally, and the first and second heat transfer parts include the first heat connection part 302a. The second and third heat transfer units are connected via the second heat connection unit 302b, and the third and fourth heat transfer units are connected via the third heat connection unit 302c.

That is, in order to further expand the flow path of the combustion gas, the associated heating element may be connected not only in a vertical series but also in a left and right series.

On the other hand, in the present invention, without further reducing the size of the high temperature regenerator, the heat transfer means is further arranged in the space that can be reduced to achieve an extreme performance improvement, or by placing the heat transfer means only in a part of the space that can be reduced performance improvement and The size can be reduced at the same time.

Experiment 1

Design and manufacture a high temperature regenerator which is smaller than the conventional high temperature regenerator (60% of the conventional high temperature regenerator) and the heat transfer area is almost the same (95% of the conventional high temperature regenerator), and attaches it to the absorption type freezer.

The outer cylinder is 1500mm long, 1440mm high and 424mm wide, and is produced by placing the rare liquid inlet, the intermediate liquid outlet, and the refrigerant vapor outlet at appropriate positions.

The heat transfer means adopts the two-stage series method, and the heat transfer area is 12.87 ㎡, and the flow path areas of the first and second heat transfer parts are different.

The lower portion of the first heat transfer section was formed with a heat transfer area of 7.56 m 2, and consisted of 12 associated heat exchangers 1074 mm long, 180 mm high and 32 mm wide, and 6 associated heat pipes 1074 mm long, 150 mm high and 32 mm wide. The second heat transfer part of the heat transfer area is 5.30 m 2, and consists of twelve associated heat exchanger tubes having a length of 1074 mm, a height of 180 mm, and a width of 32 mm.

The fuel mixing means adopts pre-mixed surface combustion method, which is made of 360mm in width, 400mm in height and 200mm in width, and has a mixing part and a primary and secondary distribution plate of 360mm in width and 250mm in height. Consist of uniform distribution.

Absorption refrigerator equipped with the high temperature regenerator of Experiment 1 uses the BUW model currently being produced.

As a result of the experiment, when the cold water inlet temperature is 12 ℃, the cooling water inlet is 32 ℃, and the refrigeration load is 161.71 ± 1.0 usRT, the gas regenerator consumes 24.3㎡ / h, flame temperature 1180 ℃, heat transfer connection 364 ℃, exhaust gas temperature 185 ℃, liquid The room temperature was also 155 ± 2 ° C. and an efficiency of 81.6%.

Experiment 2

Design and manufacture a high temperature regenerator which is smaller in size than conventional high temperature regenerators (60% of conventional high temperature regenerators) and larger heat transfer area (111% of conventional high temperature regenerators).

The outer cylinder is 1500mm long, 1440mm high and 424mm wide, and is prepared by placing the rare liquid inlet, the intermediate liquid outlet, and the refrigerant vapor outlet at appropriate positions.

The heat transfer means adopts a two-stage series method, and the heat transfer area is 15.00㎡, and the flow path areas of the first and second heat transfer parts are different.

The lower part of the first heat exchanger was 8.82m2 of heat transfer area, and was composed of 14 associative heat pipes of 1074mm in length, 180mm in height and 32mm in width, and 7 heat pipes of 1074mm in length, 150mm in height and 32mm in width. The second heat transfer part has a heat transfer area of 6.18 m2, and is composed of 14 associated heat exchanger tubes having a length of 1074 mm, a height of 180 mm, and a width of 32 mm.

The fuel mixing means adopts the premixed surface combustion method, which is made of 360mm in width, 400mm in height and 200mm in width, and has 360mm in width, 250mm in height of surface burning plate, mixing part of rotary injection method, and 1st and 2nd distribution plate. Consist of uniform distribution.

Experiment 2 The absorption chiller equipped with a high temperature regenerator is a performance test using a BUW model currently produced as in Experiment 1.

As a result of the experiment, when the cold water inlet temperature is 12 ℃, the cooling water inlet is 32 ℃, and the refrigeration load is 161.7 ± 1.0 usRT, the gas regenerator consumes 23.5㎡ / h, flame temperature 1221 ℃, heat transfer connection 323 ℃, exhaust gas temperature 180 ℃, and liquid chamber. A temperature of 155 ± 2 ° C. and an efficiency of 85.2% were measured.

Experiment 3

Produced a conventional high temperature regenerator and attached it to an absorption chiller (currently produced BUW model).

The outer cylinder is 1500mm long, 1435mm high and 720mm wide, and is a high temperature regenerator of the BUW model currently being produced.

The heat transfer means is a one-stage system located only on the combustion chamber. The heat transfer area is 13.50㎡, and it is manufactured using an associated heat transfer tube.

Fuel mixing means are manufactured by forced direct diffusion combustion method.

As a result of the experiment, when the cold water inlet temperature is 12 ° C, the cooling water inlet is 32 ° C, and the freezer load is 161.7 ± 1.0 usRT, the gas regenerator consumes 25.0㎡ / h, combustion chamber outlet 683 ° C, exhaust gas temperature 231 ° C, liquid chamber temperature 155 ± 2 ° C. The efficiency 79.9% was measured.

Table 1 below summarizes the results of the experiments 1,2,3.

TABLE 1

External volume (㎥) Heat transfer area (㎡) Fuel amount (㎡ / h) Exhaust temperature (℃) efficiency(%) Experiment 1 0.92 12.87 24.3 185 81.6 Experiment 2 0.92 15.00 23.5 180 85.2 Experiment 3 1.55 13.50 25.0 231 79.9

As can be seen from Table 1, the outer cylinder volume of the high temperature regenerator to which the technical content according to the present invention is applied is reduced, but the fuel amount and the exhaust temperature are reduced, and as a result, the efficiency is increased.

7 is a graph summarizing the results of Experiments 1, 2, and 3 above.

In the graph, when the external cylinder volume, heat transfer area, and fuel amount of the conventional high temperature regenerator (Experiment 3) are 100%, the relative comparison value of the high temperature regenerator (Experiment 1,2) to which the technical details according to the present invention are applied is shown.

As can be seen from the graph, it can be seen that when the high temperature regenerator of Experiment 1 is applied, the size is reduced by 40%, the fuel amount is reduced by 2.8%, and the efficiency is increased by 1.7%.

When applying the high temperature regenerator of Experiment 2, it can be seen that the size was reduced by 40%, the fuel amount was reduced by 6% and the efficiency was increased by 5.3%.

Therefore, as shown in the above experimental results, the high temperature regenerator according to the present invention has higher efficiency than the conventional high temperature regenerator, and the size of the high temperature regenerator itself can be reduced.

As described above, the high temperature regenerator according to the present invention may be arranged in a vertically or vertically (vertically) or horizontally (parallel) direction in a vertical direction or a mixture of heat transfer units having a plurality of associated heat transfer tubes, and thus the same as the conventional high temperature regenerator. Even if the heat transfer area has a heat pipe, the width is reduced, thereby reducing the size of the high temperature regenerator itself.

In addition, the heat transfer length can be increased by the vertical or horizontal arrangement, thereby increasing the heat transfer rate.

In addition, by adopting a premixed surface combustion method in which combustion starts on a surface burner plate and is instantaneously completed in a narrow combustion section space, the temperature of the flame is higher than that of a conventional high temperature regenerator, thereby increasing the temperature difference between the flame and the absorbing liquid. There is an advantage that can increase the heat transfer rate.

1 is a view showing the configuration of a general absorption chiller.

Figure 2a is a partial cutaway perspective view showing a conventional high temperature regenerator.

FIG. 2B is a longitudinal sectional view of FIG. 2A;

FIG. 2C is a cross-sectional view A-A of FIG. 2A; FIG.

FIG. 2D is a B-B cross sectional view of FIG. 2A;

Figure 3a is a perspective view showing a high temperature regenerator according to the present invention.

3B is a longitudinal cross-sectional view of FIG. 3A.

3C is a cross-sectional view taken along the line A-A of FIG. 3B.

3D is a cross-sectional view taken along line B-B in FIG. 3B.

3E shows a fuel mixing means.

3F is a cross sectional view of FIG. 3E;

Figure 4a is a perspective view showing an embodiment of a high temperature regenerator according to the present invention.

4B is a longitudinal cross-sectional view of FIG. 4A.

4C is a cross-sectional view A-A of FIG. 4B.

4D is a cross-sectional view taken along line B-B in FIG. 4B.

5A is a perspective view of a high temperature regenerator in which heat transfer means are vertically arranged in three stages.

5B is a cross-sectional view of FIG. 5A.

6A is a perspective view of a high temperature regenerator in which heat transfer means are arranged vertically and horizontally;

6B is a cross-sectional view of FIG. 6A.

7 is a graph summarizing the results of Experiments 1, 2, and 3.

* Description of the symbols for the main parts of the drawings *

101: premixing means 201: combustion part

301: heat transfer means 401: outer cylinder

402: liquid chamber

Claims (4)

In the high temperature regenerator provided with the absorption chiller and the absorption cold and hot water in which the fuel flowing through the fuel supply unit and the air supply unit burns and delivers the fuel to the associated heat transfer tube, whereby the heat is separated into the refrigerant vapor and the intermediate liquid. The high temperature regenerator and premixing means for mixing the fuel supplied; A combustion unit connected to one side of a surface combustion plate provided in the premixing means; A heating unit connected to the combustion unit and having at least one heat transfer unit including a plurality of associated heat transfer tubes through which combustion gas passes, and the heat transfer unit is selectively arranged in up and down or left and right directions to sequentially move the combustion gas; The high temperature regenerator comprising a heat transfer connecting portion connecting the heat transfer unit. delete The high temperature regenerator according to claim 1, wherein the cross section of the combustion gas flow path of the heat transfer unit is gradually reduced in accordance with the passage sequence of the combustion gas. The method of claim 1, wherein the premixing means comprises: a diffusion mixing plate for mixing the air and fuel supplied; A perforated plate spaced apart from the diffusion mixture plate by a plurality of holes to maintain the mixed fuel at a uniform pressure and speed; A high temperature regenerator comprising a surface combustion plate spaced apart from the porous plate by a predetermined distance to eject the mixed fuel to the combustion unit.