ABSORBOR FOR USE IN THE ABSORPTION CALORIFYING AND REFRIGERATION PUMP SYSTEMS BACKGROUND OF THE INVENTION Field of the Invention The present invention relates to heat pump and refrigeration systems and, more particularly, to improved apparatus designs for heat exchange systems. heat generator-absorber ("GAX"). Description of the related art. The heat pump and absorption cooling systems described herein by the Patents
North American Nos. 5,367,884, 5,271,235, 5,570,584, 5,579,
652 and 5,782,097, the description which is incorporated by reference herein, utilizes generator-absorber heat exchange systems ("GAX"). These systems include an absorber that has a section with operating temperatures that overlap with or exceed the temperatures in the generator such that the heat production from the absorber section can serve as heat input to the section that exceeds the generator temperature . As described in the aforementioned patents, sections that exceed or overlap with the temperature of the generator and the absorber are referred to as
Ref No. 133619"heat transfer regions". To achieve its full effectiveness, the heat production of the absorber must be produced over the total range of temperatures exceeding the absorber and must be transferred to the section exceeding the generator such that each heat element of the absorber at any specific temperature is it transfers to the generator in a location that is at a temperature only a few degrees below the temperature of the region in the absorber where the heat is extracted. The above patents describe various ways of transferring heat from the absorber to the generator in this manner. The invention describes the improved apparatus designs for use in the absorption process that allows the transfer of heat and mass to be carried out very efficiently. While the present invention is of more importance in the section that exceeds or overlays in the GAX of the absorber, it is also useful for the cooling section of the rich solution (absorber heat exchange, or AHE) and the hydronically cooled section of the absorber. It is also well suited for the section that exceeds the GAX of the generator. To carry out the maximum performance, the absorber must produce the heat of absorption at each and all temperatures throughout the range of production and transfer of each heat element to the heat transfer medium with possible temperature differences minimum. This invention describes new means by which the absorption process can be carried out with low temperature differences of the absorption surface of the cooler that is possible with the prior art. In the prior art, as shown in Fig. 1, the liquid 12 introduced into the upper part of the absorber 10 drips on the coils 14 of the pipe, which flows downwards like a falling film on the pipes, while the steam 16 which is going to be absorbed which flows upwards along and between the coils 14. The use of descending films of this type are among the most effective methods of heat and mass transfer known. Still, in the absorption of ammonia within an ammonia-water solution, it has been found that this use of concentric coils has significant limitations. One limitation of the concentric coils is the difficulty in firmly distributing the liquid over the tops of the coils so that the fluxes on both the inner and outer surfaces of the coils are equal or, preferably, in proportion to the areas of the surfaces. of the interior and exterior interior coils. Another limitation of the spiral pipe of the prior art is that the heat transfer from the coil to the interior flowing from the cooler is often low., and requires a high speed cooler and / or more than a concentric coil. A third limitation is that the flow rate of the absorber may be low enough that the downwardly flowing absorbent does not wet the surfaces of the cooling coils uniformly or completely. Rather, the streams of the downwardly flowing absorbent contact only part of the coils. A fourth limitation is that the steam that flows upward along the outside and inside of a coil may not always flow in proportion to the absorption ratios on both sides. It can flow up faster through one passage than through another, resulting in varying vapor compositions, and incomplete absorption and heat transfer. In the GAX cycle, the absorbent liquid, for example, water, that enters the top of the absorber has a low concentration of ammonia, commonly below 7% and sometimes below about 1%, and is referred to herein as "liquor". weak". As the liquor from the weak liquor travels down the absorber, it absorbs ammonia, the concentration of the ammonia increases, and under mild operating conditions the weak water can reach 50% ammonia or more at the bottom outlet of the absorber. This liquid at the outlet of the absorber is referred to herein as "rich liquor". In general, the larger the difference in concentration between the rich liquor and the weak liquor, the better the performance of the GAX apparatus. The temperature range between the two ends of the abosorber can be 93.33 ° C or more. To produce the best performance, the ammonia vapor should flow in a relative backflow to the absorbent liquid. Backflow is especially important in the production section (GAX) of the absorber and in the cooling section of the absorber for the rich liquor (section AHE). The steam in general enters the bottom of the absorber at a concentration of about 99% ammonia and 1% water. When the steam flows upward in counterflow with the liquid, the composition of the vapor changes, preferably as close as possible to the equilibrium with the liquid with which it is in contact as possible. In the temperature-pressure diagram of Fig. 2, each point on the solid lines represents the concentration of the ammonia in the liquid at a temperature and pressure of this point. Similarly, the faded lines represent the concentration of ammonia in the vapor that is in equilibrium with the liquid at the same temperature and pressure. As can be seen in Fig. 2, ammonia concentrations in equilibrium vapors are always greater than ammonia concentrations in the liquids with which they are in equilibrium. Also, the amount of ammonia in equilibrium in the vapor is in relation to that in the liquid that changes up and down with the pressure. As shown in fig. 2, the concentration of ammonia in the vapor that is in equilibrium with the liquid that changes in the same direction as the liquid, but to different extensions, through ammonia to the temperature range of the water. As an example, the concentration of ammonia in the steam, (shown by dotted lines and at the top of the diagram) changes slightly on the left-hand side of the range and faster on the right-hand side. The concentration of liquid ammonia changes in an opposite way, rapidly to the left and more slowly to the right. Thus, in the absorber, when 99% of the ammonia vapor enters the absorber and flows upward, it first absorbs the ammonia vapor into the liquid, but then, the liquid water could evaporate in the vapor. Finally, the evaporation ends of the water and, near the top, the absorption of both the vapors of ammonia and water occurs, until the steam is absorbed all over. It is therefore very important that the flows of both steam and liquid are carefully controlled. When a part of this control, the absorber of the invention uses only one surface for absorption, the inner surface of the absorber housing. Additional aspects and advantages of the invention will be set forth in the drawings and in the written description which continues, and in part will be apparent from the drawings and the written description or may be studied from the practice of the invention. The advantages of the invention will be realized and achieved by the generator-absorber heat exchange apparatus particularly indicated in the drawings, the written description and the claims thereof. BRIEF DESCRIPTION OF THE INVENTION In order to carry out this and other advantages, and in accordance with the purpose of the invention as clearly included herein and described herein, the present invention, in one aspect, provides a generator-absorber heat exchange apparatus that includes a generator and an absorber. Each of the generator and absorber includes a cylindrical housing in generally having inner wall surfaces. The absorber is configured so that the weak solution ammonia-water liquid entering the upper part of the absorber that flows upwardly along the surface of the inner wall of the absorber thus comes into contact in a counterflow manner generally the vapor of the rich solution entering the bottom of the absorber and flowing upwards through the absorber. The surface of the inner wall of the absorber includes a plurality of spaced apart shaped nodes that increase the transfer of ammonia from the steam flowing upwardly through the absorber to the liquid flowing downward along the surface of the inner wall of the absorber. increase the transfer of heat from the liquid to the surface of the knotted inner wall. According to another aspect of the invention, as clearly included and described here, a generator-absorber heat exchange apparatus including a generator and an absorber is provided. The absorber has a lower internal pressure than the internal pressure of the generator, and the generator and the absorber each include a cylindrical housing generally having surfaces of the inner wall forming a hollow interior. The absorber is configured such that the weak solution of the ammonia-water liquid entering the upper part of the absorber flows downwardly along the surface of the inner wall of the absorber so that it is generally contacted in a counter-flow manner the vapor of the rich solution entering the bottom of the absorber and flowing upwards through the absorber. The hollow interior of the absorber housing includes a plurality of flow deflectors. Each of the flow deflectors includes a base that directs the liquid flowing down through the absorber in the direction of the surface of the inner wall, and an edge extending from the base to a skirt that forms an open end . The skirt of the flange and the surface of the inner wall of the absorber form an access path for the liquid flowing down the surface of the inner wall of the absorber to pass from a flow deflector to an adjacent flow deflector. The access road is impenetrable to the steam that flows upwards. The edge includes a plurality of perforations that allow the steam that flows upward through the absorber to flow horizontally in the direction of the surface of the inner wall. The perforations together with the pressure drop of the flowing liquid causes the vapor to impinge on the liquid flowing down along the surface of the inner wall to increase the ammonia transfer of the steam flowing up through the absorber the liquid flowing down along the surface of the inner wall of the absorber and to increase the transfer of heat from the liquid to the knotty surfaces. According to a preferred embodiment of the invention, the generator-absorber heat exchange apparatus includes an absorber having both the knotted inner surface and a plurality of flow deflectors described above. According to another embodiment of the invention, the generator-absorber heat exchange apparatus includes an absorber having a secondary fluid cooling section close to half the absorber, and a generator-absorber heat exchange section close to the top of the absorber. The apparatus includes three helical heat exchange coils extending around the outer surface of the absorber housing adjacent to the secondary fluid cooling section. The second helical coil extends around the outer surface of the absorber housing adjacent to the heat exchange section of the absorber. The third helical coil extends around the outer surface of the absorber housing adjacent to the generator-absorber heat exchange section. The foregoing and other advantages and aspects of this invention will be apparent upon review of the following description in conjunction with the drawings. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a diagram of a heat transfer configuration of the prior art; Fig. 2 is a pressure-temperature-composition diagram (P-T-X) of the ammonia-water compositions; Fig. 3a is a front view of a mode of the knots of this invention; Fig. 3b is a cross-sectional view of one embodiment of the knots of the invention; Fig. 4 is a cross-sectional view of one embodiment of the invention illustrating the knots, flow deflectors, and heat transfer coils of the invention; Fig. 5 is a graph of an absorber illustrating the flow deflectors and the heat transfer heat transfer coils in one embodiment of the invention; The Fig. 6 illustrates an embodiment of the invention in relation to the joining of the heat transfer coils to the absorber; FIG. 7 is a graph of an absorber illustrating flow deflectors and heat transfer coils in an embodiment of the invention, wherein the absorber is a component of the heat pump; Fig. 8 is a graph showing the heat transfer results obtained by using two types of knots according to the invention; and Fig. 9 is a flow chart of a heat pump using a generator-absorber heat exchange apparatus. DETAILED DESCRIPTION OF THE PREFERRED MODALITIES According to a first embodiment of the invention, in order to provide a good and continuous humidity of the entire inner surface of the shell of the absorber, this surface is preferably knotty, as shown in Fig. 3. knots improve the flow of the absorbent liquid, which has been distributed around the inner surface of the shell, and maintains the equal distribution of the liquid by causing a constant fractionation of the small currents that flow around each pyramid of knots. The knots also increase the effective surface area of the part. inside the shell. The knots can be of different sizes and shapes. A preferred shape of the knots in a diamond shape, as shown in Fig. 3a. The present inventor has experimented with three different types of diamond-shaped knots. A vertical diamond-shaped knot 20, as shown in Figure 3a, has an angle of 60 ° at the top, as shown. The horizontal diamond-shaped knots (not shown) have an angle of 60 ° at the top, that is, the configuration illustrated in Figure 3a after turning Figure 90 °. The square diamond-shaped knots (not shown) have an angle of 90 °. The number of knots / horizontal centimeter is preferably in the range of between about 3.14 to about 5.90. The inventor has found from the test performed so far that 4.7 knots / horizontal centimeter can provide the best performance of those analyzed. Preferably, the knots have a depth 22 as shown in Figure 3b which are in the range of about .038 to about 0.15 centimeters, more preferably about 0.076 centimeters, depending on the number of knots / horizontal centimeter. Generally, the fewer the knots / centimeter, the greater the depth of. -the knots, and the more the knots / centimeter, the deeper depth will be deeper. Experimental results with diamond-shaped knots generally show that the higher the proportion of the liquid flow, the better the heat transfer coefficient will be. Figure 8 shows the heat transfer results obtained with the square diamond shaped knots (data points shown as black dots) and with the horizontal diamond shaped knots (data points shown as x) each having a separation of 4.72 knots / horizontal centimeter and a depth of about 0.076 centimeters. In Figure 8, U is the heat transfer coefficient and A is the heat transfer surface area. For the analysis of horizontal and square diamond shaped knots, the surface area of the heat transfer is the same. The data in Figure 8 represented with triangles represents the test of an initial design that worked much better than the absorbers, but they have a low heat transfer surface area because several design parameters have not been optimized. With the horizontal diamond-shaped knots, the curve in the upper left moves upward and something in the left provides better results with lower flows. The horizontal knots have been the best of the three at the lowest flow rates. In this way, for a 5-ton heat pump system, vertical diamond-shaped knots can work better, square diamond-shaped knots can work better for a 4-ton system, while knots in the form of Horizontal diamond can have a better performance in a 3-ton system. The tests performed to record have used a uniform type and size of knot on the total height of the GAX and the cooled sections of the rich solution of the absorber. However, the absorption of ammonia in the liquid causes the proportion of the liquid flow to increase as it flows down through the absorber, almost doubling the proportion of the flow at the outlet of the absorber. The improvements shown in Figure 8 are averages of increases that occur over the total heights and over the range of the proportions of the flows. The inventor believes that by modifying the shapes and size of the knots along the height of the absorber, each being in a better fit for the proportion of the flow of the liquid at a particular point can be obtained a much better performance. Another embodiment of the invention, as shown in Figures 4 and 5, allows control of the vapor flowing up through the absorber by keeping it as essentially a current rather than two or more. More important, in this mode, is that the contact of the vapor with the liquid is greatly improved. More than the slow vertical flow of ammonia vapor through the surface of the liquid, as in Figure 1, in this mode the vapor collides with the surface of the liquid at much higher speeds causing it to flow like a jet of ammonia vapor at right angles on the surface of the cylindrical liquid. In this embodiment of the invention, the shock is used to increase the absorption rates by means of the velocity of the vapor jets that collide on the liquid, by causing the mixing of the absorbent liquid where the steam collides, and by causing a greater movement of the liquid on the inner surface of the shell. This shock also causes the concentration of ammonia in the vapor and liquid to be closer to the equilibrium concentrations shown in Figure 2. In this embodiment, the vapor flow described above in relation to the liquid is achieved by means of a structure inside the shell of the absorber, shown in Figures 4 and 5. The purpose of this structure is to cause the steam to be directed through a sequence of collisions with the liquid flowing down on the inner surface of the breastplate. This mode creates a vapor current that is self-controlled and a single stream of liquid, which increases the total control of the process. The absorber of Figure 4 is composed of a vertical group of radially perforated steel cups, or flow deflectors 30, placed inside the absorber 10, which are upside down and separated apart to allow steam 32 to flow from one to another. The steam baffles 30 include a base 34 and an edge 36. The edge 36 extends from the base 34 to a skirt 38 at the end of the edge 36. The skirt 38 forms an access path with the surface of the interior wall for the liquid 39 flowing down through the absorber along the surface of the inner wall. The steam 32 enters the deflector 30 of the bottom flow and separates into several small streams that flow radially through perforations 40 (holes) in the cylindrical wall of the flow deflector 30. The jet of steam that leaves the holes created by perforations 40 flows radially towards the surface of the shell of the absorber, each to collide in the liquid on the gnarled surface of the shell of the absorber. At each shock stage, some vapor is rapidly absorbed by the shock process. Another amount is absorbed by contact with another liquid on the surface of the shell. The unabsorbed vapor, of a new composition, then flows upward in the next flow deflector through the open end 42 between the top of the bottom flow deflector and the bottom of the second flow deflector immediately above it. A portion of the ammonia vapor is thus absorbed into the liquid by means of the flow through each impact flow deflector. The steam is reduced in volume in each flow deflector and finally completely absorbed in the upper part. Steam and liquid in this way are brought close to one another in each shock stage. The compositions and the masses of the vapor and the liquid therefore change at each shock stage. Ideally, the number of shock stages could be very large, but the tests to record have shown that the practical quantities, probably up to about 36 for a complete absorber, are sufficient to achieve a fairly efficient absorption. For absorbers having a height in the range of about 91.44 to about 182.8 centimeters, it is believed that the preferred number of flow deflectors, i.e. the preferred number of shock stages, is in the range of about 14 to 36. It is preferred that in each flow deflector 30, the perforations 40 are of the appropriate diameter and number to produce the appropriate speed and amount of movement of the jets in relation to the volume of steam flowing through each flow deflector. The perforations must also be properly separated, generally in an alternate arrangement rather than in line, to produce the best absorption. At this stage in the development of the absorbers, several dimensions of the perforations (in the heat exchange sections of the GAX and the absorber) have been tested by trial and error and visualization tests with air and water. In the inventors' test to record, circular perforations have been used, although other forms of perforations can also be used in the. invention. The visualization tests lead to the conclusion that the optimum steam velocity through each perforation can be in the order of about 121.92 centimeters / second. Several designs were tested in order to obtain the desired speed. After developing the design configuration that achieves the desired speed, a subsequent test on an ammonia / water absorber confirms that the design that is based on a velocity of 121.92 centimeters / second, flows through the perforations in fact produce a transfer of heat much better than other proven designs. The diameter of the perforations of the flow deflector can be in the range of about 0.079 to about 0.79 centimeters. The inventor has found from the test that, for an absorber tube of 15.24 centimeters of ID, perforations of about 0.47 centimeters in diameter may have a better performance for flow deflectors in or near the bottom of the ICA section of the absorber At or near the top of the absorber, the smallest perforations in the order of about 0.079 to about 0.15 centimeters in diameter can work best. In this way, from the bottom to the top of the absorber,. the diameter of the perforations preferably can change gradually from about 0.476 to about 0.158 centimeters, more preferably from about 0.476 to about 0.082 centimeters. The number of perforation lines per flow deflector can be in the range of about 1 to about 6. It has been found that 4 perforation lines per flow deflector can provide the best performance. The number of perforations / line around the circumference of the flow deflector can be in the range of about 20 to about 50. The inventor has found that about 30 perforations / line around the circumference of the flow deflector can be best. The height of each flow deflector is preferably in the range of about 2.54 to about 7.62 centimeters, with the preferred height that is about 4.45 centimeters, depending on the height of the absorber. It is preferable that the flow deflectors consist of a metal or an alloy, such as steel, that is thin enough to provide a sharp hole, such as a thickness of about 0.05 of about 0.12 centimeters, more preferably close to 0.089 centimeters However, the flow deflectors may also be composed of polymeric materials or other suitable materials. The open end 42 of the flow deflectors 30, the bottom, are enlarged as shown in Figure 4, to form the peripheral steam orifice 32 to flow from a lower flow deflector to an upper one. The larger diameter in the projection is designed to be in contact, or near the contact, with the surface of the inner wall of the absorber, which is preferably knotty (not shown), so that it can serve as a means to establish a 44 close of liquid on the knotted surface. The liquid seal 44 has three purposes. It prevents the steam from escaping upwards through the knots, it serves as a water load to provide the necessary pressure to extract steam through the perforations 40, and it is an access way for the liquid at the lowest level. The seal is formed by the narrow contact of the skirt of the flow deflector with the knots. The altitude of the skirt in contact with the knots may be sufficient to allow the liquid loading of approximately 0.254-0.476 centimeters to cause the steam to be extracted through the perforations 40 of the flow deflectors. The flow deflectors 30 can be fixed in a place in the hollow interior of the housing. absorber, for example, when using spacers 46 as shown in Figure 4. Other suitable means known in the mechanical art for fixing workpieces in place can be used. As shown in Figure 5, to transfer the absorption heat of the GAX from the shell of the absorber 10 to the heat transfer liquor (which can be weak liquor, boiling rich liquor, or a liquor of intermediate concentration), a tube or GAX heat transfer tubes 50 for the transfer liquor are tightly wound around the cooled section 56 (section of the AHE) of the rich liquor and the secondary fluid tube coils 58 are wound around the hydronically cooled section 60 ( usually a secondary antifreeze fluid) of the absorber. See Figure 5. All the coils are then attached to the shell of the absorber 10 to obtain a good heat transfer for the three fluids that serve as the coolers. This metallic connection has been successfully realized by immersing the assembly completely sealed in molten tin. It can also be submerged in molten solder. Other methods such as welding with brass and welding are also other possibilities. Tinning, welding with tin and lead alloys, welding with brass and welding, etc. they are intended to provide a continuous metallic path for the heat that is transferred from the absorbent fluid to the fluid that is heated as shown in Figure 5 and, more specifically, by Figure 6. The solder or solder, or the strong solder etc. . they can preferably be made in a manner that they form welding angles of the bonding metal between the shell 77 and the tubes 78 to provide a broad path for heat flow, as opposed to the line contact that can occur when merely rolling the tube in. the breastplate
Mechanically, small tube spiers serve as collars around the shell, increasing the strength of the shell to withstand internal pressure. Thus, the thickness of the shell wall can be reduced, reducing weight and cost. All GAX heat transfer fluids described in the patents identified on page 1 and incorporated by reference herein may be used for the heat transfer of the GAX section of this absorber design. Figure 5 shows the absorber divided into three sections, the upper section 52 is the section of the GAX. The middle section 54, the section of the AHE, is used to heat the rich solution that must be heated from the outlet temperature of the absorber to the inlet temperature of the generator. The bottom section 60 in Figure 5 is the heat production section of the absorber. This section heats the secondary fluid that is used to separate heating in the winter and used to dissipate heat production to outside air in the summer, as shown in Figure 9. The rich solution and secondary fluid streams can flow in parallel paths through more than one coil, as shown in Figure 5. In the embodiment shown in Figure 5, the secondary fluid enters two parallel secondary fluid tube coils 58 through two parallel inlets 62 of secondary fluid and exits through the parallel 64 exits of secondary fluid. Similarly, the rich solution enters two coils of rich solution tube 54 parallel through two parallel inlets 66 of rich solution and exits through two parallel outlets 68 of rich solution. The purpose of using parallel tube coils for a stream is to improve the transfer of heat through the metal wall of the tubes to the fluid that is heated. The upper section (the GAX section) of the absorber in Figure 5 is cooled by, and transfers heat to, the GAX heat transfer fluid. There, the number of tube coils on the outer surface of the shell can vary as desired or is required by the heat transfer fluid. Figure 5 shows the three parallel GAX heat transfer fluid tube coils 50 which constitute a stream of the weak solution flowing through three passages in sequence as described in one embodiment (Figure 3) of the North American Patent. No. 5,367,884 ("884 patent"). In this embodiment of the invention, the tube coils 50 of the GAX heat transfer fluid have three inlets 70 that receive the weak liquor that has circulated through the heat transfer region of the generator (not shown) and three outputs 72, in two of the weak liquor circulates outside the absorber and returns to the generator, and one that returns the weak liquor to the entrance 73 of the absorber. In many tests conducted by the inventor, three passages have been very effective. However, as described in the '884 patent, it may also be a sequence of four parallel tube coils in the GAX section for four passages of the weak liquor (Patent Figure 4, 884) or up passage of rich liquor ( Figures 7, 7A, 8, 8A, of the? 884 patent); without tube coil (Figures 5 and 6 of the '884 patent); or two tube coils for two rich liquor passages (Figure 9 of the '884 patent). Other arrangements of tube coils can be used for the GAX section of the absorber as described in US Pat. Nos. 5,271,235, 5,570,584, 5,579,652 and 5,782,097. For example, for the combination of the weak liquor and boiling rich liquor of the US Patent No. 5,579,652 ("patent 652"), a coil of the weak liquor and a rich liquor coil (Figures 4 and 6 of the patent? 652 ) may be preferred, but other embodiments have only one rich liquor coil (Figures 3 and 5 of the '652 patent). For the intermediate liquor GAX system of US Patent No. 5, 570,584 ("patent '584"), one coil (Figures 4, 6, 7, and 9-11 of the' 584 patent) two serpentines (Figure 3 of the "patent? 584"), or three coils (Figure 12 of the "584 patent") carrying the intermediate liquor can be used. For the rich liquor modality of the North American Patent of US Pat. No. 5,782,097 ("patent 097"), a coil carrying the rich liquor (Figures 3 and 4 of the "097 patent") are preferably used. For the mode of US Patent No. 5,271,235, one or two coils can be used for the GAX section. The division of the absorber into three sections can also be performed as shown in Figure 7, wherein the low temperature section 80 of the bottom of the absorber 10 both heats the secondary fluid in a coil 82 of the secondary fluid and the liquor rich in a coil 84 of rich liquor. In the embodiment of Figure 7, the secondary fluid is introduced to a secondary fluid coil 82 through two parallel inlets 81 of the secondary fluid and exits through two parallel outlets 83 of the secondary fluid. The rich liquor is introduced into the coil 84 of the rich liquor through two parallel inlets 85 of the rich liquor and continues upwards to further warm up in the intermediate section 86, before exiting through two parallel outlets 87 of rich solution. The GAX heat transfer fluid is heated by the GAX heat transfer coil 88 adjacent to the GAX section 90. In Figure 7, unlike Figure 5, the rich liquor enters the coil 84 of the rich liquor at the bottom of the absorber 10 at the parallel inlets of the rich liquor where it is heated by heat which in Figure 5 is transferred to the secondary fluid. To ensure that the secondary fluid is heated to the desired temperatures in the embodiment of Figure 7, the coil 82 of the secondary fluid can extend beyond the section 80 of the low temperature from the bottom of the absorber 10 to the intermediate section 86 ( not shown). Alternatively, the ratio of the flow of the secondary fluid through the coil 82 of the secondary fluid can be reduced to allow the secondary fluid to be heated to the desired temperature at the parallel outlets 83 of the secondary fluid. The design of Figure 7 can also serve to produce two secondary fluid streams, one much hotter than the other, by using two secondary coils of different heights. The distribution of the liquid in the upper part of the absorber around the inner walls of the absorber can be done in manners known in the art. Preferably, a roll die 74 as shown in Figures 5 and 7 is used to spray the hot liquid on the top of the absorber after it has circulated between the heat transfer regions of the absorber and the generator. The roll nozzle 74 preferably introduces the liquid in the form of fine droplets into the hot steam at the top of the absorber. In their radial trajectories to the cylindrical inner wall of the absorber, the droplets absorb the hot steam in that space and are also heated by the absorption to be very close to the equilibrium temperature before coming into contact with the inner wall of the absorber. In this way, the upper part of the absorber is heated very close to the maximum temperature of the absorber, represented as point F in Figure 2 of US Patent No. 5,367,884.
It will be apparent to those with skill in the art that various modifications and variations may be made in the generator-absorber heat exchange apparatus of the invention without departing from the essence or scope of the invention. Thus, it is intended that the present invention cover the modifications and variations of this invention provided that fall within the scope of the claims and their equivalents. It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.