JP5547560B2 - Absorption heat pump - Google Patents

Description

  The present invention relates to an absorption heat pump that generates steam, and more particularly to an absorption heat pump including an absorber having a large number of heat transfer tubes.

  There is an absorption heat pump in which refrigerant vapor generated in an evaporator is guided to an absorber, and water is heated by absorption heat generated when the refrigerant vapor is absorbed by an absorbing solution in the absorber to obtain water vapor (for example, Patent Document 1). reference). In recent years, with such an absorption heat pump, a demand for an increase in size has been conspicuous.

JP 2006-138614 A

  However, when trying to increase the size of the absorption heat pump, the number of heat transfer tubes of the lively absorber increases. Then, a large deviation occurs in the flow rate of the fluid to be heated in the heat transfer tube, and the effective area ratio of the heat transfer tube decreases. In particular, it becomes prominent when the number of stages of pipe arrangement in the vertical direction increases. Especially in an absorption heat pump that tries to obtain water vapor, in a multi-pass structure in which the flow direction of the tube group is reversed at the tube plate part, when turning into a new tube group, there is a lot of liquid in the lower tube group, and the upper tube group There was a problem that the steam increased in volume, and when the mass flow rate was increased, a large flow rate flowed in the lower part, and the upper part of the steam accounted for most of the ratio, resulting in poor heat transfer.

  In view of the above-described problems, the present invention is an absorption heat pump capable of suppressing a decrease in the effective area ratio of the heat transfer tube without causing a large deviation in the flow rate of the heated fluid in the heat transfer tube of the absorber that generates the heated fluid gas. The purpose is to provide.

  In order to achieve the above object, the absorption heat pump 100A according to the first aspect of the present invention heats the fluid fluid 103 to be heated with absorbed heat generated by absorbing refrigerant gas, for example, as shown in FIG. An absorber A1 for generating a heated fluid gas; the absorber A1 is a heat transfer tube group 12 composed of a plurality of heat transfer tubes arranged horizontally, and sprays an absorbing liquid on the outside, and A heat transfer tube group 12 composed of a plurality of heat transfer tubes through which the heated fluid liquid flows; and a heated fluid chamber 121 for supplying the heated fluid liquid on the heated fluid liquid supply side of the heat transfer tube group 12; The fluid chamber 121 includes a partition 122 that divides the heat transfer tube group 12 into an equal number of divided heat transfer tube groups 12a and 12b in the vertical direction; Supply ports 131a-1, 131b-1 To.

  When configured as in this aspect, the absorber has a heat transfer tube group, and the heated fluid chamber of the heat transfer tube group is a partition that divides the heat transfer tube group into equal number of divided heat transfer tube groups in the vertical direction; Since each divided heat transfer tube group has a supply port that supplies the heated fluid liquid evenly, there is no large deviation in the flow rate of the heated fluid in the heat transfer tube of the absorber, and a reduction in the effective area ratio of the heat transfer tube is suppressed. can do.

  The absorption heat pump according to the second aspect of the present invention is the absorption heat pump according to the first aspect. For example, as shown in FIG. 1, the supply ports 131 a-1 and 131 b-1 are connected to the divided tube groups 12 a and 12 b. Distributing mechanisms 132a and 132b that evenly distribute the fluid to be heated are provided.

  When configured as in this aspect, the supply port has a distribution mechanism that evenly distributes the heated fluid liquid to the divided tube group, so that a large deviation in the flow rate of the heated fluid in the heat transfer tube does not occur more reliably. The absorption heat pump which can suppress the reduction | decrease of the effective area ratio of a heat exchanger tube can be provided.

  The absorption heat pump according to the third aspect of the present invention is the absorption heat pump 100A, 100B according to the first aspect or the second aspect. For example, as shown in FIGS. 4 and 5, each divided heat transfer tube group 12a, Each of 12b is composed of a plurality of paths (three paths in FIGS. 4 and 5).

  When configured in this manner, each divided heat transfer tube group is configured in a plurality of paths, so that the flow rate of the fluid to be heated in the heat transfer tube of the absorber is not greatly biased and the effective area ratio of the heat transfer tube is reduced. The length of the heat transfer tube can be shortened while suppressing the above. In other words, since there are multiple paths, the number of heat transfer tubes increases. And since there are multiple passes, the flow direction is reversed when one pass is over, and the distribution of liquid and gas tends to be uneven in the lower and upper heat transfer tube groups, but it is divided into divided heat transfer tube groups And a supply port that supplies the heated fluid liquid evenly to each divided heat transfer tube group, so that the heat transfer tube is effective without causing a large deviation in the flow rate of the heated fluid in the heat transfer tube of the absorber. A reduction in the area ratio can be suppressed.

  The absorption heat pump according to the fourth aspect of the present invention is the absorption heat pump 100A, 100B according to any one of the first to third aspects, for example, as shown in FIGS. A gas-liquid separator 22 for introducing the heated fluid gas generated in the containers A1-1 and A1-2 and separating the heated fluid gas and the heated fluid liquid accompanying the heated fluid gas; Absorbers A1-1 and A1-2 on the outlet side of the divided tube groups 12a and 12b and the connection ports 22a of the gas-liquid separator 22 so that the entire divided heat transfer tube groups 12a and 12b are immersed in the fluid to be heated. 22b or the heated fluid chamber 128 on the heated fluid outlet side of the divided tube groups 12a and 12b is formed.

  If comprised like this aspect, since it comprises so that the whole division | segmentation heat exchanger tube group may be immersed in the said to-be-heated fluid liquid, the blow-by of the gas of to-be-heated fluid can be suppressed.

  ADVANTAGE OF THE INVENTION According to this invention, the absorption heat pump which can suppress the reduction | decrease of the effective area ratio of a heat exchanger tube without producing big bias | deviation in the fluid flow rate to be heated in the heat exchanger tube of the absorber which generates a fluid fluid to be heated is provided. It becomes possible.

It is a typical systematic diagram of the absorption heat pump of the single stage temperature rising which is embodiment of this invention. It is a typical systematic diagram of the absorption heat pump of the two-step temperature rising which is embodiment of this invention. It is the typical partial systematic diagram which extracted and showed the absorber and gas-liquid separator of the absorption heat pump which concern on embodiment of this invention. It is a typical sectional view explaining the absorber of a first embodiment of the present invention. It is typical sectional drawing explaining the absorber of 2nd embodiment of this invention. It is typical sectional drawing explaining the modification of the absorber of 1st embodiment of this invention. It is typical sectional drawing explaining the case where a to-be-heated fluid is circulated between an absorber and a gas-liquid separator using a bubble pump function.

  Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or similar members are denoted by the same or similar reference numerals, and redundant description is omitted.

  First, an absorption heat pump 100A according to a first embodiment of the present invention will be described with reference to the schematic system diagram of FIG. As illustrated, the present absorption heat pump includes an absorber A1, an evaporator E1, a regenerator G, a condenser C, and a solution heat exchanger X1 as main components. In the present embodiment, typically, an aqueous solution of lithium bromide is used as an absorbing solution (dilute solution or concentrated solution), and water is used as a refrigerant.

  The operation of the main component equipment is as follows. The absorber A1 heats and evaporates the water as the fluid to be heated with the absorption heat generated when the solution absorbs the refrigerant vapor. The evaporator E1 heats and evaporates the water as the refrigerant liquid with the hot water 102 as the heat source, and sends the water vapor as the refrigerant vapor to the absorber A1. The regenerator G regenerates the solution by generating the refrigerant vapor by heating the dilute solution having a reduced concentration by absorbing the refrigerant vapor in the absorber A1 (making it a concentrated solution). The condenser C cools the refrigerant vapor generated in the regenerator G with the cooling water 101 and condenses it. The solution heat exchanger X1 exchanges heat between the diluted solution from the absorber A1 and the concentrated solution from the regenerator G.

  The absorption heat pump 100A further includes a concentrated solution tube 2 that guides the concentrated solution from the regenerator G to the absorber A1 by the solution pump 1, a diluted solution tube 4 that guides the diluted solution from the absorber A1 to the regenerator G, and a refrigerant liquid. The refrigerant pipe 6 is connected to the evaporator E1 from the condenser C by the refrigerant pump 5, and the refrigerant pipe 6a for returning the refrigerant liquid not evaporated by the evaporator E1 to the suction side of the refrigerant pump 5, which connects each device. doing. A heat exchanger X2 is inserted and disposed in the refrigerant pipe 6 and the refrigerant pipe 6a. Between the refrigerant liquid sent from the condenser C to the evaporator E1 and the refrigerant liquid returned from the evaporator E1 to the suction side of the pump 5. Heat exchange. In this way, the pump 5 for sending the refrigerant liquid from the condenser C to the evaporator E1 also serves as a pump for spraying the refrigerant liquid on the evaporator E1, so that one pump can be omitted. The refrigerant pipe 6a may be directly connected to the condenser C. Further, a flow path 7 is provided between the evaporator E1 and the absorber A1 to guide the refrigerant vapor evaporated in the evaporator E1 to the absorber A1, and between the regenerator G and the condenser C, the regeneration is performed. And a flow path 8 for guiding the refrigerant vapor generated in the condenser G to the condenser C.

  The condenser C has a cooling water pipe 9 that leads the cooling water 101, the evaporator E1 and the regenerator G have hot water pipes 10 and 11 that lead the heat source hot water 102, and the absorber A1 to obtain a desired high-temperature steam. A heat transfer tube (heat transfer tube group) 12 is provided.

  On the other hand, the absorption heat pump 100A of the present embodiment includes a gas-liquid separator 22 that separates water as a heated fluid heated by the absorber A1 into liquid water and water vapor. A makeup water pipe 3 is connected to the gas-liquid separator 22. A makeup water pump 16 and a makeup water heater 15 are arranged in the makeup water pipe 3. Hot water 102 is supplied to the makeup water heater 15 to heat (preheat) the water 103 as the fluid to be heated.

  The gas-liquid separator 22 is provided with a liquid level gauge L3, and the liquid level in the gas-liquid separator 22 is brought to a predetermined level by controlling the replenishment water pump 16 with the detection output of the liquid level gauge L3. maintain.

  A supply pipe 3a for supplying water 103 as a fluid to be heated from the gas-liquid separator 22 is connected to the inlet of the heat transfer pipe 12 of the absorber A1, and the gas-liquid separator 22 is connected to the outlet side of the heat transfer pipe 12. A return pipe 3b (3b-1, 3b-2, 3b-3) for returning the water vapor evaporated by the absorber A1 is connected to the main body.

  From the gas-liquid separator 22, the water 103 of about 1 to 3 times (more preferably 1.5 to 2 times) the amount of evaporation is introduced into the heat transfer tube 12 of the absorber A1. In this manner, the heat transfer coefficient on the water side that is the fluid to be heated can be increased. The gas-liquid separator 22 includes a pressure detector P1 and a controller CONT. The controller CONT adjusts the opening degree of the control valve 41 so that the internal pressure of the gas-liquid separator 22 detected by the pressure detector P1 is maintained at a predetermined set value.

  In the absorption heat pump having the above configuration, when the heat source hot water 102 is supplied to the hot water pipe 11 of the regenerator G, the solution in the regenerator G evaporates to become a concentrated solution. The concentrated solution is heated by the solution pump 1 through the solution heat exchanger X 1, sent to the absorber A 1, and sprayed on the heat transfer surface of the heat transfer tube 12. On the other hand, the refrigerant sent to the evaporator E1 by the refrigerant pump 5 is heated and evaporated by the heat source hot water 102 passing through the hot water pipe 10. The refrigerant vapor reaches the absorber A1 through the flow path 7 and is absorbed by the sprayed concentrated solution, and the concentrated solution becomes a diluted solution. The concentrated solution is heated to a high temperature by the absorbed heat at this time, heats the heat transfer surface of the heat transfer tube 12, heats the water 103 passing through the heat transfer tube 12, generates steam 104, and is discharged from the heat transfer tube 12. The

  The dilute solution in the absorber A1 passes through the dilute solution tube 4, and the concentrated solution passing through the concentrated solution tube 2 is heated by the solution heat exchanger X1 and returned to the regenerator G. The steam generated in the regenerator G reaches the condenser C through the flow path 8, is cooled and condensed by the cooling water 101 passing through the cooling water pipe 9, and the cycle is repeated.

  The absorber A1 is provided with a liquid level gauge L1 for detecting the liquid level of the solution accumulated at the bottom. A solution outlet is provided at the bottom. The detection output of the liquid level gauge L1 is sent to the inverter 18 that drives the solution pump 1, and the solution pump 1 is controlled. Thereby, the flow rate of the concentrated solution sent from the regenerator G to the absorber A1 is controlled, and the liquid level of the solution level accumulated at the bottom of the absorber A1 is maintained at a specified level.

  The evaporator E1 is also provided with a liquid level gauge L2 for detecting the liquid level of the refrigerant liquid accumulated at the bottom. A refrigerant liquid outlet is provided at the bottom. The detection output of the level gauge L2 is output to the control valve 20, and the control valve 20 is controlled to control the flow rate of the refrigerant supplied from the condenser C to maintain the liquid level of the refrigerant liquid in the evaporator E1. .

  The specific structure of the absorber A1 will be described in detail later with reference to FIGS.

  With reference to FIG. 2, the other structural example of the absorption heat pump which concerns on this invention is demonstrated. This absorption heat pump is an example of two-stage temperature rise. As shown in this figure, a high-temperature absorber AH and a gas-liquid separator EHS are provided. Here, the absorber A2 corresponding to the absorber A1 in FIG. 1 is a low-temperature absorber, and the evaporator E2 corresponding to the evaporator E1 is a low-temperature evaporator. Further, the high temperature evaporator EH is on the heated side of the low temperature absorber A2.

  The refrigerant liquid sent from the condenser C through the refrigerant pipe 6 is supplied to the gas-liquid separator EHS through the control valve 32 and the refrigerant branch pipe 30. On the other hand, the refrigerant vapor from the high-temperature evaporator EH is sent to the gas-liquid separator EHS through the refrigerant pipe 34-1. Thereby, the refrigerant liquid from the condenser C is heated and evaporated by the gas-liquid separator EHS. The refrigerant liquid separated from the gas and liquid returns to the low-temperature absorber A2 through the refrigerant pipe 34-2. A baffle plate 33 is provided in the gas-liquid separator EHS. The baffle plate 33 separates the refrigerant liquid from the refrigerant gas by causing the gas liquid to collide with the baffle plate 33 so that the refrigerant liquid does not flow to the high temperature absorber AH.

  The concentrated solution from the regenerator G is heated (preheated) by the solution pump 1 through the solution heat exchanger X1 and the heat exchanger X3, and sent to the high-temperature absorber AH. Here, the refrigerant vapor from the gas-liquid separator EHS is absorbed by the concentrated solution, and the concentrated solution becomes a diluted solution. The concentrated solution is heated to a high temperature by the absorbed heat at this time, and the heat transfer surface of the heat transfer tube 35 is heated, and the water 103 passing through the heat transfer tube 35 is heated to become steam. The water vapor is introduced into the gas-liquid separator 22 to be gas-liquid separated, and the water vapor 104 is discharged from the vapor pipe 13.

  The dilute solution in the high temperature absorber AH passes through the dilute solution tube 37, heats the concentrated solution sent to the high temperature absorber AH by the heat exchanger X3, and flows into the low temperature absorber A2 through the control valve 40. The control valve 40 is controlled by the output of the liquid level gauge L1 that detects the liquid level of the solution accumulated at the bottom of the low temperature absorber A2, and the liquid level of the solution level at the bottom of the low temperature absorber A2 is maintained at a predetermined level. . The high temperature absorber AH is provided with a liquid level gauge L4 for detecting the liquid level of the solution at the bottom. The detection output of the level gauge L4 is sent to the inverter 18 that drives the solution pump 1, and the rotational speed of the solution pump 1 is adjusted to adjust the flow rate of the concentrated solution sent to the high temperature absorber AH, thereby absorbing the high temperature. The liquid level of the solution at the bottom of the vessel AH is maintained at a predetermined level.

  The gas-liquid separator EHS is provided with a liquid level gauge L5 for detecting the liquid level of the refrigerant liquid accumulated at the bottom, and the control valve 32 is adjusted by the detection output of the liquid level gauge L5 to The liquid level of the separator EHS is maintained at a predetermined level. Further, the liquid level of the refrigerant liquid accumulated at the bottom of the low temperature evaporator E2 is also maintained at a predetermined level by adjusting the control valve 20 with the detection output of the liquid level gauge L2 to adjust the amount of refrigerant liquid supplied from the condenser C. To do.

  The absorption heat pumps 100A and 100B having the configurations shown in FIGS. 1 and 2 are described as spray-type evaporators in which the evaporators E1 and E2 are sprayed with the refrigerant liquid from the condenser C on the heat transfer tubes that guide the heat source hot water 102. However, a configuration in which a heat transfer tube that guides the heat source hot water 102 into the refrigerant liquid may be provided. The former is suitable for an evaporator operating at a relatively low temperature, and the latter is suitable for an evaporator operating at a relatively high temperature. In the temperature rising type absorption heat pump as in the present embodiment, unlike the absorption refrigerator, the evaporator operates at a relatively high temperature, so the latter can often be used. With such a configuration, in the two-stage temperature rising absorption heat pump, not only the high temperature absorber AH but also the low temperature absorber A2 has a large deviation in the flow rate of the heated fluid in the heat transfer tube of the absorber that generates the heated fluid gas. Therefore, the absorption heat pump that can suppress the reduction in the effective area ratio of the heat transfer tubes of both absorbers, that is, the absorption heat pump as a whole, has a high COP and can easily obtain high-temperature steam. .

  With reference to FIG. 3, the structure of absorber A1 with which embodiment of this invention is provided is demonstrated. In FIGS. 1 and 2, the configurations of the absorbers A1 and AH are only shown to a sufficient extent to explain what action the overall configuration of the absorption heat pumps 100A and 100B has. The specific structure will be described below. The high-temperature absorber AH of FIG. 2 has the same structure as the absorber A1 of the absorption heat pump 100A of FIG. 1, but will be described as the absorber A1 below. The low temperature absorber A2 in FIG. 2 can also be applied with the same configuration because the refrigerant evaporates in the heat transfer tube.

  Specifically, the absorber A1 suitable for the embodiment of the present invention includes a heat transfer tube group 12 including a plurality of heat transfer tubes arranged horizontally. The heat transfer tube group 12 is equally divided into divided heat transfer tube groups 12a, 12b, and 12c. This figure shows a case where the number of divided heat transfer tube groups is three. However, the number of divided heat transfer tube groups may be two or four or more. The heat transfer tube group 12 (12a, 12b, 12c) is sprayed with an absorbing liquid on the outside thereof, and water as a fluid to be heated is allowed to flow inside each heat transfer tube.

  The deviation of the flow rate of the fluid to be heated becomes remarkable when the number of heat transfer tubes arranged in the vertical direction increases. Accordingly, the heat transfer tube group 12 is divided into a plurality of parts in the vertical direction.

  A more specific structure of the absorber A1 will be described with reference to FIG. Here, as a first embodiment, an explanation will be given of the absorber A1-1 when the number of divided heat transfer tube groups is two. A first water chamber 121 as a heated fluid chamber for supplying water is provided on the side of supplying water as the heated fluid liquid of the heat transfer tube group 12. The first water chamber 121 includes a partition 122 that divides the heat transfer tube group 12 into equal number of divided heat transfer tube groups 12a and 12b in the vertical direction. Here, the heated fluid chamber is specifically referred to as a water chamber. In some cases, only steam collects in this water chamber, but for convenience, it is also called a water chamber.

  Here, the equal number is typically the same number, but may be substantially the same number. In other words, the number of heat transfer tubes in the divided heat transfer tube groups 12a and 12b may be an equal number so that the flow rate of water, which is the fluid to be heated flowing into each heat transfer tube, is not excessive and does not cause a large deviation. For example, if the number of tubes exceeds 170, the flow rate will be uneven (whether the unevenness occurs due to vertical and horizontal distribution, the diameter of the heat transfer tube, the temperature of the water vapor to be obtained by the absorber, etc.) Although the limit number or the number of vertical stages are different, it is expressed here as a number), but it is assumed that the required number of absorber tubes is 480.

  In this case, when divided into two divided heat transfer tube groups, the number of tubes in each divided heat transfer tube group is 240. This is more than the limit number of 170 at which the flow rate is not biased. Next, when divided into three divided heat transfer tube groups, the number of tubes in each divided heat transfer tube group is 160. This is less than the limit number of 170 at which the flow rate is not biased. Therefore, it can be seen that the division into three is sufficient. In this case, the equivalent number is typically 160, but it may be divided into three parts of 150, 160, and 170. This is also included in the concept of an equal number. This is because the number is within a range that produces an effect that the flow is not biased.

  Here, the case where the first water chamber 121 is divided into two divided water chambers 121a and 121b by being partitioned by the partition 122 will be described. The divided water chambers 121a and 121b cover the divided heat transfer tube groups 12a and 12b, respectively.

  The two divided water chambers 121a and 121b, and thus the divided heat transfer tube groups 12a and 12b, are typically divided so as to be lined up and down (the same applies to three or more divided water chambers and divided heat transfer tube groups). Divided so that they line up vertically). By dividing in this way, it is possible to avoid that each divided heat transfer tube group is arranged long in the vertical direction.

  Furthermore, supply ports 131a-1 and 131b-1 for supplying water equally to the divided water chambers 121a and 121b and thus supplying water equally to the divided heat transfer tube groups 12a and 12b are provided in the divided water chambers 121a and 121b, respectively. It has been. Supply pipes 131a and 131b are connected to the supply ports 131a-1 and 131b-1, respectively. The supply pipes 131a and 131b are branched from the supply pipe 131. In other words, water as the fluid to be heated is supplied from the supply pipe 131 to the divided water chambers 121a and 121b in parallel and evenly via the supply pipes 131a and 131b. The supply pipes 131a and 131b are provided with orifices 132a and 132b as distribution mechanisms for evenly distributing water to the divided heat transfer tube groups 12a and 12b, respectively, as part of the supply ports 131a-1 and 131b-1. .

  These are orifices in which the size of the opening is adjusted so that the pressure loss cancels the difference in the position heads (and the flow loss of the pipes) of the divided tube groups 12a and 12b. Thus, for example, the opening of the orifice 132b disposed below is smaller than the opening of the orifice 132a disposed above. This is because the position head is larger in the lower part, so that a relatively small opening is sufficient.

  The reason for inserting orifices in both systems is that if the loss in the piping and heat transfer tube group is small, the flow distribution may vary greatly depending on the slight difference in pressure loss between the two systems (for example, the presence or absence of a bend). This is in order to suppress the influence of other pressure loss differences. At this time, if it is necessary to consider the position head, adjustment is made by changing the resistance for each orifice.

  As a distribution mechanism that evenly distributes water, for example, a distribution mechanism that has the same effect in terms of the size and length of the piping may be used without providing it in a clearly visible form such as an orifice. . In addition, the case where it is divided into three parts of 150, 160, and 170 and this is also included in the concept of an equal number has been described, but the supply port for supplying the heated fluid liquid equally to the divided heat transfer tube group As described above, the fluid to be heated may be supplied so as to meet each of the so-called evenly distributed heat transfer tube groups. Therefore, as long as the position head of the divided tube group does not cause a problem, the pipe size may be simply made equal, or the pipe size may be commensurate with the number of heat transfer tube groups having a slight difference.

  In addition, when there is no pump for circulating the heated water and it is circulated by the bubble pump function (see FIG. 7), an orifice is not provided, and a piping from each divided water chamber outlet to the gas-liquid separator 22 is provided separately. By adjusting the height (ha, hb, hc) from the outlet to the gas-liquid separator inlet, uniform distribution is performed. When it is difficult to adjust the height, a gas-liquid separation chamber may be provided separately to aim at even distribution. In this case, the vapor side of each separator is communicated, and the liquid level is adjusted by each separator. Note that the bubble pump capacity is determined by the pushing-in of the liquid and the height of the gas-liquid two-phase part.

  In the absorber of the first embodiment shown in FIG. 4, 12 heat transfer tube groups 12 are arranged in the vertical direction (the number in the horizontal direction (the depth direction in the figure is not shown, for example, 15)). ing. This is divided into two in the longitudinal direction (vertical direction) into the divided heat transfer tube group 12a and the divided heat transfer tube group 12b. The first water chamber 121 is divided by a partition 122 into divided water chambers 121a and 121b that cover the divided heat transfer tube group 12a and the divided heat transfer tube group 12b, respectively.

  Both ends of the heat transfer tube group 12 are expanded to two opposing tube plates 125 and 126 to constitute a shell and tube heat exchanger. The first water chamber 121 is welded and connected to the tube plate 125 to form a water chamber. On the opposite side of the first water chamber 121, a second water chamber 123 is welded and connected to the tube plate 126 to form a water chamber.

  The heat transfer tube group 12 in which 12 tubes are arranged in the vertical direction is covered at both ends by a first water chamber 121 and a second water chamber 123. The second water chamber 123 is provided with a partition 124 corresponding to the partition 122 of the first water chamber, and the second water chamber is divided water that covers the divided heat transfer tube group 12a and the divided heat transfer tube group 12b, respectively. It is divided into chambers 123a and 123b. Therefore, it can be said that the heat transfer tube group 12 is divided into the divided heat transfer tube groups 12a and 12b by the partitions 122 and 124. Each of the divided heat transfer tube groups 12a and 12b divided into two is further divided into six, one, two, and three from below. Thus, in the absorber A1-1 of the present embodiment, the divided tube groups 12a and 12b are each formed in three passes.

  Note the divided heat transfer tube group 12b divided into one, two, and three heat transfer tube groups. The divided heat transfer tube group 12b is divided into a lower one heat transfer tube group, a middle two heat transfer tube group, and an upper three heat transfer tube group by a partition 122-1b in the divided water chamber 121b. It is divided and divided by a partition 124-1b in the divided water chamber 123b into a heat transfer tube group consisting of one lower row, a heat transfer tube group consisting of two middle rows, and a heat transfer tube group consisting of three upper rows.

  That is, in the first water chamber 121b, the lower one heat transfer tube group is covered by the divided water chamber 121b-1, and the middle two heat transfer tube group and the upper three heat transfer tube group. Is covered with a divided water chamber 121b-2. Further, in the second water chamber 123b, the lower one heat transfer tube group and the middle two heat transfer tube group are covered by the divided water chamber 123b-1, and the upper three heat transfer tube group. Is covered with a divided water chamber 123b-2.

  In other words, the heat transfer tube group 12b is divided into a heat transfer tube group consisting of a single lower row and a middle heat transfer tube group by means of a partition 122-1b in the divided water chamber 121b and a partition 124-1b in the divided water chamber 123b. It is divided into a heat tube group and an upper three heat transfer tube group. Thus, the divided heat transfer tube group 12b of the absorber A1-1 is configured as a three-pass heat exchanger.

  The same applies to the divided heat transfer tube group 12a above the divided heat transfer tube group 12b.

  The divided water chamber 123b-2 of the divided water chamber 123b of the second water chamber is connected to the connection port 22b of the gas-liquid separator 22 by the pipe 133b, and the divided water of the divided water chamber 123a of the second water chamber is divided. The chamber 123a-2 is connected to the connection port 22a of the gas-liquid separator 22 by a pipe 133a. The connection port 22b is disposed vertically above the outlet of the divided water chamber 123b-2, and thus vertically above the heat transfer tube group 12b, and the connection port 22a is vertically above the outlet of the divided water chamber 123a-2. As a result, it arrange | positions rather than the heat exchanger tube group 12a at the perpendicular direction. Therefore, only the steam does not blow through the pipes 133a and 133b from the heat transfer pipes (steam gathers and wins) arranged at the top of the uppermost divided heat transfer pipe group of the heat transfer pipe groups 12a and 12b.

  The gas-liquid separator 22 is formed in a vertically long shape, and a baffle plate 22e is arranged in the vertical direction in the upper space. The connection ports 22a and 22b are provided to face the baffle plate 22e. Therefore, the water vapor mixed with liquid water blown into the gas-liquid separator 22 from the connection ports 22a and 22b collides with the baffle plate 22e, and the liquid water is separated. Below the baffle plate 22e is a passage opened between the bottom and the water surface of the gas-liquid separator 22. Accordingly, the water vapor and water that have flowed downward along the baffle plate 22e collide with the water surface and further separate the gas and liquid. The water vapor completely separated from the liquid water flows upward along the baffle plate 22 e and is led out from the vapor pipe 13 connected to the top of the gas-liquid separator 22. The water separated from the steam collects at the bottom of the gas-liquid separator 22.

  With reference to FIG. 4, the operation of the absorber A1-1 used in the first embodiment will be described. Liquid water as the fluid to be heated supplied from the supply pipe 131 is divided into the supply pipe 131a and the supply pipe 131b branched from the supply pipe 131. Since the supply pipe 131a and the supply pipe 131b are respectively provided with the orifices 132a and 132b, the divided water flows equally to the supply pipe 131a and the supply pipe 131b. Here, “equal” means equal to the extent that there is no significant bias in heat transfer.

  The water that has flowed into the supply pipe 131b flows into one pipe group in the vertical direction of the lower stage (for example, 15 pipes in the horizontal direction). In this tube group, the absorption heat is mainly given as sensible heat from the absorption liquid (solution) outside the heat transfer tube, and the temperature of water as the heated fluid rises. Part of it evaporates here.

  The liquid water and water vapor that have flowed into the divided water chamber 123b-1 from the lower heat transfer tube group are reversed in the divided water chamber 123b-1, and flow into the middle two vertical heat transfer tube groups. In this heat transfer tube group, a considerable amount of water becomes steam.

  Liquid water and water vapor flowing from the middle heat transfer tube group into the divided water chamber 121b-2 are reversed in the divided water chamber 121b-2 and flow into the upper three heat transfer tube groups in the vertical direction. In this heat transfer tube group, the water that has not evaporated so far evaporates into water vapor. In the present embodiment, the amount of water supplied from the supply pipe 131 is 1 to 3 times (more preferably 1.5 to 2 times) the amount of water to be evaporated. That is, the ratio of the supply water to the evaporation water of the supply water is 1 to 3 times or 1.5 to 2 times. When the supply water ratio is 1, almost all of the supplied water evaporates in the absorber A1-1. Therefore, only water vapor is output to the gas-liquid separator 22 from the upper heat transfer tube group. When the supply water ratio is twice, half the amount of water, and when the supply water ratio is three times, nearly 70% of the supplied water comes out to the gas-liquid separator 22. In any case, the volume is overwhelmingly water vapor.

  The reason why the number of heat transfer tube groups is increased to 1 in the lower stage, 2 in the middle stage, and 3 in the upper stage is that, as described above, the proportion of steam increases in the upward direction and the volume flow rate increases.

  Thus, according to the present embodiment, since the number of heat transfer tube groups in the vertical direction is three even in the upper stage, it is possible to suppress an uneven flow of water vapor mixed with flowing water. The operation is the same in the heat transfer tube group 12a having the same structure.

  In the conventional technique corresponding to the present embodiment, that is, the conventional technique that is not divided from the heat transfer tube groups 12a and 12b, the number of heat transfer tube groups in the upper stage of three passes is six. In the water chamber on the tube plate 125 side, the divided water chamber covering the middle and upper stages is long in the vertical direction, so that gas and liquid are separated in this, and the gas and liquid flowing into the six tube groups are biased. . To make it worse, only one of the uppermost tubes of the six tube groups is likely to flow with water vapor. That is, a blow-through occurs. As a result, the gas-liquid flowing in the lower pipe has a higher liquid ratio and a poor flow. Therefore, the heat transfer efficiency of the entire absorber must be lowered.

  On the other hand, according to the embodiment of the present invention, since the heat transfer tube group is divided, it is possible to suppress the uneven flow of water vapor mixed with water flowing in the heat transfer tube, and to transfer the entire absorber A1-1. Thermal efficiency can be kept high, and thus the COP of the absorption heat pump can be kept high. Further, the temperature of the steam that can be generated can be increased.

  In the above embodiment, piping from each divided water chamber outlet to the gas-liquid separator 22 is provided separately. However, as shown in FIG. 6, each outlet chamber (absorption in the first embodiment in FIG. 4) is provided. In terms of a vessel, the divided water chamber 123a-2 and the divided water chamber 123b-2) can be integrated into a single pipe 133e from the outlet to the gas-liquid separator inlet. In this case, it is desirable to increase the resistance of the orifice in order to supply water to be heated evenly distributed.

  Next, with reference to FIG. 5, the structure and operation of the absorber A1-2 used in the absorption heat pump according to the second embodiment will be described. The absorber A1-2 of the present embodiment is the same as the absorber A1-1 of the first embodiment except for the structure of the second water chamber 128. Here, it demonstrates centering on a different point from absorber A1-1.

  A second water chamber 128 is provided by being welded and connected to the tube plate 126. The second water chamber 128 forms one space so as to cover both the heat transfer tube groups 12a and 12b. In the internal space of the second water chamber 128, there is an internal water chamber 128a-1 in which the lower vertical direction of the heat transfer tube group 12a covers one heat transfer tube group and the middle vertical direction covers two heat transfer tube groups. Is provided. Adjacent to the upper part, an internal water chamber 128a-2 is provided in which the upper vertical direction covers three heat transfer tube groups.

  The upper part of the internal water chamber 128 a-2 is opened in the second water chamber 128. The internal water chamber 128a-2 forms a liquid pool in which water, which is a fluid to be heated that has not evaporated, accumulates. An edge 128c is formed on the opened top. The open upper edge 128c is formed such that the accumulated water overflows beyond it. The height of the edge is determined so that the accumulated water completely covers up to the three uppermost heat transfer tube groups in the vertical direction.

  Since the internal water chamber 128a-2 is configured as described above, the water accumulated here covers the upper heat transfer tube group, and steam blows through the upper heat transfer tube group. Can be suppressed. In the present embodiment, since the heat transfer tube group is divided into divided heat transfer tube groups, the flow rate of water, which is the fluid to be heated, is not greatly biased, but by forming the internal water chamber 128a-2, It becomes possible to reliably suppress the blow-through.

  Similarly, in the internal space of the second water chamber 128, an internal water chamber 128b-1 corresponding to the internal water chamber 128a-1 is provided, and an internal water chamber 128b-2 corresponding to the internal water chamber 128a-2 is provided. Is provided. The internal water chamber 128b-2 has an upper edge 128d corresponding to the upper edge 128c.

  Above the second water chamber 128, a steam passage 133c for sending steam toward the gas-liquid separator 22 is provided, and the steam passage 133c is connected to the gas-liquid separator 22 through a supply port 22c. Further, below the second water chamber 128, a water passage 133d for sending liquid water that has not evaporated by the absorber A1-2 toward the gas-liquid separator 22 is provided, and the water passage 133d is connected to the supply port 22d. To the gas-liquid separator 22.

  The water vapor that has passed through the water accumulated in the internal water chamber 128a-2 in the form of bubbles exits into the space of the second water chamber 128, and is then guided to the gas-liquid separator 22 through the vapor passage 133c. The high temperature water that overflows the edge 128c of the internal water chamber 128a-2 exits into the space of the second water chamber 128 and then accumulates at the bottom thereof, and is guided to the gas-liquid separator 22 through the water passage 133d. The same applies to the internal water chamber 128b-2. In the present embodiment, since the second water chamber 128 has a function as a gas-liquid separator, the gas-liquid separator 22 can be omitted or simplified.

  Since it comprises in this way, in absorber A1-2, since the heat exchanger tube group is divided | segmented into the division | segmentation heat exchanger tube group, the big deviation does not arise in the flow volume of the water which is a to-be-heated fluid, and suppresses the blow-by of a vapor | steam. Can do. Furthermore, since the water accumulated in the internal water chambers 128a-2 and 128b-2 covers the upper heat transfer tube group, it is further ensured that steam blows through the upper heat transfer tube group through the upper heat transfer tube group. It becomes possible to suppress.

  In the above embodiment, the divided heat transfer tube group has been described in the case of three passes in which the divided heat transfer tube group is divided into a lower stage, a middle stage, and an upper stage. In that case, if it demonstrates with absorber A1-1, the division | segmentation water chamber 121b-2 will be connected to the gas-liquid separator 22. FIG. It can also be applied to four or more passes.

  As described above, when the absorption heat pump has a large capacity and the number of heat transfer tubes of the absorber that generates steam increases, a large deviation occurs in the flow rate of the fluid to be heated in the heat transfer tubes, and the effective area ratio of the heat transfer tubes decreases. To do. In particular, it becomes prominent when the number of stages of pipe arrangement in the vertical direction increases. In particular, in a multi-pass structure in which the flow direction of the tube group is reversed at the tube plate part, when turning and entering a new pipe, there is a lot of liquid in the lower pipe, more steam in the upper part, and more in the lower part when making a mass flow rate. The upper part of the flow is steam, and the upper part of the steam makes up most of the ratio, resulting in poor heat transfer. However, according to the embodiment of the present invention, the heat transfer tube group of the absorber is divided, so that even if the number of heat transfer tubes in the absorber increases, a large deviation occurs in the flow rate of the heated fluid in the heat transfer tubes. It is possible to suppress the reduction of the effective area ratio of the heat transfer tube. In other words, it is possible to suppress the steam from occupying the upper part of the heat transfer tube group, and it is possible to maintain heat transfer well.

DESCRIPTION OF SYMBOLS 1 Solution pump 2 Concentrated solution pipe 3 Supply water pipe 3a Supply pipe 3b, 3b-1, 3b-b-3 Return pipe 4 Dilute solution pipe 5 Refrigerant pump 6 Refrigerant pipe 7, 8 (refrigerant vapor) flow path 9 Cooling water pipe 10, 11 Hot water tube 12 Heat transfer tube (Heat transfer tube group)
12a, 12b, 12c Divided heat transfer tube group 13 Steam tube 15 Makeup water heater 16 Makeup water pump 18 Inverter 20 Control valve 22 Gas-liquid separators 22a, 22b, 22c, 22d Connection port 22e Baffle plate 30 Refrigerant branch pipe 32 Control valve 33 Baffle plates 34-1 and 34-2 Refrigerant tube 35 Heat transfer tubes 40 and 41 Control valves 100A and 100B Absorption heat pump 101 Cooling water 102 Heat source hot water 103 Heated fluid (water)
104 Steam (water vapor)
121 First water chamber 121a, 121b Divided water chamber 121a-1, 121a-2, 121b-1, 121b-2 Divided water chamber 122, 122-1a, 122-1b Partition 123 Second water chamber 123a, 123b Divided Water chamber 123a-1, 123a-2, 123b-1, 123b-2 Divided water chamber 124, 124-1a, 124-1b Partition 125, 126 Tube plates 131, 131a, 131b Supply pipe 132a, 132b Orifice 133c Steam passage 133d 133e Water passage A1, A2 Absorber AH High temperature absorber C Condenser CONT Controller E1, E2 Evaporator EH High temperature evaporator EHS Gas-liquid separator G Regenerator L1, L2, L3, L4, L5 Level gauge P1 Pressure Detector X1, X2, X3 Heat exchanger

Claims (4)

An absorber for generating a heated fluid gas by heating the heated fluid liquid with absorbed heat generated by absorbing the refrigerant gas;
The absorber is a heat transfer tube group consisting of a plurality of heat transfer tubes arranged horizontally, and a heat transfer tube group consisting of a plurality of heat transfer tubes that scatter the absorbing liquid on the outside and flow the heated fluid liquid on the inside. ;
A heated fluid chamber for supplying the heated fluid liquid on the heated fluid liquid supply side of the heat transfer tube group;
The heated fluid chamber includes a partition that divides the heat transfer tube group into a first divided heat transfer tube group and a second divided heat transfer tube group that are equal in number in the vertical direction;
A supply port for supplying the heated fluid liquid in parallel to the first and second divided heat transfer tube groups, wherein the divided heat transfer tube groups of the first and second divided heat transfer tube groups are evenly divided. have a supply port for supplying the heating fluid;
Before SL each divided heat transfer tube group are configured multiple paths, respectively;
Absorption heat pump. The number of heat transfer tubes constituting each path of each divided heat transfer tube group configured in the plurality of paths is configured to increase from the lower stage toward the upper stage;
The absorption heat pump according to claim 1. The absorption heat pump according to claim 1 or 2 , wherein the supply port has a distribution mechanism that evenly distributes the fluid to be heated to the divided tube group. A gas-liquid separator that introduces the heated fluid gas generated by the absorber and separates the heated fluid gas and the heated fluid liquid accompanying the heated fluid gas;
The divided heat transfer across the tube bank to form a liquid pool so immersed in the heated fluid, the divided heat transfer tube group of outlet-side the absorber and the gas-liquid separator of the connection port, or the divided Den A heated fluid chamber is formed on the heated fluid outlet side of the heat tube group, and the liquid reservoir is formed with an edge so as to completely cover the accumulated liquid up to the uppermost heat transfer tube group in the vertical direction. The absorption heat pump according to any one of claims 3 to 3.

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