JP2011242014A - Absorption heat pump - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an absorption heat pump capable of recovering a heat amount of a heat source fluid as much as possible.SOLUTION: The absorption heat pump includes: a first evaporator E1 for heating and evaporating a refrigerant by the heat source fluid GH1; a first absorber A1 for absorbing the evaporated refrigerant and heating a medium to be heated with absorption heat; a first regenerator G1 for heating and regenerating absorption liquid ALi whose concentration is lowered in the first absorber A1 by the heat source fluid GH202; a second evaporator E2 for evaporating the refrigerant by the heat source fluid GH102; a second absorber A2 for absorbing the evaporated refrigerant and heating the medium to be heated with the absorption heat; and a second regenerator G2 for heating and regenerating the absorption liquid whose concentration is lowered in the second absorber A2 by the heat source fluid GH5. The first evaporator E1, the second evaporator E2, the second regenerator G2 and the first regenerator G1 are arranged in the order from the upstream side to the downstream side of the heat source fluid GH in a flow path 60 through which the heat source fluid GH is made to flow.

Description

    The present invention relates to an absorption heat pump. In particular, the present invention relates to an absorption heat pump that recovers heat from a heat source gas such as exhaust gas to heat a medium to be heated. Further, the present invention relates to an absorption heat pump that utilizes a temperature difference as large as possible from the inlet temperature with high-temperature water or the like.

  As shown in FIG. 6, the conventional temperature rising type absorption heat pump uses the exhausted warm water WH as a heat source. For example, hot water of 85 ° C. is introduced into an absorption heat pump, and is used up to about 80 ° C. to 75 ° C. with the regenerator GG and the evaporator EE, and high temperature water or steam SS of 120 ° C. or higher is produced with the absorber AA. The steam generated in the regenerator GG is cooled and condensed by the cooling water WC in the condenser CC, and returned to the evaporator EE. On the other hand, the exhaust heat source having a small heat capacity, such as exhaust gas, is suddenly lowered in temperature by heat recovery, and it is difficult to directly recover heat by the temperature rising type absorption heat pump. For this reason, heat is recovered from the exhaust gas into the hot water WH, and the hot water WH is used as a heat source for the heat pump. In this case, the heat exchange from the exhaust gas to the hot water WH reduces the temperature that can be used, and the temperature rise of the heated fluid is reduced. Therefore, studies are also underway to directly introduce the exhaust gas to the temperature rising type absorption heat pump. . In this way, more heat can be recovered than when converted to hot water WH.

JP 2006-207883 A

  However, since the exhaust gas has a small heat capacity, the temperature difference between the entrance and exit of the heat recovery apparatus becomes very large when heat recovery is attempted to the lowest possible temperature. For example, when exhaust gas is supplied to an absorption heat pump at 200 ° C. and used up to 100 ° C. to obtain 180 ° C. steam, the temperature change of the exhaust gas becomes as large as 100 ° C. If a large entrance / exit temperature difference can be used effectively, the amount of recovered heat can be increased. However, because of the large temperature difference between the inlet and outlet, if this is used directly in an absorption heat pump, there is a risk of overconcentration of the absorption liquid or crystals on the high temperature side of the exhaust gas. It was difficult to do. In particular, there has been difficulty in trying to increase the amount of generated steam by recovering heat to as low a temperature as possible.

  In order to solve the above-described problem, the absorption heat pump according to the first aspect of the present invention uses a heat source fluid GH1 to heat and evaporate the refrigerant as shown in FIGS. 1 (a), 3 and 4, for example. One evaporator E1; a first absorber A1 that absorbs the refrigerant evaporated in the first evaporator E1 and heats the medium W1 to be heated by absorption heat; and a refrigerant that is absorbed by the first absorber A1 A first regenerator G1 that heats and regenerates the absorption liquid ALi having a reduced concentration by the heat source fluid GH202; a second evaporator E2 that heats and evaporates the refrigerant by the heat source fluid GH102; and a second evaporator A second absorber A2 that absorbs the refrigerant evaporated in E2 and heats the medium to be heated with absorption heat; and absorbs the refrigerant in the second absorber A2 and lowers the concentration by the heat source fluid GH5. And a second regenerator G2 for regenerating; The generator E1, the second evaporator E2, the second regenerator G2, and the first regenerator G1 are arranged in the flow path 60 through which the heat source fluid GH flows from the upstream side to the downstream side of the heat source fluid GH. Arranged in this order.

  Hereinafter, the heat source fluid (for example, exhaust gas) first supplied to the evaporator E1 is referred to as GH1, the heat source fluid that passes through the evaporator E1 and is supplied to the evaporator E2 is referred to as GH102, and passes through the evaporator E2 to be regenerated. The heat source fluid supplied to the regenerator G2 is referred to as GH5, and the heat source fluid that passes through the regenerator G2 and flows into the regenerator G1 is referred to as GH202. Further, the heat source fluid discharged through the regenerator G1 is referred to as GH4. Further, when it is not necessary to distinguish the heat source fluid (for example, exhaust gas) as the heat source fluid flowing through each part, or when it is handled comprehensively, it is simply referred to as GH.

  If comprised like this aspect, in the second evaporator, the refrigerant evaporates at a temperature lower than that of the first evaporator, and in the second regenerator, the refrigerant is heated at a temperature higher than that of the first regenerator. Played. The absorbents of the first absorber and the second absorber operate at substantially the same temperature. Further, since the second and first regenerators are arranged downstream of the first and second evaporators with respect to the flow of the heat source fluid such as the heat source gas, the heat source fluid is the first and second regenerators. After the temperature has dropped to some extent in the evaporator, it is fed to the second and first regenerators. Therefore, it is possible to suppress the excessive concentration of the absorbing solution and the risk of crystallization due to the high-temperature heat source fluid. By making the heat source fluid input sequence as described above, an evaporator that evaporates on the high temperature side and a regenerator that regenerates on the low temperature side are combined, and an evaporator that evaporates on the low temperature side and a regenerator that regenerates on the high temperature side are combined. In combination, the heat source fluid can be utilized as low as possible.

  Furthermore, you may provide the 1st condenser and 2nd condenser which condense the refrigerant gas which evaporated with the 1st regenerator and the 2nd regenerator, respectively. The first condenser and the second condenser may be provided separately, but may be a common condenser. If it is common, the entire configuration can be compactly summarized.

  The absorption heat pump typically pumps the heat held by the heat source fluid GH from the first evaporator E1 to the first absorber A1, and from the second evaporator E2 to the second absorber A2, thereby heating the medium to be heated. It is a heat pump which heats.

  The absorption heat pump according to the second aspect of the present invention is the absorption heat pump according to the first aspect or the second aspect. For example, as shown in FIG. 3, the heat source fluid GH is a heat source gas, and the first evaporation The evaporator E1 and the second evaporator E2 are the evaporator upper tube plates 152 and 252, the evaporator lower tube plates 153 and 253, the evaporator upper tube plates 152 and 252 and the evaporator lower tube plates 153 and 253, respectively. A plurality of vertical heat transfer tubes 151 and 251 through which the liquid refrigerant flows inside; the first regenerator G1 and the second regenerator G2 A plurality of pipes 172, 272, regenerator lower tube plates 173, 273, and a plurality of absorbent liquids ALi flow inside the regenerator upper tube plates 172, 272 and the regenerator lower tube plates 173, 273. Vertical heat transfer tubes 171 and 271 The heat source gas GH flows outside the plurality of vertical heat transfer tubes 151, 251, 171, 271 and intersects with the vertical heat transfer tubes 151, 251, 171, 271; 151, 251, 271 and 171 are the first evaporator E1, the second evaporator E2, the second regenerator G2, and the first regenerator G1, respectively, and the first evaporator tube group 150. A second evaporator tube group 250, a second regenerator tube group 270, and a first regenerator tube group 170, the first evaporator tube group 150, the second evaporator The tube group 250, the second regenerator tube group 270, and the first regenerator tube group 170 are linearly arranged with respect to the flow of the heat source gas GH.

  If comprised like this aspect, it is comprised so that the heat source gas GH may flow the outer side of a several vertical heat exchanger tube, and a vertical heat exchanger tube may cross | intersect. And a second evaporator, a second regenerator, and a first regenerator, respectively, a first evaporator tube group, a second evaporator tube group, and a second regenerator tube group The first regenerator tube group, the first evaporator tube group, the second evaporator tube group, the second regenerator tube group and the first regenerator tube group are heat sources. Since the gas GH is arranged linearly with respect to the flow of the gas GH, when using a heat source gas such as an exhaust gas having a large volume flow rate as a heat source for the evaporator and the regenerator, the pressure loss due to the flow resistance can be kept low. . Therefore, the power for making this flow can be suppressed small, and the energy saving effect can be enhanced.

The absorption heat pump according to the third aspect of the present invention is the absorption heat pump according to the second aspect, for example, as shown in FIG. 5, in the flow path of the heat source gas GH, on the downstream side of the second evaporator E2. A bypass passage 91 that bypasses the second regenerator G2 from the end and flows the heat source gas GH downstream of the second regenerator G2, and a flow that restricts the flow of the heat source gas GH in the bypass passage 91 Limiting means 92 is provided.
Here, “restriction” may be “restriction” that does not include “blocking”, but is typically a concept including “blocking”.

  With this configuration, it is possible to limit the amount of heating in the second regenerator where absorption liquid is excessively concentrated or crystals are likely to occur. Therefore, excessive concentration or crystallization of the absorbing solution can be suppressed.

  The absorption heat pump according to the fourth aspect of the present invention is the absorption heat pump according to any one of the first to third aspects. For example, as shown in FIG. The vessel A1 and the second absorber A2 are configured to heat the water W1 as a medium to be heated and generate water vapor S having a pressure higher than atmospheric pressure, and separate the generated water vapor S from the accompanying water. A gas-liquid separator 11 is provided.

  With this configuration, the first absorber and the second absorber are configured to heat water as a medium to be heated and generate water vapor having a pressure higher than atmospheric pressure. Since the gas-liquid separator that separates the water from the water is used, it is possible to generate water vapor by pumping heat from the heat source fluid that is relatively low temperature as low as possible, and to obtain water vapor by separating the accompanying water. it can.

  The absorption heat pump according to the fifth aspect of the present invention is the absorption heat pump according to any one of the first to fourth aspects. For example, as shown in FIG. In the flow path 60, the heat exchanger B which generate | occur | produces water vapor | steam directly with the heat | fever of the heat source fluid GH is provided in the upstream of the 1st evaporator E1.

  If comprised in this way, the input path | route of the heat source fluid GH becomes the order of the heat exchanger B, the 1st evaporator E1, the 2nd evaporator E2, the 2nd regenerator G2, and the 1st regenerator G1. . Since the heat exchanger B that directly generates water vapor by the heat of the heat source fluid GH is provided upstream of the first evaporator E1 in the flow path 60 of the heat source fluid GH, the supply temperature of the heat source fluid GH generates the steam S. When the temperature is higher than the temperature that can be directly generated, the makeup water W1 is directly heated by the heat source fluid GH, and steam can be directly generated.

  ADVANTAGE OF THE INVENTION According to this invention, it becomes possible to provide the absorption heat pump which can collect | recover as much calorie | heat amount of a heat source fluid as possible.

It is a flow sheet which shows the composition of the absorption heat pump concerning a first embodiment of the present invention. (A) is the whole flow sheet, (b) is the partial flow sheet which extracted and showed the 1st evaporator E1 and the heat exchanger B in the modification of 1st Embodiment. It is a Duhring diagram which shows the state of the absorption liquid on the flow sheet of Fig.1 (a). It is the perspective view which looked at the evaporator and regenerator which are used with the absorption heat pump which concerns on 1st embodiment of this invention from the diagonally upward direction, notching a part of upper header. It is the top view which looked at the evaporator and regenerator which are used with the absorption heat pump which concerns on 1st embodiment of this invention from the upper direction of the axial direction of a vertical heat exchanger tube, removing the header. It is the top view which looked at the evaporator and regenerator which are used with the absorption heat pump which concerns on 2nd embodiment of this invention from the upper direction of the axial direction of a vertical heat exchanger tube, removing a header. It is a flow sheet which shows the composition of the conventional absorption heat pump.

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

  With reference to the flow sheet of FIG. 1, the structure of the absorption heat pump which concerns on 1st embodiment of this invention is demonstrated. (A) is a flow sheet showing the entire absorption heat pump 100, (b) is a modification of the first embodiment, and heat for directly heating makeup water with a heat source fluid upstream of the first evaporator E1. The case where the exchanger B is provided is shown. The absorption heat pump 100 includes a first absorption heat pump unit 100-1 and a second absorption heat pump unit 100-2. The first absorption heat pump unit 100-1 absorbs the refrigerant vapor CS (the refrigerant is, for example, water) by the absorption liquid ALi (for example, lithium bromide aqueous solution), and the refrigerant vapor CS from the absorption liquid ALi. A regenerator G1 that evaporates and regenerates the absorbing liquid ALi, an evaporator E1 that generates the refrigerant vapor CS from the refrigerant liquid CL, and a condenser C that condenses the refrigerant vapor CS into the refrigerant liquid CL are provided. The pressure of the evaporator E1 and the pressure of the absorber A1 are practically equal, and the pressure of the regenerator G1 and the pressure of the condenser C are practically equal.

  The second absorption heat pump unit 100-2 includes an absorber A2, a regenerator G2, and an evaporator E2 just like the first absorption heat pump unit 100-1, and the condenser is the first absorption heat pump. The condenser C common to the unit 100-1 is used. Each component described above basically has the same function in the first and second absorption heat pump units. In addition, although a condenser may be separately provided in the 1st absorption heat pump part 100-1 and the 2nd absorption heat pump part 100-2, if it makes it common, the simplification of an apparatus can be achieved.

  Hereinafter, each component will be described in detail for the first absorption heat pump unit 100-1. A description of the components corresponding to the first and second absorption heat pump units is omitted as appropriate. As a general rule, the sign of each component device is distinguished as 100 series in the first absorption heat pump unit 100-1 and 200 series in the second absorption heat pump unit 100-2. The absorbers A1 and A2, the regenerators G1 and G2, and the evaporators E1 and E2 are distinguished by simply adding 1 or 2 after the alphabet.

  The absorber A1 includes (1) an absorbent liquid spray 122 for transferring (supplying) the absorbent liquid ALi, which is a concentrated solution, and spraying the transferred absorbent liquid ALi inside the absorber A1, and (2) a makeup water W1. A heated pipe 123 is provided that heats the replenished water W1 that has been transferred by the absorbing liquid ALi that has been transferred and has absorbed the refrigerant vapor CS. The bottom of the absorber A1 is an absorption liquid reservoir sufficient to accumulate the absorption liquid ALi.

  The evaporator E1 includes a vertical heat transfer pipe 151 that causes the refrigerant liquid CL transferred from the condenser C by the refrigerant liquid transfer pipe 5 to flow inside and is heated and evaporated by the exhaust gas GH1 as a heat source gas flowing outside. Moreover, the liquid level sensor L101 which is installed in the upper header 155 of the evaporator E1 and detects the liquid level of the refrigerant liquid CL in the evaporator E1 is provided. The liquid level sensor L101 maintains the liquid level of the refrigerant in the evaporator E1 constant by adjusting the refrigerant supply valve V103 via the control device 21 (common to the first and second heat pump units). . Note that the refrigerant pump P4 (common to the first and second heat pump units) may be driven by an inverter motor without adjusting the refrigerant supply valve V103 to adjust the rotation speed of the refrigerant pump. In the figure, the refrigerant pump is common to the first and second absorption heat pumps. However, when the liquid level of the evaporators E1 and E2 is maintained separately by adjusting the rotation speed of the refrigerant pump, the refrigerant pump is also provided separately. Good. This is because the top and bottom of the liquid level can occur independently in the evaporator E1 and the evaporator E2. In the absorption heat pump 100, the refrigerant vapor CS evaporated in the evaporator E1 is sent to the absorber A1 through the refrigerant vapor transfer pipe 116. The structure of the evaporator E1 will be described in detail with reference to FIGS. Here, the exhaust gas is typically a gas having a temperature of about 200 ° C. or less after a high temperature portion is used in various processes in a factory. The exhaust gas from the boiler may be a gas before using the high temperature portion and before discharging from the chimney.

  The regenerator G1 flows the absorption liquid ALi transferred from the absorber A1 through the absorption liquid transfer pipe 103, heats it with the exhaust gas GH202 as a heat source gas flowing outside, generates refrigerant vapor, and concentrates it. A vertical heat transfer tube 171 is provided. Here, the exhaust gas GH202 is exhaust gas that passes through the evaporators E1, E2 and the regenerator G2 and uses the amount of heat, and has a certain temperature drop. In addition, the absorbing liquid ALi is an absorbing liquid whose concentration is decreased by absorbing the refrigerant in the absorber A1, that is, a dilute solution. The liquid level sensor L102 is provided in the upper header 175 of the regenerator G1 and detects the liquid level of the absorbing liquid ALi in the regenerator G1. The liquid level sensor L102 maintains the liquid level of the absorbing liquid in the regenerator G1 by adjusting the solution pump P101 via the control device 21 (note that a control valve is used instead of adjusting the solution pump P101). May be provided). In the first absorption heat pump unit 100-1, the absorption liquid ALi concentrated in the regenerator G1 is sent to the absorber A1 through the absorption liquid transfer pipe 102. The refrigerant vapor CS generated in the regenerator G1 is sent to the condenser C through the refrigerant vapor transfer pipe 117 and the refrigerant vapor transfer pipe 17. Here, the refrigerant vapor transfer pipe 17 is a pipe that transfers the refrigerant vapor CS to the condenser C after joining the refrigerant vapor transfer pipe 217 from the regenerator G2.

  Furthermore, with reference to Fig.1 (a), the structural apparatus of the 2nd absorption heat pump part 100-2 is demonstrated. As described above, descriptions of components that are common to or correspond to the first and second absorption heat pump units are omitted as appropriate.

  The absorber A2 includes an absorption liquid spray 222 that sprays the absorption liquid ALi that is a concentrated solution inside the absorber A2, and a heated pipe 223 that heats the makeup water W1. The bottom of the absorber A2 is an absorption liquid reservoir sufficient to accumulate the absorption liquid ALi.

  The evaporator E2 is disposed downstream of the evaporator E1 in the exhaust gas flow channel 60. The exhaust gas channel 60 is an exhaust gas channel in which an evaporator E1, an evaporator E2, a regenerator G2, and a regenerator G1 are arranged in this order. The arrangement of the exhaust gas flow channel 60 and each device will be described later in detail with reference to FIG. The evaporator E2 includes a vertical heat transfer tube 251 that causes the refrigerant liquid CL to flow inside and is heated and evaporated by the exhaust gas GH102 flowing outside. Here, the exhaust gas GH102 is exhaust gas in which the exhaust gas G1 is used in the evaporator E1 and the temperature is lowered to some extent. The liquid level sensor L201 is installed in the upper header 255 of the evaporator E2 and detects the liquid level of the refrigerant liquid CL in the evaporator E2. The liquid level sensor L201 maintains the liquid level of the refrigerant in the evaporator E2 by adjusting the refrigerant supply valve V203 via the control device 21. As described in the evaporator E1, the refrigerant pump may be adjusted by driving the refrigerant pump P4 as an inverter motor without providing the refrigerant supply valve V203. In this case, the refrigerant pump is preferably provided separately from the evaporator E1. In the absorption heat pump 100, the refrigerant vapor CS evaporated in the evaporator E2 is sent to the absorber A2 through the refrigerant vapor transfer pipe 216. The structure of the evaporator E2 will be described in detail with reference to FIGS. 3 to 5 together with the evaporator E1.

  The regenerator G2 is disposed in the exhaust gas flow channel 60 on the downstream side of the evaporator E2 and on the upstream side of the regenerator G1. The regenerator G2 flows the absorption liquid ALi transferred from the absorber A2 through the absorption liquid transfer pipe 203, heats it with the exhaust gas GH5 as a heat source gas flowing outside, generates refrigerant vapor, and concentrates it. A vertical heat transfer tube 271 is provided. Here, the exhaust gas GH5 is exhaust gas that passes through the evaporator E1 and the evaporator E2 and uses the amount of heat to lower the temperature to some extent. Moreover, this absorption liquid ALi is an absorption liquid, ie, a dilute solution, whose concentration has been reduced by absorbing the refrigerant in the absorber A2. The liquid level sensor L202 is provided in the upper header 275 of the regenerator G2 and detects the liquid level of the absorbing liquid ALi in the regenerator G2. The liquid level sensor L202 maintains the liquid level of the absorbing liquid in the regenerator G2 by adjusting the solution pump P201 via the control device 21 (note that a control valve is used instead of adjusting the solution pump P201). May be provided). In the second absorption heat pump unit 100-2, the refrigerant liquid CL concentrated in the regenerator G2 is sent to the absorber A2 through the absorption liquid transfer pipe 202. The refrigerant vapor CS generated in the regenerator G2 is sent to the condenser C through the refrigerant vapor transfer pipe 217 and the refrigerant vapor transfer pipe 17.

  The condenser C includes a cooling pipe 30 that cools the refrigerant vapor CS that is supplied with the cooling water WC and is sent from the regenerator G1 and the regenerator G2 to the condenser C. The temperature of the cooling water WC is, for example, 32 ° C. at the inlet of the cooling pipe 30 and 37 ° C. at the outlet.

  The absorption heat pump 100 includes (1) a gas-liquid separator 11, (2) a makeup water transfer pipe 7 that is connected to the gas-liquid separator 11 and transports makeup water W1 to the gas-liquid separator 11, and (3) gas Makeup water transfer pipe 6 for transferring makeup water W1 from the liquid separator 11 to the heated pipes 123, 223 of the absorbers A1, A2, and (4) makeup water from the heated pipes 123, 223 to the gas-liquid separator 11. Supply water transfer lines 110 and 210 for transferring W1 back and (5) steam S (for example, 180 ° C.) generated in the gas-liquid separator 11 is supplied to the steam header. And a steam supply line 8 to be provided.

  The absorption heat pump 100 further (6) connects the regenerator G1 and the absorber A1, and transfers the absorption liquid ALi, which is a concentrated solution regenerated by the regenerator G1, to the absorption liquid spray 122 of the absorber A1. Absorption liquid transfer pipe for connecting the line 102 and (6b) the regenerator G2 and the absorber A2 and transferring the absorption liquid ALi, which is a concentrated solution regenerated by the regenerator G2, to the absorption liquid spray 222 of the absorber A2. 202 and (7) an absorbent liquid transfer line 103 that connects the absorber A1 and the regenerator G1 and transfers the absorbent ALi that is a dilute solution accumulated in the absorber A1 to the regenerator lower header 176 of the regenerator G1. And (7b) an absorbent liquid transfer line 203 that connects the absorber A2 and the regenerator G2, and transfers the absorbent ALi that is a dilute solution accumulated in the absorber A2 to the regenerator lower header 276 of the regenerator G2. (8) with condenser C Connecting a Hatsuki E1 and evaporator E2, and a refrigerant liquid flow pipe 5 for transferring the refrigerant liquid CL condensed in the condenser C into the evaporator E1 and the evaporator E2.

  The absorption heat pump 100 further includes (9) an absorption liquid ALi that is a concentrated solution transferred to the heated side through the absorption liquid transfer pipe 102 and a regenerator lower header 176 through the absorption liquid transfer pipe 103. A concentrated solution that is transferred to the heated side through the solution (absorption liquid) heat exchanger X101 and (9b) the absorption liquid transfer pipe 202 that exchanges heat with the absorption liquid ALi that is a dilute solution to be transferred. A solution (absorbing liquid) heat exchanger X201 is provided that exchanges heat between a certain absorbing liquid ALi and an absorbing liquid ALi that is a dilute solution transferred to the regenerator lower header 276 through the absorbing liquid transfer pipe 203. .

  The absorption heat pump 100 further includes a heat exchanger X2 in which the exhaust heat source GH3 flows on the heating side, the makeup water W1 is transferred to the heated side through the makeup water transfer pipe 7, and heat exchange is performed. Although the heat exchanger X2 is shown as an independent heat exchanger in the figure, the heat transfer section of the heat exchanger X2 is provided in the exhaust gas flow between the evaporator E1 inlet or the evaporator E2 and the regenerator G2. Is preferred.

  A solution pump P101 and a solution pump P202 are installed in the absorption liquid transfer line 102 and the absorption liquid transfer line 202, respectively. The solution pump P101 and the solution pump P202 are absorption liquids regenerated by the regenerator G1 and the regenerator G2, respectively. ALi is transferred to absorber A1 and absorber A2, respectively. The solution pump P101 is installed on the upstream side of the solution heat exchanger X101, and the solution pump P201 is installed on the upstream side of the solution heat exchanger X201. The refrigerant liquid transfer pipe 5 is provided with a refrigerant pump P4 as a refrigerant boosting means, and the refrigerant pump P4 transfers the refrigerant liquid CL condensed by the condenser C to the evaporator E1 and the evaporator E2.

  A water supply pump P <b> 12 is installed in the makeup water transfer pipe 7, and the water supply pump P <b> 12 transports makeup water W <b> 1 to the gas-liquid separator 11. A check valve 37 is installed immediately downstream of the water supply pump P12 in the makeup water transfer pipe 7 to prevent the makeup water W1 from flowing backward. The makeup water transfer pipe 6 is provided with a feed water pump P13. The feed water pump P13 transports makeup water W1 from the gas-liquid separator 11 to the heated pipes 123 and 223, and further supplies makeup water transfer pipes 110 and 210. It passes through the heated pipes 123 and 223 and returns to the gas-liquid separator 11 to circulate the makeup water W1.

  Refrigerant supply valves V103 and V203 for adjusting the flow rate of the refrigerant liquid CL transferred to the evaporator lower headers 156 and 256 are installed on the downstream side of the refrigerant pump P4 in the refrigerant liquid transfer pipe 5.

  The gas-liquid separator 11 is provided with a pressure sensor P for detecting the pressure, and a liquid level sensor L3 for detecting the liquid level of the makeup water W1 accumulated in the lower part. The steam supply pipe 8 is provided with a steam valve V1 that adjusts the pressure of the steam S to be supplied. As shown in the figure, a check valve 38 for preventing the backflow of steam from a steam header (not shown) may be installed in the steam supply line 8. When the check valve 38 is installed, the backflow of steam from the steam header can be surely prevented regardless of the operation of the steam valve V1.

  The supply temperature of the exhaust gas GH1 as the heat source gas is, for example, 200 ° C. The exhaust gas GH1 supplied to the evaporator E1 is deprived of heat by the evaporator E1 and becomes exhaust gas GH102 and flows into the evaporator E2, and is deprived of heat by the evaporator E2 and becomes exhaust gas GH5 having a temperature of about 150 ° C. It flows into the regenerator G2, where heat is taken away to become exhaust gas GH202 and flows into the regenerator G1, where heat is taken away by the regenerator G1 and exhausted at about 100 ° C. as exhaust gas GH4.

  As already explained, the exhaust gas supplied to the evaporator E1 is supplied to GH1, the exhaust gas supplied to the evaporator E2 through the evaporator E1 is supplied to GH102, and the exhaust gas supplied to the regenerator G2 through the evaporator E2. The exhaust gas flowing through the regenerator G2 through the regenerator G2 is referred to as GH202, and the exhaust gas discharged through the regenerator G1 is referred to as GH4. In addition, when it is not necessary to distinguish exhaust gas as gas flowing through each device, or when it is comprehensively handled, it is simply referred to as GH.

  The preheating of the makeup water W1 is preferably performed with a high-temperature gas from the supply side of the heat source gas such as exhaust gas to the gas GH5 in the middle of the evaporator E2 and the regenerator G2. Alternatively, although not shown, it may be performed by a heat exchanger that is heated by the inlet absorbing liquid supplied to the regenerator G2, or by a heat exchanger that is heated by the refrigerant vapor generated in the evaporator E1 or the evaporator E2. May be.

  The absorption heat pump 100 includes a control device 21. A liquid level signal (not shown) representing the liquid level from the liquid level sensor L101 is sent to the control device 21, and a signal is sent from the control device 21 to the refrigerant supply valve V103 which is a control valve for controlling the flow rate of the refrigerant liquid CL. Send. In this way, the opening of the refrigerant supply valve V103 is adjusted so that the liquid level of the evaporator E1 becomes constant (however, in the figure, a simplified control signal is sent directly from the liquid level sensor L101 to the refrigerant supply valve V103. Shown to be sent). The relationship between the liquid level sensor L201 and the refrigerant supply valve V203 is the same.

  A liquid level signal (not shown) representing the liquid level from the liquid level sensor L102 is sent to the control device 21 to control the flow rate of the absorbing liquid ALi so as to keep the liquid level at a constant level. A control signal (not shown) is sent to the inverter motor INV that drives the solution pump P101, and the rotational speed of the inverter motor INV is adjusted to control the liquid level of the regenerator G1 to be constant (in the drawing). For the sake of simplicity, it is shown that a signal is sent directly from the liquid level sensor L102 to the inverter motor INV). The relationship between the liquid level sensor L202 and the solution pump P201 is the same.

  A liquid level signal (not shown) representing the liquid level from the liquid level sensor L3 of the gas-liquid separator 11 is sent to the control device 21 so that the liquid level is maintained at a substantially constant level. The water supply pump P12 is turned on / off (in the drawing, for simplicity, a signal is directly sent from the liquid level sensor L3 to the water supply pump P12). A control signal (not shown) for controlling the flow rate of the makeup water W1 is sent from the control device 21 to the feed water pump P12 so as to keep the liquid level at a constant level (actually an inverter motor not shown as described above). The rotation speed of the water supply pump P12 may be adjusted so that the liquid level of the gas-liquid separator 11 becomes constant.

  A pressure signal (a broken line in the figure) from the pressure sensor P is sent to the control device 21, and the supply amount of the steam S is adjusted from the control device 21 so that the pressure of the gas-liquid separator 11 becomes a predetermined value P1. A control signal to be controlled (broken line in the figure) is sent to the steam valve V1, and the opening degree of the steam valve V1 is adjusted so that the pressure of the gas-liquid separator 11 becomes a predetermined value P1. For example, the predetermined value P1 may be set slightly higher (about 0.05 MPa) than the steam header pressure. Although the exhaust gas GH1 and the exhaust gas GH3 are shown to be supplied in parallel, they may be supplied in series, in part in parallel, or in part in series.

  Next, the operation of the first embodiment will be described with reference to FIGS. FIG. 2 is a Duhring diagram showing the states of the absorbing liquid and the refrigerant. The vertical axis represents the refrigerant temperature, and the horizontal axis represents the solution (absorbing liquid) temperature.

  First, the first absorption heat pump unit 100-1 will be described. Absorbing liquid ALi (a state is a position of B12 in FIG. 2) which is a dilute solution that has left the absorber A1 is transferred by the absorbing liquid transfer pipe 103 and passes through the solution heat exchanger X101. The absorption liquid ALi passes through the heat exchanger X101 and is cooled by the absorption liquid ALi which is a concentrated solution transferred from the regenerator G1 to the absorber A1 through the absorption liquid transfer pipe 102 (absorption after cooling). The state of the liquid ALi is the position of B18 in FIG. The absorbing liquid ALi cooled by the solution heat exchanger X101 is transferred to the regenerator lower header 176.

  The absorption liquid ALi is heated by the exhaust gas GH202 while flowing through the vertical pipe 171 from the regenerator lower header 176 of the regenerator G1 (the state of the absorption liquid ALi is the position B15 in FIG. 2), and is absorbed by the absorption liquid ALi. The refrigerant that has been evaporated evaporates as refrigerant vapor CS. In this way, the concentrated liquid ALi that is concentrated and regenerated flows out from the absorbent outlet 102a provided in the regenerator upper header 175 portion. A square hole represented by a solid line in the upper header 175 of the regenerator G1 shown in FIG. 1 is the outlet 102a. Moreover, the broken line connected to it has shown the exit header.

  Absorbing liquid ALi that has become a concentrated solution (the state is the position of B14 in FIG. 2) is transferred to absorbing liquid spray 122 of absorber A1 through absorbing liquid transfer pipe 102. While passing through the absorption liquid transfer line 102, the pressure is increased by the solution pump P101 and then heated by the absorption liquid ALi, which is a dilute solution transferred from the absorber A1 to the regenerator G1 in the solution heat exchanger X101 (absorption liquid transfer). The state of the absorption liquid ALi passing through the pipe line 102 is transferred to the absorption liquid spray 122 of the absorber A1 in the position B17 in FIG.

  In the absorber A1, the absorption liquid ALi (the state of the absorption liquid ALi is the position B16 in FIG. 2), which is a concentrated solution sprayed from the absorption liquid spray 122 into the absorber A1, is a refrigerant evaporated in the evaporator E1. The replenishing water W1 as a heated medium passing through the heated pipe 123 is absorbed by the absorption heat, and is accumulated at the bottom of the absorber A1 (the state of the absorbing liquid ALi is the position of B12 in FIG. 2). ).

  As described above, the solution pump P101 transfers the absorption liquid ALi at a flow rate that makes the liquid level of the absorption liquid ALi in the regenerator G1 constant, from the regenerator G1 to the absorber A1. The transfer amount is controlled by the control device 21. By keeping the liquid level of the regenerator G1 constant, a liquid seal between the absorber A1 and the regenerator G1 having a large refrigerant vapor pressure difference is secured. The absorbing liquid in the system, excluding the absorbing liquid staying in the regenerator G1, is mainly accumulated at the bottom of the absorber A1. Therefore, the bottom of the absorber A1 is configured to have a capacity sufficient for its accumulation. A check valve 139 is provided on the outlet side of the pump P101 in the absorption liquid transfer line 102. During operation of the heat pump 100, the absorber A1 has a higher pressure than the regenerator G1. Therefore, when the heat pump 100 is stopped, that is, when the pump P101 is stopped, the absorbing liquid flows from the absorber A1 into the regenerator G1 if it is silent. The reverse rotation of the pump P101 is prevented by the check valve 139. When the heat pump 100 is stopped, the absorption liquid ALi accumulated in the absorbers A1 and A2 flows through the absorption liquid transfer pipes 103 and 203, respectively, and accumulates in the regenerators G1 and G2, respectively. Therefore, each of the regenerator upper headers 175 and 275 has a capacity sufficient to accommodate the absorbing liquid in the system. The absorbing liquid ALi accumulated in the regenerator upper headers 175 and 275 at the time of stoppage is sent to the absorbers A1 and A2 by liquid level control when the heat pump 100 is started. Or, before introducing the exhaust gas GH, it may be sent to the absorbers A1 and A2 in advance.

  The refrigerant vapor CS evaporated in the regenerator G1 is sent to the condenser C through the refrigerant vapor transfer pipes 117 and 17. The refrigerant vapor CS sent to the condenser C is cooled and condensed by the cooling water WC passing through the cooling pipe 30 in the condenser C to become a refrigerant liquid CL (the state is the position of D1 in FIG. 2). The refrigerant liquid CL of the condenser C passes through the refrigerant liquid transfer pipe 5, is pressurized by the refrigerant pump P4, is controlled in flow rate by the refrigerant supply valve V103, and is sent to the evaporator E1.

  The refrigerant liquid CL sent to the evaporator E1 is heated and evaporated by the exhaust gas GH1 while flowing from the evaporator lower header 156 to the inside of the vertical heat transfer pipe 151 (the state of the refrigerant is a position D2 in FIG. 2). . The evaporated refrigerant vapor CS is sent to the absorber A1 through the refrigerant vapor transfer pipe 116, and is absorbed by the absorption liquid ALi by the absorber A1.

  The opening degree of the refrigerant supply valve V103 is adjusted by the control device 21, and the amount of the refrigerant liquid CL transferred from the condenser C to the evaporator E1 is adjusted. That is, the amount of the refrigerant liquid CL to be transferred is adjusted so as to make the liquid level of the refrigerant liquid CL accumulated in the evaporator E1 constant. Such control is performed to replenish the evaporated amount of the refrigerant liquid and to prevent the refrigerant pump P4 from sucking gas. The refrigerant liquid in the entire system, excluding the refrigerant liquid staying in the evaporator E1 and the evaporator E2, accumulates at the bottom of the condenser C. Therefore, the bottom of the condenser C is configured to have a capacity sufficient for its accumulation. When the heat pump 100 is stopped, the refrigerant liquid CL may flow backward from the higher pressure evaporators E1 and E2 through the refrigerant liquid transfer pipe 5 to the condenser C having a lower pressure than the evaporators E1 and E2. In order to avoid such reverse rotation of the refrigerant pump P4 immediately after the stop, a check valve 40 may be provided on the outlet side of the refrigerant pump P4. Instead, the control device 21 may be configured such that the refrigerant supply valves V103 and V203 (open when the heat pump is stopped to prevent backflow if left to liquid level control) are fully closed when the heat pump is stopped.

  The operation of the second absorption heat pump unit 100-2 is also the same as that of the first absorption heat pump unit 100-1. What is necessary is just to replace the 100s in the code of each device with the 200s. Here, the description will focus on the different parts. The state of the absorbing liquid ALi, which is a dilute solution exiting the absorber A2, is the position B22 in FIG. The state of the absorbing liquid ALi after being cooled by the solution heat exchanger X201 is the position B28 in FIG.

  This absorption liquid ALi is heated by the exhaust gas GH5 while flowing in the vertical pipe 271 from the regenerator lower header 276 of the regenerator G2 (the state of the absorption liquid ALi is the position B25 in FIG. 2), and becomes the absorption liquid ALi. The absorbed refrigerant evaporates as refrigerant vapor CS. The temperature of the exhaust gas GH5 is higher than the temperature of the exhaust gas G202 used in the regenerator G1. In this way, the concentrated liquid ALi that is concentrated and regenerated flows out from the absorbent outlet 202a provided in the regenerator upper header 275 part.

  Absorbing liquid ALi that has become a concentrated solution (the state is the position of B24 in FIG. 2) is transferred to absorbing liquid spray 222 of absorber A2. During this time, the absorbing liquid ALi, which is a dilute solution transferred from the absorber A2 to the regenerator G2, is heated, and the state of the absorbing liquid ALi is at a position B27 in FIG.

  Absorbing liquid ALi that is a concentrated solution dispersed in absorber A2 (the state of absorbing liquid ALi is the position of B26 in FIG. 2) absorbs refrigerant vapor CS evaporated in evaporator E2, and heats pipe 223. The replenishing water W1 serving as a medium to be heated passing through is heated with absorption heat and accumulated at the bottom of the absorber A2 (the state of the absorbing liquid ALi is the position B22 in FIG. 2).

  Since the actions of the solution pump P201, the control device 21, and the check valve 239 are the same as those of the first absorption heat pump unit 100-1, description thereof will be omitted.

  The refrigerant vapor CS evaporated in the regenerator G2 merges with the refrigerant vapor CS evaporated in the regenerator 1, and is sent to the condenser C. The refrigerant vapor CS is cooled by the condenser C and condensed to become a refrigerant liquid CL. In the present embodiment, since the condenser C is common to the first absorption heat pump unit 100-1, the state on the Duering diagram of FIG. 2 is D1 described in the first absorption heat pump unit 100-1. The position is the same. (If the condensers are not common, they will not be in the same position, but if the cooling water WC under the same conditions is used, they will be in the same position as D1.) The refrigerant liquid CL in the condenser C is a refrigerant. The flow rate is controlled by the supply valve V203, and it is sent to the evaporator E2.

  The refrigerant liquid CL sent to the evaporator E2 is heated and evaporated by the exhaust gas GH102 while flowing from the evaporator lower header 256 to the inside of the vertical heat transfer pipe 251 (the state of the refrigerant is a position D3 in FIG. 2). . The evaporated refrigerant vapor CS is sent to the absorber A2, and is absorbed by the absorption liquid ALi by the absorber A2. As described above, since the evaporator E2 is disposed on the downstream side of the evaporator E1 in the exhaust gas flow path 60, the refrigerant evaporation temperature of the evaporator E2 is lower than that of the evaporator E1.

  Since the operation of the refrigerant supply valve V203 and the control device 21 is the same as that of the first absorption heat pump unit 100-1, description thereof will be omitted.

  As described above, in the present embodiment, two absorption cycles (or three or more) may be provided. These two cycles correspond to the first absorption heat pump unit 100-1 and the second absorption heat pump unit 100-2. The first absorption heat pump unit 100-1 includes an absorber A1, an evaporator E1, a regenerator G1, and a condenser C1, and the second absorption heat pump unit 100-2 includes an absorber A2 and an evaporator E2. , A regenerator G2 and a condenser C2 (common to the condenser C1 in the first embodiment), and is connected to one exhaust gas flow channel 60 from the upstream side of the exhaust gas flow, that is, from the high temperature side. The components, the evaporator E1, the evaporator E2, the regenerator G2, and the regenerator G1 are arranged in this order.

  In the case of including the third or more, that is, up to the nth (n ≧ 3) absorption heat pump unit 100-n, from the upstream side of the flow of the exhaust gas GH, the evaporator E1, the evaporator E2, ... the evaporator En, The regenerator Gn... Is arranged in the order of the regenerator G2 and the regenerator G1.

  As shown in FIG.1 (b), you may provide the heat exchanger B which produces | generates a vapor | steam directly as a modification of this Embodiment. This is useful when the exhaust gas GH is an exhaust gas GH0 at a temperature higher than the temperature at which steam can be directly generated on the inlet side. In the heat exchanger B, the makeup water W1 is directly heated by the exhaust gas GH0 to directly generate steam. In this case, as shown in the figure, the exhaust gas introduction path is set in the order of B, E1, E2, G2, and G1.

  Thus, the absorption heat pump 100 of the present embodiment includes the first absorption heat pump unit 100-1 in which the evaporator E1 having a high evaporation temperature and the regenerator G1 having a low regeneration temperature are combined, and the evaporation temperature (from the evaporator E1). A) a second absorption heat pump unit 100-2 that combines a low evaporator E2 and a regenerator G2 having a higher regeneration temperature (than that of the regenerator G1), and both absorption heat pump units have a condenser C having a common condensation temperature. Prepare. In other words, an evaporator that generates high-temperature refrigerant vapor using the exhaust gas on the high temperature side, and the absorption liquid is regenerated using the exhaust gas on the low-temperature side downstream of the exhaust gas flow (the concentration is not high because the boiling point is not so high). Combine with a low) regenerator. This is the first absorption heat pump unit 100-1. Therefore, a cycle on the low concentration side on the Dueling diagram shown in FIG. 2 is possible, and 180 ° C. water vapor can be obtained from 200 ° C. exhaust gas.

  Similarly, an evaporator that generates a relatively low-temperature refrigerant vapor using low-temperature exhaust gas whose temperature has dropped to some extent, and a relatively high temperature upstream of the exhaust gas flow (exhaust gas used in the first evaporator E1). Is combined with a regenerator that regenerates the absorbing solution (having a relatively high boiling point and a relatively high concentration) using the exhaust gas on the side lower than the temperature of the first regenerator G1. This is the second absorption heat pump unit 100-2. Therefore, a cycle on the high concentration side on the Duhring diagram shown in FIG. 2 is possible, and 180 ° C. water vapor can be obtained from 200 ° C. exhaust gas, similarly to the first absorption heat pump unit 100-1.

  The makeup water W <b> 1 supplied to the makeup water transfer pipe 7 is pressurized by the feed water pump P <b> 12 and transferred to the gas-liquid separator 11. The makeup water W1 exiting the feed water pump P12 is heated by the exhaust gas GH3 in the heat exchanger X2 and transferred to the gas-liquid separator 11.

  The flow rate of the make-up water W1 supplied to the gas-liquid separator 11 is adjusted so that the level of the make-up water W1 accumulated in the gas-liquid separator 11 is constant. It is adjusted by controlling. The reason why the liquid level of the makeup water W1 of the gas-liquid separator 11 is adjusted to be constant is to replenish the gas-liquid separator 11 with an amount corresponding to the lost makeup water W1 supplied as steam S.

  The make-up water W1 transferred to the gas-liquid separator 11 passes through the make-up water transfer pipe 6 and is boosted by the feed water pump P13 and sent to the heated pipes 123 and 223 of the absorbers A1 and A2. The absorbers A1 and A2 Then, it is heated by the absorption heat of the absorption liquid ALi that absorbs the refrigerant vapor CS to generate the vapor S, returns to the gas-liquid separator 11 through the makeup water transfer pipes 110 and 210, and separates the vapor and the liquid. The generated steam S passes through the steam supply line 8, and the flow rate is adjusted by the steam valve V <b> 1 controlled by the control device 21 so that the pressure of the gas-liquid separator 11 becomes the first predetermined pressure P <b> 1. It is supplied to a header (not shown).

  The pressure of the gas-liquid separator 11 is controlled to be a predetermined pressure P1 because the pressure of the gas-liquid separator 11 is controlled to be higher than the pressure of the steam header (not shown), and the gas-liquid separator 11 is controlled. Is always higher than the pressure of the steam header by a certain pressure so that the steam S generated by the absorption heat pump 100 is always supplied to the steam header, and the steam S is stably supplied to the load (not shown) side. This is to make it happen.

  With the configuration as described above, the absorption heat pump 100 of the present embodiment pumps the heat held in the exhaust gas GH from the evaporator E1 to the absorber A1 and from the evaporator E2 to the absorber A2 to replenish the medium to be heated. Water W1 is heated. In the present embodiment, the makeup water W1 is heated to become steam and is supplied to the outside.

  With reference to the perspective view of FIG. 3 and the top view of FIG. 4, the structure of the evaporators E1 and E2 and the regenerators G2 and G1 constituting the absorption heat pump 100 of the first embodiment of the present invention will be described. FIG. 3 is a perspective view of the evaporators E1 and E2 and the regenerators G2 and G1 as viewed from obliquely above with a part of each upper header cut away. FIG. 4 is a plan view of the evaporators E1 and E2 and the regenerators G2 and G1 as viewed from above with their respective upper headers removed. In this figure, the refrigerant liquid inlets and refrigerant vapor outlets of the evaporators E1 and E2, and the absorption liquid inlet and the absorption liquid outlet of the regenerators G2 and G1 are not shown.

  The evaporator E1 included in the absorption heat pump 100 of the present embodiment includes an upper tube plate 152 that is horizontally disposed and a lower tube plate 153 that is disposed in parallel thereto. A plurality of vertical heat transfer tubes 151 are disposed vertically between the upper tube plate 152 and the lower tube plate 153. Each vertical heat transfer tube 151 is inserted into a hole formed in each of the upper and lower tube sheets 152 and 153 and expanded, and then sealed to ensure airtightness. The plurality of vertical heat transfer tubes 151 are arranged in a lattice or zigzag pattern in a rectangular region when viewed from the axial direction of the tubes, forming a group of tubes. The liquid refrigerant liquid CL flows inside the plurality of vertical heat transfer tubes 151. That is, the evaporator E1 has a water tube boiler structure.

  The structure of the evaporator E2 is the same as that of the evaporator E1 except that the structure is on the downstream side of the flow of the exhaust gas GH of the evaporator E1. In other words, an upper tube plate 252 and a lower tube plate 253 are provided, and a plurality of vertical heat transfer tubes 251 are arranged between the two tube plates. The evaporator E2 has a water tube boiler structure just like the evaporator E1.

  Similarly, the regenerator G1 provided in the absorption heat pump 100 of the present embodiment includes an upper tube plate 172 arranged horizontally and a lower tube plate 173 arranged in parallel thereto. A plurality of vertical heat transfer tubes 171 are vertically arranged between the upper tube plate 172 and the lower tube plate 173. Each vertical heat transfer tube 171 is inserted into holes formed in the upper and lower tube plates 172 and 173 and expanded, and then sealed to ensure airtightness. The plurality of vertical heat transfer tubes 171 are arranged in a lattice or zigzag manner in a rectangular region when viewed from the axial direction of the tubes, forming a group of tubes. The absorbing liquid ALi flows inside the plurality of vertical heat transfer tubes 171. That is, the regenerator G has a water tube boiler structure.

  The structure of the regenerator G2 is the same as that of the regenerator G1 except that the regenerator G2 is located upstream of the regenerator G1 in the flow of the exhaust gas GH and downstream of the evaporator E2. That is, an upper tube plate 272 and a lower tube plate 273 are provided, and a plurality of vertical heat transfer tubes 271 are arranged between the two tube plates. The regenerator G2 has a water tube boiler structure just like the regenerator G1.

  In the absorption heat pump 100 of the present embodiment, the upper tube plates 152 and 252 of the evaporators E1 and E2, the upper tube plates 172 and 272 of the regenerators G1 and G2, and the lower tube plates 153 and 253 of the evaporators E1 and E2 The lower tube plates 173 and 273 of the regenerators G1 and G2 are each formed as an integral tube plate. Since the evaporators E1 and E2 and the regenerators G2 and G1 are heated by the exhaust gas GH, which is a common heat source, they can be provided adjacent to each other and can be efficiently manufactured by forming them as a single unitary plate. It becomes. The evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are preferably arranged as close as possible as long as the headers of the evaporators E1 and E2 and the regenerators G2 and G1 are possible. . Alternatively, it is preferable to arrange the dampers as the flow restricting means described below as close as possible as long as they can be inserted and arranged. By disposing them close to each other, the flow path of the exhaust gas GH can be prevented from becoming long and the flow loss of the exhaust gas GH can be suppressed.

  In addition, you may form the above tube sheet separately by each evaporator and regenerator. Further, it may be common to the evaporator E1 and the evaporator E2, and may be common to the regenerator G2 and the regenerator G1. This is because, when the apparatus size is large, the division may be preferable from the viewpoint of manufacturing and transportation.

  In the absorption heat pump 100 of the present embodiment, exhaust gas crosses the vertical heat transfer tubes 151, 251, 271, and 171 outside the plurality of vertical heat transfer tubes 151, 251, 271, and 171 of the evaporators E 1 and E 2 and the regenerators G 2 and G 1. GH1, GH102, GH5, and GH202 flow and are configured to be discharged as exhaust gas GH4. The flow of the exhaust gas GH between the upper tube plates 152 and 252 and the lower tube plates 153 and 253 of the evaporators E1 and E2, and between the upper tube plates 272 and 172 and the lower tube plates 273 and 173 of the regenerators G2 and G1. A path 60 is formed. In the present embodiment, the exhaust gas GH flows through the flow path 60 so as to intersect the vertical heat transfer tube 151 and the like at right angles. With respect to the vertical heat transfer tube 151 and the like, the exhaust gas GH flows to the outside of the tube, and the refrigerant liquid CL and the absorption liquid ALi flow to the inside of the tube, so that a large flow path 60 of the exhaust gas GH can be secured and an increase in the flow rate can be avoided.

  The plurality of vertical heat transfer tubes 151, 251, 271 and 171 are composed of the evaporator tubes E1 and E2 and the regenerators G2 and G1, respectively, and constitute the evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170, respectively. The evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are linearly arranged with respect to the flow of the exhaust gas GH. The linear arrangement means that the flow path 60 of the exhaust gas GH is arranged in one path instead of a plurality of paths like so-called two paths or three paths. In other words, when the evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are removed and the exhaust side is viewed from the supply side of the exhaust gas GH, the exhaust side can be seen through the flow path 60 of the exhaust gas GH. Say.

  Since the heat source is a gas such as exhaust gas with a small heat capacity per unit volume because it is arranged linearly, and it is necessary to flow a heat source gas with a very large volume flow rate to obtain the required amount of heat, flow resistance The pressure loss due to can be kept low. In other words, bending loss or loss due to turns can be reduced. The power for causing the heat source gas such as exhaust gas to flow tends to increase, but this can be kept small, and the energy saving effect is not reduced.

  As described above, in the evaporators E1 and E2 and the regenerators G2 and G1, the upper tube plates and the lower tube plates may not be formed as a single tube plate, but may be separated from each other. If separate, the arrangement of the evaporators E1 and E2 and the regenerators G2 and G1 can be determined by their own convenience. Even when each device is separated, the evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are linearly arranged with respect to the flow of the exhaust gases GH1, GH102, GH5, GH202, and GH4. does not change. In the case of separate bodies, these devices are preferably arranged as close as possible. This is to keep the flow path loss of the exhaust gas low.

  In the present embodiment, the regenerator tube groups 270 and 170 are arranged on the downstream side of the evaporator tube groups 150 and 250 with respect to the flow of the exhaust gas GH.

  When the heat source is a gas such as exhaust gas, the temperature range to be used is large. For example, it is supplied at 200 ° C. and discharged at 100 ° C. In this case, a temperature difference of 100 ° C. is used. Therefore, when exhaust gas is used as a heat source, there is a risk of overconcentration of the absorbing solution by a relatively high temperature gas and crystallization. However, since the regenerator tube groups 270 and 170 are disposed on the downstream side of the evaporator tube groups 150 and 250, the exhaust gas GH is supplied to the regenerators G2 and G1 after the temperature is lowered to a certain degree by the evaporators E1 and E2. The Accordingly, it is possible to suppress the overconcentration of the absorbing solution and the risk of crystallization due to the upstream portion to which the exhaust gas GH is supplied, in other words, the relatively high temperature portion.

  Further, in the present embodiment, the evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are blocked from the outside air, and cooperate with the tube plates 152, 153, 252, 253, 272, 273, 172, and 173. And side plates 154a, 154b, 254a, 254b, 274a, 274b, 174a, 174b (see FIG. 4) constituting the flow path of the exhaust gas GH. A water-cooled wall may be used instead of the side plate 154a or the like, but if it is about 250 ° C. or lower, typically about 200 ° C. like exhaust gas, it can be constituted by a simple flat plate (iron plate) and has a simple structure. It becomes. That is, a single-layer structure or a single-plate structure can be used instead of a structure in which a fluid having pressure between layers is accommodated in a multilayer structure like a water-cooled wall. In the absorption heat pump 100 of the present embodiment, the evaporators E1 and E2 and the regenerators G2 and G1 are often pressure vessels having a pressure equal to or higher than atmospheric pressure. In that case, each of the upper headers 155, 255, 275, 175 and the lower headers 156, 256, 276, 176 (especially the header of the evaporator in the absorption heat pump) is subjected to pressure, but the side plate is not a water-cooled wall but a simple single-layer flat plate. Therefore, it becomes easy to deal with strength. In the present embodiment, the inside of the header of the regenerator can be negative pressure, but since the side plate is not a water-cooled wall but a simple single-layer flat plate, it is easy to cope with external pressure.

  As already described, the evaporators E1 and E2 and the regenerators G2 and G1 or the evaporator tube groups 150 and 250 and the regenerator tube groups 270 and 170 are linear with respect to the flow of the exhaust gas GH. Is arranged. Typically, the side plates 154a and 254a and the side plates 274a and 174a are formed in a single flat shape, and the side plates 154b and 254b and the side plates 274b and 174b are formed in a single flat shape, respectively. Is formed of a single flat plate, and the evaporator upper tube plates 152 and 252 and the regenerator upper tube plates 272 and 172 are formed in one plane, and the evaporator lower tube plates 153 and 253 and the regenerator are formed. It can be said that the lower tube plates 273 and 173 are similarly formed in a single flat shape, and preferably each formed by a single flat plate.

  It is preferable that the outside air side of the side plates 154a, 154b, 254a, 254b, 274a, 274b, 174a, 174b is provided with a heat insulating material. This is because the heat that can be used is not released to the outside although it is said that the temperature is not so high. It is also for safety to the human body.

  Further, in the present embodiment, the evaporators E1 and E2 and the regenerators G2 and G1 regenerate with the evaporator upper headers 155 and 255 so as to cover the upper openings of the respective tube groups 150, 250, 270, and 170. Regenerator upper headers 275 and 175 are provided, and evaporator lower headers 156 and 256 (refrigerant liquid supply chamber) and regenerator lower headers 276 and 176 (solution supply chamber) are provided so as to cover the lower opening. The evaporator upper headers 155 and 255 may also serve as a gas-liquid separation chamber. With this configuration, the structure can be simplified.

  The combination of the evaporators E1 and E2 and the regenerators G2 and G1 used in the second embodiment of the present invention will be described with reference to the plan view of FIG. FIG. 5 is a plan view of the vertical heat transfer tubes 151, 251, 271, and 171 as viewed from the axial direction, that is, from above, with the upper headers of the evaporators E1 and E2 and the generators G2 and G1 removed. In the present embodiment, the regenerator tube group 270 is bypassed from the downstream end of the evaporator tube group 250 in the flow path 60 of the exhaust gas GH as the heat source gas, and the exhaust gas GH is removed from the regenerator tube group 270. A bypass passage 91 is provided to flow downstream.

  The bypass channel 91 is a channel that guides all or part of the exhaust gas GH5 after passing through the exhaust gas GH102 or the evaporator tube group 250 to the downstream side of the regenerator tube group 270.

  Here, the downstream end of the evaporator tube group 250 is a downstream portion of the vertical heat transfer tube 251 that is the most downstream in the flow direction of the exhaust gas GH, that is, the exhaust gas GH102 passes through the entire evaporator tube group 250. A portion that becomes the exhaust gas GH5, that is, a space portion between the evaporator tube group 250 and the regenerator tube group 270 is preferable. However, as illustrated, the exhaust gas GH102 includes a plurality of upstream portions of the evaporator tube group 250. The part after passing a vertical heat exchanger tube may be sufficient. That is, it may be a portion including a space portion between the evaporator tube group 250 and the regenerator tube group 270, or may be a portion slightly upstream. At this time, it is preferable that the portion where the bypass flow path 91 starts does not cover the regenerator tube group 270. The purpose of providing the bypass passage 91 is to prevent excessive concentration of the absorption liquid in the regenerator G2, and thus crystallization.

  If the starting point of the bypass passage 91 is a portion where the exhaust gas GH102 passes through the entire evaporator tube group 250 and becomes the exhaust gas GH5, the evaporator E2 can use the high-temperature portion of the exhaust gas GH102 as much as possible and use heat. From the viewpoint of However, even if the start point of the bypass passage 91 is a part after the exhaust gas GH102 has passed a certain number of vertical heat transfer tubes 251 upstream of the evaporator tube group 250, the amount of heat of the exhaust gas GH102 is considerably utilized by the evaporator E2. In addition, the flexibility of the device configuration can be increased. That is, the space portion between the evaporator tube group 250 and the regenerator tube group 270 can be configured to be short, and the apparatus can be made compact and the flow resistance can be reduced.

  The bypass channel 91 includes a damper 92 that limits the bypass flow rate. This is because the bypass passage 91 bypasses the exhaust gas GH5 sufficient to prevent excessive concentration of the absorption liquid ALi in the regenerator G2 and thus crystallization. There is no need to bypass more than necessary. It is preferable that the damper 92 can not only limit the flow rate of the exhaust gas GH5 but also can block it. This is because when the concentration of the absorbing solution in the regenerator G2 is not in the dangerous region, it is preferable to completely shut it off from the viewpoint of heat recovery.

  In FIG. 5, the bypass 91 is shown as bypassing both the regenerator G2 and the regenerator G1, but at least the regenerator G2 may be bypassed. The reason why the absorption liquid is excessively concentrated and has a high risk of crystallization is because the regenerator G2 is located upstream of the exhaust gas.

  In this embodiment, a concentration detector DEN (see FIG. 1) for detecting the concentration of the absorbing liquid ALi in the regenerator G2 may be provided. When the regenerator G1 is compared with the regenerator G2, the regenerator G2 has a possibility of crystals and overconcentration, as shown in the Duling diagram (see FIG. 2). Therefore, when the outlet concentration of the regenerator G2 increases, the concentration capacity of the regenerator G2 may be adjusted. Therefore, the concentration detector DEN is provided, and the opening degree of the damper 92 is adjusted according to the concentration of the absorbing liquid ALi in the regenerator G to adjust the amount of exhaust gas flowing into the regenerator G2. The concentration detector DEN is installed in a position where the concentration of the absorbing liquid ALi in the regenerator G2 is highest, typically in the upper header 275. In addition, as shown in FIG. 1, you may install in the absorption liquid transfer pipe line 202 which guide | induces the absorption liquid ALi from the upper header 275 to absorber A2. In that case, a position as close to the regenerator G2 as possible is preferable. The concentration detector DEN is not limited to a detector that directly detects the concentration, but may be one that indirectly detects the concentration. That is, a physical quantity corresponding to the concentration, for example, a density of the absorbing solution may be detected. The density here may be a calculated value related to the density. That is, the concentration may be detected from density and temperature, may be detected from sound speed and temperature, and may be based on density and specific gravity instead of concentration. Alternatively, the concentration may be estimated from the relationship between the solution temperature at the outlet of the regenerator and the vapor pressure (or dew point) of the regenerator G2. That is, it may be calculated from the vapor-liquid equilibrium relationship of the solution. Since the vapor pressure or dew point of the regenerator is strongly influenced by the cooling water temperature, the danger of concentration may be determined from the solution temperature and the cooling water temperature. What is estimated or calculated in this way is also a form of concentration detection.

  In this embodiment, it is preferable to provide a damper 93 between the evaporator E2 and the regenerator G2, more specifically between the evaporator tube group 250 and the regenerator tube group 270. If the bypass flow path 91 and the damper 92 are provided, a considerable amount of the exhaust gas GH5 can flow through the bypass 91 due to the flow path resistance of the regenerator tube group 270 (and the regenerator tube group 170). By providing this, the range of adjustment can be expanded. The damper 93 is a multi-leaf type, that is, a flat plate in which the main body portion is divided into a plurality of pieces in the vertical or horizontal direction, and is rotatable around the longitudinal central axis of each of the vertically or horizontally long plates. When the multi-leaf type is used, it is not necessary to make a large space between the evaporator E2 and the regenerator G2, and the combination of the evaporators E1 and E2 and the regenerators G2 and G1 can be easily made compact. The damper 92 may also be a multi-leaf type.

  It is preferable that the damper 93 not only restricts the flow rate of the exhaust gas GH5 but also can block it. This is because, depending on the concentration of the absorbing solution in the regenerator G2, there may be a case where it is desired to temporarily block completely. When the damper 93 is completely shut off, the damper 92 is normally fully opened.

  When the bypass channel 91 is provided, it seems that the side plates 274b and 174b have a multilayer structure instead of a single layer structure or a single plate structure. However, the bypass channel 91 is different from the structure of the water-cooled wall having a multilayer structure to which the internal pressure is applied. That is, when the exhaust gas GH flows through the exhaust gas passage 60, the pressure is low enough to be ignored. Therefore, the side plates 274b and 174b can be a single layer structure or a single plate structure, and are the same as the case where the bypass channel 91 is not provided. Only a bypass passage 91 that does not need to be handled as a pressure vessel is provided outside the side plates 274b and 174b having a single layer structure.

  According to a trial calculation, when the inlet temperature of the exhaust gas GH1 is 200 ° C. and the steam S of 180 ° C. is obtained, the exhaust gas boiler can obtain only about 12 heat, whereas the absorption heat pump uses about 43 The amount of heat is obtained. Moreover, when the inlet temperature of the exhaust gas GH1 is 180 ° C., the amount of heat obtained is naturally zero in the exhaust gas boiler, whereas when the absorption heat pump is used, a heat amount of about 32 is obtained. Here, the generated steam calorific value is shown as a relative number with the calorific value when the exhaust gas is used from 200 ° C. to 100 ° C. being 100.

  The evaporators E1 and E2 and the regenerators G2 and G1 not only have a common tube plate, but may have a can body as an integral structure.

  The absorption heat pump of the present invention is used when a heat source outlet temperature difference is greatly utilized, and particularly used for recovering heat from a heat source gas such as exhaust gas and heating a medium to be heated.

5 Refrigerant liquid transfer line 7 Supply water transfer line 8 Steam supply line 11 Gas-liquid separators 17, 117, 217 Refrigerant vapor transfer pipe 100 Absorption heat pump 100-1 First absorption heat pump unit 100-2 Second absorption Heat pump unit 102, 103, 202, 203 Absorbing liquid transfer pipe 116, 216 Refrigerant vapor transfer pipe 122, 222 Absorbing liquid spray 123, 223 Heated pipe 21 Control device 30 Cooling pipe 37 Check valve 38 Check valve 40 Check Valve 60 Exhaust gas channel 91 Bypass channel 92, 93 Damper 139, 239 Check valve 150, 250 Evaporator tube group 151, 251 Vertical heat transfer tube 152, 252 Evaporator upper tube plate 153, 253 Evaporator lower tube plate 154a, 154b, 254a, 254b Evaporator side plates 155, 255 Evaporator upper header 156, 256 Evaporator lower header 170, 27 0 Regenerator tube group 171, 271 Vertical heat transfer tube 172, 272 Regenerator upper tube plate 173, 273 Regenerator lower tube plate 174a, 174b, 274a, 274b Regenerator side plate 175, 275 Regenerator upper header 176, 276 Regenerator lower Header A1, A2 Absorber (absorption part)
ALi Absorbent B Heat exchanger C Condenser CS Refrigerant vapor CL Refrigerant liquid DEN Concentration sensor E1, E2 Evaporator G1, G2 Regenerator GH, GH0, GH1, GH3, GH4, GH5, GH102, GH202 Exhaust gas L101, L201, L102 , L202, L3 Liquid level sensor P Pressure sensor P4 Refrigerant pump P12, P13 Feed water pump P101, P201 Solution pump S Steam V1 Steam valve V103, V203 Refrigerant supply valve W1 Supply water WC Cooling water X2 Heat exchanger X101, X201 Solution heat Exchanger

Claims (5)

A first evaporator that heats and evaporates the refrigerant with a heat source fluid;
A first absorber that absorbs the refrigerant evaporated in the first evaporator and heats the medium to be heated with absorption heat;
A first regenerator that absorbs the refrigerant in the first absorber and regenerates the absorbed liquid having a reduced concentration by the heat source fluid;
A second evaporator that heats and evaporates the refrigerant with the heat source fluid;
A second absorber that absorbs the refrigerant evaporated in the second evaporator and heats the medium to be heated with absorption heat;
A second regenerator that regenerates the refrigerant by absorbing the refrigerant in the second absorber and heating it with the heat source fluid;
The first evaporator, the second evaporator, the second regenerator, and the first regenerator are arranged in a flow path through which the heat source fluid flows from the upstream side to the downstream side of the heat source fluid. Arranged in order;
Absorption heat pump. The heat source fluid is a heat source gas;
The first evaporator and the second evaporator are respectively
An evaporator upper tube sheet,
An evaporator lower tube sheet,
A plurality of vertical heat transfer tubes provided between the evaporator upper tube plate and the evaporator lower tube plate, through which the liquid refrigerant flows;
The first regenerator and the second regenerator are respectively
A regenerator upper tube sheet;
A regenerator lower tube sheet,
A plurality of vertical heat transfer tubes through which the absorbing liquid flows inside the regenerator upper tube sheet and the regenerator lower tube sheet;
The heat source gas flows outside the plurality of vertical heat transfer tubes across the vertical heat transfer tubes;
The plurality of vertical heat transfer tubes include the first evaporator, the second evaporator, the second regenerator, and the first regenerator, respectively, The second evaporator tube group, the second regenerator tube group, and the first regenerator tube group, the first evaporator tube group, the second evaporator tube group, The second regenerator tube group and the first regenerator tube group are linearly arranged with respect to the flow of the heat source gas;
The absorption heat pump according to claim 1.   A bypass flow path that bypasses the second regenerator from the downstream end of the second evaporator and flows the heat source gas to the downstream side of the second regenerator in the heat source gas flow path. An absorption heat pump according to claim 1 or 2, further comprising a flow restriction means for restricting a flow of the heat source gas in the bypass flow path.   The first absorber and the second absorber are configured to heat water as the medium to be heated and generate water vapor having a pressure higher than atmospheric pressure, and separate the generated water vapor from the accompanying water. The absorption heat pump of any one of Claims 1 thru | or 3 provided with the gas-liquid separator which performs.   5. The heat exchanger according to claim 1, further comprising a heat exchanger that directly generates water vapor by heat of the heat source fluid in the flow path of the heat source fluid upstream of the first evaporator. Absorption heat pump.

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