Efficient recovery type second-class absorption heat pump
By adopting two-stage absorption and evaporation structures and processes in the factory, combining refrigerant water flashing and heat recovery heat exchangers, the problems of insufficient steam grade and yield, low heat exchange efficiency and unstable liquid level in the prior art are solved. , achieving efficient and stable heat pump operation and energy utilization.
Patent Information
- Application Number
- CN202420849411.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-23
- Publication Date
- 2024-12-06
- Estimated Expiration
- 2034-04-23
AI Technical Summary
The existing Class II absorption heat pumps cannot effectively improve steam grade and output in factories, and there are problems of low heat exchange efficiency and unstable liquid level, resulting in energy waste and fluctuations in steam production.
The structure and process of two-stage absorption and evaporation are adopted. The low-pressure absorber is refrigerant water circulation, and the high-pressure evaporator has no heat transfer pipe. Heat exchange is performed by flashing the refrigerant water, and intermediate concentration and dilute solution are set on the solution circulation pipeline. Heat recovery heat exchanger, increase refrigerant water heating heat exchanger, increase steam pressure and output, and reduce internal losses.
It improves the output taste and output of steam, reduces energy waste, ensures stability of liquid level, improves heat exchange efficiency, meets the cooling and steam demand of low-temperature waste heat resources, and reduces processing and operation costs.
Smart Images
Figure CN222123541U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of heat exchange equipment and relates to a high-efficiency recovery type second-class absorption heat pump. Background Art
[0002] A large amount of high-temperature steam is required in the production process, and at the same time, there are a large amount of low-temperature waste heat resources. The use of Class II absorption heat pump units to extract low-temperature waste heat can produce high-temperature steam and save high-grade heat source consumption. It has been widely used in recent years. However, the low-temperature waste heat discharged by factory production is expected to be recycled and utilized to the maximum extent, and more high-grade steam can be produced at the same time. On the one hand, it can meet the cooling needs of low-temperature waste heat resources, and on the other hand, it can meet the needs of factory steam use. The structure, process and control technology of conventional Class II absorption heat pumps cannot significantly improve the quality of the produced steam. How to improve the heat exchange efficiency of the heat pump unit so that the absorption heat pump can operate efficiently and stably, and produce a large amount of high-grade steam, and at the same time use effective control to ensure that the liquid level in the flash tank remains stable and avoid fluctuations in steam production has become one of the important research topics at present. Utility Model Content
[0003] The purpose of the utility model is to overcome the deficiencies in the above-mentioned background technology and provide a high-efficiency recovery type second-class absorption heat pump, which adopts a two-stage absorption and evaporation structure and process, wherein the refrigerant water circulates in the low-pressure absorber tube and the solution circulates outside the tube, and no heat transfer tube is arranged inside the high-pressure evaporator. The high-pressure evaporator exchanges heat by flash evaporation of the refrigerant water. The refrigerant water flows by gravity and density difference, and no power device is required, which reduces the processing cost and operation cost of the unit. In addition, an intermediate concentration solution heat recovery heat exchanger and a dilute solution heat recovery heat exchanger are arranged on the solution circulation pipeline to recover the solution. The superheated heat heats the refrigerant water, reducing the amount of flash of the solution in the low-pressure absorber and regenerator. At the same time, a refrigerant heating heat exchanger is set on the refrigerant water pipeline between the low-pressure evaporator, high-pressure evaporator and condenser to increase the temperature of the refrigerant water sent to the low-pressure steamer and high-pressure evaporator, thereby reducing internal heat exchange losses, achieving efficient use of heat source water, improving the output quality and output of steam, and improving the heat exchange efficiency of the unit, avoiding energy waste. At the same time, effective control is adopted to ensure that the liquid level in the flash tank remains stable, avoiding fluctuations in steam production, and ensuring stable operation of the unit.
[0004] The technical solution adopted by the utility model to solve the technical problem is: a high-efficiency recovery type second-class absorption heat pump, including a condenser, a regenerator, a low-pressure evaporator, a low-pressure absorber, a high-pressure evaporator, a high-pressure absorber, a low-temperature heat exchanger, a high-temperature heat exchanger, a refrigerant heating heat exchanger, a solution pump, a refrigerant liquid delivery pump, and a flash tank, wherein the condenser and the regenerator can be arranged in two cylinders or in one cylinder, and the condenser and the regenerator are connected through a refrigerant steam channel A; the low-pressure evaporator and the low-pressure absorber can be arranged in two cylinders or in one cylinder. It is arranged in a cylinder, and the low-pressure evaporator and the low-pressure absorber are connected through the refrigerant steam channel B; the low-pressure evaporator and the low-pressure absorber are arranged on the upper part of the condenser and the regenerator, the high-pressure evaporator and the high-pressure absorber are arranged on the upper part of the low-pressure evaporator and the low-pressure absorber, and the flash tank is arranged on the upper part of the high-pressure absorber; the condenser is connected to the cooling water inlet pipeline and the cooling water outlet pipeline, the low-pressure evaporator is connected to the heat source water inlet pipeline and the heat source water pipeline, the regenerator is connected to the heat source water pipeline and the heat source water outlet pipeline, and the low-pressure evaporator and the regenerator are connected through the heat source water pipeline.
[0005] The regenerator and the low-temperature heat exchanger are connected via a concentrated solution pipeline A, on which a solution pump is arranged, the low-temperature heat exchanger and the high-temperature heat exchanger are connected via a concentrated solution pipeline B, the high-temperature heat exchanger and the high-pressure absorber are connected via a concentrated solution pipeline C and an intermediate concentration solution pipeline A, the high-temperature heat exchanger and the low-pressure absorber are connected via an intermediate concentration solution pipeline B, the low-pressure absorber and the low-temperature heat exchanger are connected via a dilute solution pipeline A, the low-temperature heat exchanger and the regenerator are connected via a dilute solution pipeline B, no power device is configured between the high-pressure absorber, the high-temperature heat exchanger and the low-pressure absorber, and no power device is configured between the low-pressure absorber, the low-temperature heat exchanger and the regenerator.
[0006] The low-pressure absorber and the high-pressure evaporator are connected through a refrigerant water pipeline A and a refrigerant water pipeline B. The refrigerant water circulates inside the low-pressure absorber tube and the solution circulates outside the tube. No heat transfer tube is arranged inside the high-pressure evaporator. The high-pressure evaporator performs heat exchange by flash evaporation of refrigerant water. No power device is arranged between the low-pressure absorber and the high-pressure evaporator. The condenser and the refrigerant heating heat exchanger are connected through a refrigerant water pipeline C and a refrigerant water pipeline H. A refrigerant liquid delivery pump is arranged on the refrigerant water pipeline C. The refrigerant water pipeline D connected to the refrigerant heating heat exchanger is divided into two paths, one of which is connected to the low-pressure evaporator through a refrigerant water pipeline E, and the other is connected to the refrigerant water pipeline A through a refrigerant water pipeline F. A refrigerant regulating valve A is arranged on the refrigerant water pipeline F. The low-pressure evaporator and the refrigerant heating heat exchanger are connected through a refrigerant water pipeline G. A refrigerant regulating valve B is arranged on the refrigerant water pipeline G.
[0007] The low-pressure evaporator and the high-pressure evaporator are respectively provided with a liquid level detection device C and a liquid level detection device B.
[0008] The high-pressure absorber and the flash tank are connected through hot water circulation pipeline A and hot water circulation pipeline B. No power device is configured between the high-pressure absorber and the flash tank. The water supply pipeline is connected to the hot water circulation pipeline B. A water supply control valve is arranged on the water supply pipeline. A steam pipeline, a pressure sensor, a safety discharge device, and a liquid level detection device A are arranged on the flash tank. A steam control valve is arranged on the steam pipeline.
[0009] An intermediate concentration solution heat recovery heat exchanger is arranged on the intermediate concentration solution pipeline B, a dilute solution heat recovery heat exchanger is arranged on the dilute solution pipeline B, the intermediate concentration solution heat recovery heat exchanger and the dilute solution heat recovery heat exchanger are connected via a refrigerant water pipeline J, the dilute solution heat recovery heat exchanger and the refrigerant water pipeline C are connected via a refrigerant water pipeline I, a refrigerant regulating valve C is arranged on the refrigerant water pipeline I, and the intermediate concentration solution heat recovery heat exchanger and the refrigerant water pipeline D are connected via a refrigerant water pipeline K.
[0010] The power device includes a circulation pump, a booster pump or a stepless speed regulator joint.
[0011] The beneficial effects of the utility model are:
[0012] (1) A two-stage absorption and evaporation structure and process is adopted. The refrigerant water circulates inside the low-pressure absorber tube and the solution circulates outside the tube. No heat transfer tube is set inside the high-pressure evaporator. The high-pressure evaporator exchanges heat by flash evaporation of the refrigerant water. The refrigerant water flows by gravity and density difference. No power device is required, which reduces the processing cost and operating cost of the unit. The heat in the low-pressure absorber is transferred to the high-pressure evaporator through the refrigerant water, and then transported to the high-pressure absorber, which increases the temperature of the hot water in the high-pressure absorber, thereby increasing the pressure of the flash tank to produce steam.
[0013] (2) An intermediate concentration solution heat recovery heat exchanger and a dilute solution heat recovery heat exchanger are set on the solution circulation pipeline to recover the superheated heat of the solution to heat the refrigerant water, thereby reducing the flash of the solution in the low-pressure absorber and the regenerator. At the same time, a refrigerant heating heat exchanger is set on the refrigerant water pipeline between the low-pressure evaporator, the high-pressure evaporator and the condenser to increase the temperature of the refrigerant water sent to the low-pressure steam generator and the high-pressure evaporator. According to the superheat of the intermediate concentration solution flowing out of the high-temperature heat exchanger and the superheat of the dilute solution flowing out of the low-temperature heat exchanger, the opening of the refrigerant regulating valve is adjusted to maximize the waste heat recovery, reduce the internal heat exchange loss, realize the efficient use of heat source water, improve the output quality and output of steam, improve the heat exchange efficiency of the unit, avoid energy waste, meet the cooling needs of users for low-temperature waste heat resources, and meet the needs of the factory for high-quality use of steam. At the same time, effective control is adopted to ensure that the liquid level in the flash tank remains stable, avoid fluctuations in steam production, and ensure stable operation of the unit. BRIEF DESCRIPTION OF THE DRAWINGS
[0014] Figure 1 It is a schematic diagram of the structure of a high-efficiency recovery type second-class absorption heat pump according to Embodiment 1 of the present utility model;
[0015] Figure 2 It is a schematic diagram of the structure of a high-efficiency recovery type second-class absorption heat pump of Example 2 of the utility model.
[0016] In the figure: condenser 1, regenerator 2, low-pressure evaporator 3, low-pressure absorber 4, high-pressure evaporator 5, high-pressure absorber 6, low-temperature heat exchanger 7, high-temperature heat exchanger 8, refrigerant heating heat exchanger 9, solution pump 10, refrigerant liquid delivery pump 11, flash tank 12, steam control valve 13, water supply control valve 14, pressure sensor 15, safety discharge device 16, liquid level detection device A17, liquid level detection device B18, cooling water inlet pipeline 19, cooling water outlet pipeline 20, heat source water inlet pipeline 21, heat source water pipeline 22, heat source water outlet pipeline 23, hot water circulation pipeline A24, hot water circulation pipeline B25, water supply pipeline 26, steam pipeline 27, refrigerant steam channel A28, refrigerant steam channel B29, cooling water outlet pipeline 20, heat source water inlet pipeline 21, heat source water pipeline 22, heat source water outlet pipeline 23, hot water circulation pipeline A24, hot water circulation pipeline B25, water supply pipeline 26, steam pipeline 27, refrigerant steam channel A28, refrigerant steam channel B29, agent steam channel C30, concentrated solution pipeline A31, concentrated solution pipeline B32, concentrated solution pipeline C33, intermediate concentration solution pipeline A34, intermediate concentration solution pipeline B35, dilute solution pipeline A36, dilute solution pipeline B37, refrigerant water pipeline A38, refrigerant water pipeline B39, refrigerant water pipeline C40, refrigerant water pipeline D41, refrigerant water pipeline E42, refrigerant water pipeline F43, refrigerant regulating valve A44, liquid level detection device C45, refrigerant water pipeline G46, refrigerant water pipeline H47, refrigerant regulating valve B48, dilute solution heat recovery heat exchanger 49, intermediate concentration solution heat recovery heat exchanger 50, refrigerant water pipeline I51, refrigerant regulating valve C52, refrigerant water pipeline J53, refrigerant water pipeline K54. DETAILED DESCRIPTION
[0017] The present invention is further described below in conjunction with the accompanying drawings, but the present invention is not limited to the following embodiments. Example 1
[0018] like Figure 1As shown, the first specific embodiment of the utility model involves a high-efficiency recovery type second-class absorption heat pump, including a condenser 1, a regenerator 2, a low-pressure evaporator 3, a low-pressure absorber 4, a high-pressure evaporator 5, a high-pressure absorber 6, a low-temperature heat exchanger 7, a high-temperature heat exchanger 8, a refrigerant heating heat exchanger 9, a solution pump 10, a refrigerant liquid delivery pump 11, and a flash tank 12, wherein the condenser 1 and the regenerator 2 can be arranged in two cylinders or in one cylinder, and the condenser 1 and the regenerator 2 are connected through a refrigerant steam channel A28; the low-pressure evaporator 3 and the low-pressure absorber 4 can be arranged in two cylinders or in one cylinder, and the low-pressure evaporator 3 and the low-pressure absorber 4 can be arranged in two cylinders or in one cylinder. The low-pressure absorber 4 is connected through the refrigerant steam channel B29; the low-pressure evaporator 3 and the low-pressure absorber 4 are arranged on the upper part of the condenser 1 and the regenerator 2, the high-pressure evaporator 5 and the high-pressure absorber 6 are arranged on the upper part of the low-pressure evaporator 3 and the low-pressure absorber 4, and the flash tank 12 is arranged on the upper part of the high-pressure absorber 6; the condenser 1 is connected to the cooling water inlet pipeline 19 and the cooling water outlet pipeline 20, the low-pressure evaporator 3 is connected to the heat source water inlet pipeline 21 and the heat source water pipeline 22, the regenerator 2 is connected to the heat source water pipeline 22 and the heat source water outlet pipeline 23, the low-pressure evaporator 3 and the regenerator 2 are connected through the heat source water pipeline 22, and the heat source water enters the low-pressure evaporator 3 and the regenerator 2 in series.
[0019] The regenerator 2 and the low-temperature heat exchanger 7 are connected via a concentrated solution pipeline A31, on which a solution pump 10 is arranged, the low-temperature heat exchanger 7 and the high-temperature heat exchanger 8 are connected via a concentrated solution pipeline B32, the high-temperature heat exchanger 8 and the high-pressure absorber 6 are connected via a concentrated solution pipeline C33 and an intermediate concentration solution pipeline A34, the high-temperature heat exchanger 8 and the low-pressure absorber 4 are connected via an intermediate concentration solution pipeline B35, the low-pressure absorber 4 and the low-temperature heat exchanger 7 are connected via a dilute solution pipeline A36, the low-temperature heat exchanger 7 and the regenerator 2 are connected via a dilute solution pipeline B37, the solution circulation between the high-pressure absorber 6, the high-temperature heat exchanger 8 and the low-pressure absorber 4 relies on gravity and pressure difference to flow, and there is no need to configure a power device such as a circulation pump, and the solution circulation between the low-pressure absorber 4, the low-temperature heat exchanger 7 and the regenerator 2 relies on gravity and pressure difference to flow, and there is no need to configure a power device such as a circulation pump. The regenerator 2, the low-pressure absorber 4, the high-pressure absorber 6, the low-temperature heat exchanger 7, the high-temperature heat exchanger 8, and the solution pump 10 form a solution cycle, that is, the concentrated solution from the regenerator 2 is heated by the solution pump 10 through the low-temperature heat exchanger 7 and the high-temperature heat exchanger 8 in turn and then transported to the high-pressure absorber 6. The concentrated solution absorbs the heat of the refrigerant vapor from the high-pressure evaporator 5 through the refrigerant vapor channel C30 in the high-pressure absorber 6. The concentrated solution is diluted once to form an intermediate concentration solution. At the same time, the absorbed heat is released to the hot water in the hot water circulation pipeline A24 and the hot water circulation pipeline B25; the intermediate concentration solution enters the high-temperature heat exchanger 8 through the intermediate concentration solution pipeline A34 to heat the concentrated solution, and the high-temperature heat exchanger 8 flows out After the temperature of the intermediate concentration solution is reduced, it enters the low-pressure absorber 4 through the intermediate concentration solution pipeline B35. In the low-pressure absorber 4, the intermediate concentration solution absorbs the heat of the refrigerant vapor in the low-pressure evaporator 3 through the refrigerant vapor channel B29. The intermediate concentration solution is diluted twice in the low-pressure absorber 4 to form a dilute solution. At the same time, the absorbed heat is released to the refrigerant water in the refrigerant water pipeline A38 and the refrigerant water pipeline B39; the dilute solution enters the low-temperature heat exchanger 7 through the dilute solution pipeline A36 to heat the concentrated solution, and then enters the regenerator 2 through the dilute solution pipeline B37. The dilute solution is heated and concentrated by the heat source water in the regenerator 2 to form a concentrated solution, and the generated refrigerant vapor enters the condenser 1 through the refrigerant vapor channel A28 to be condensed.
[0020] The low-pressure absorber 4 and the high-pressure evaporator 5 are connected by a refrigerant water pipeline A38 and a refrigerant water pipeline B39. The low-pressure absorber 4 has refrigerant water circulating inside the tube and solution circulating outside the tube. No heat transfer tube is arranged inside the high-pressure evaporator 5. The high-pressure evaporator 5 exchanges heat by flash evaporation of refrigerant water. The refrigerant water between the low-pressure absorber 4 and the high-pressure evaporator 5 flows by gravity and density difference, and there is no need to configure a power device such as a circulating pump. The heat in the low-pressure absorber 4 is transferred to the high-pressure evaporator 5 through the refrigerant water, and then transported to the high-pressure absorber 6, thereby increasing the temperature of the hot water in the high-pressure absorber 6, realizing a two-stage absorption and evaporation structure and process, thereby increasing the pressure of the flash tank 12 to produce steam, and fully The cooling demand of the user's low-temperature waste heat resources is met, and the demand for high-grade use of factory steam is met at the same time; the condenser 1 and the refrigerant heating heat exchanger 9 are connected through the refrigerant water pipeline C40 and the refrigerant water pipeline H47, and a refrigerant liquid delivery pump 11 is arranged on the refrigerant water pipeline C40; the refrigerant water pipeline D41 connected to the refrigerant heating heat exchanger 9 is divided into two paths, one of which is connected to the low-pressure evaporator 3 through the refrigerant water pipeline E42, and the other is connected to the refrigerant water pipeline A38 through the refrigerant water pipeline F43, and a refrigerant regulating valve A44 is arranged on the refrigerant water pipeline F43; the low-pressure evaporator 3 and the refrigerant heating heat exchanger 9 are connected through the refrigerant water pipeline G46, and a refrigerant regulating valve B48 is arranged on the refrigerant water pipeline G46. The condenser 1, the low-pressure evaporator 3, the low-pressure absorber 4, the high-pressure evaporator 5, and the refrigerant liquid delivery pump 11 form a refrigerant water cycle, that is, the refrigerant water in the low-pressure absorber 4 tube absorbs the heat from the solution outside the low-pressure absorber 4 tube. After the refrigerant water is heated, it enters the high-pressure evaporator 5 through the refrigerant water pipeline B39 to flash evaporate to form high-temperature refrigerant steam. The high-temperature refrigerant steam enters the high-pressure absorber 6 through the refrigerant steam channel C30. The refrigerant water then enters the low-pressure absorber 4 tube through the refrigerant water pipeline A38 to be heated and heated. The refrigerant water stored in the lower part of the low-pressure evaporator 3 enters the refrigerant heating heat exchanger 9 through the refrigerant water pipeline G46 by the action of pressure difference and gravity, and then enters the refrigerant heating heat exchanger 9 through the refrigerant water pipeline H47. Enters the condenser 1; the low-temperature refrigerant water from the condenser 1 is sent to the refrigerant heating heat exchanger 9 through the refrigerant liquid delivery pump 11, and is heated by the high-temperature refrigerant water from the low-pressure evaporator 3, thereby reducing the internal heat exchange loss, improving the heat exchange efficiency of the unit, and avoiding energy waste; the refrigerant water flowing out of the refrigerant heating heat exchanger 9 is divided into two paths, one of which is sent to the low-pressure evaporator 3 through the refrigerant water pipeline E42, and the refrigerant water in the low-pressure evaporator 3 absorbs the heat from the heat source water to form refrigerant vapor, and the refrigerant vapor enters the low-pressure absorber 4 through the refrigerant vapor channel B29, and the other is sent to the high-pressure evaporator 5 through the refrigerant water pipeline F43 to replenish the refrigerant liquid in the high-pressure evaporator 5.
[0021] The low-pressure evaporator 3 and the high-pressure evaporator 5 are provided with a liquid level detection device C45 and a liquid level detection device B18, respectively, for detecting the liquid storage height in the low-pressure evaporator 3 and the high-pressure evaporator 5. When the liquid level detection device C45 detects that the low-pressure evaporator 3 is at a high liquid level, the opening of the refrigerant regulating valve B48 is increased, and when the liquid level detection device C45 detects that the low-pressure evaporator 3 is at a low liquid level, the opening of the refrigerant regulating valve B48 is reduced; when the liquid level detection device B18 detects that the high-pressure evaporator 5 is at a high liquid level, the opening of the refrigerant regulating valve A44 is reduced, and when the liquid level detection device B18 detects that the high-pressure evaporator 5 is at a low liquid level, the opening of the refrigerant regulating valve A44 is increased, and effective control is adopted to ensure that the liquid levels in the low-pressure evaporator 3 and the high-pressure evaporator 5 remain stable, thereby ensuring the stable operation of the unit.
[0022] The high-pressure absorber 6 and the flash tank 12 are connected via a hot water circulation pipeline A24 and a hot water circulation pipeline B25. The hot water circulation between the high-pressure absorber 6 and the flash tank 12 flows by gravity and density difference, and there is no need to configure a power device such as a circulation pump. The water supply pipeline 26 is connected to the hot water circulation pipeline B25, and a water supply control valve 14 is arranged on the water supply pipeline 26. The flash tank 12 is provided with a steam pipeline 27, a pressure sensor 15, a safety discharge device 16, and a liquid level detection device A17, and a steam control valve 13 is arranged on the steam pipeline 27. The heat in the low-pressure absorber 4 is transferred to the high-pressure evaporator 5 through the refrigerant water. The high-pressure absorber 6 absorbs the heat of the high-temperature refrigerant steam formed by flash evaporation in the high-pressure evaporator 5. The hot water stored in the flash tank 12 enters the high-pressure absorber 6 through the hot water circulation pipeline B25. After the hot water is heated and heated, it enters the flash tank 12 through the hot water circulation pipeline A24 to flash out high-pressure steam. When the pressure of the flash tank 12 detected by the pressure sensor 15 is higher than the set value, the steam control valve 13 is opened, and the high-pressure steam is transported to the user through the steam pipeline 27. When the flash tank 12 is over-pressured, the high-pressure steam is discharged from the flash tank 12 through the safety discharge device 16. At the same time, the water supply control valve 14 performs start-stop control and opening adjustment according to the height of the liquid level in the flash tank 12 detected by the liquid level detection device A17. Effective control is adopted to ensure that the liquid level in the flash tank 12 remains stable, avoid fluctuations in steam production, and ensure stable operation of the unit. Example 2
[0023] like Figure 2As shown, the second type of high-efficiency recovery type absorption heat pump of the second specific embodiment of the utility model is based on the first embodiment, an intermediate concentration solution heat recovery heat exchanger 50 is arranged on the intermediate concentration solution pipeline B35, a dilute solution heat recovery heat exchanger 49 is arranged on the dilute solution pipeline B37, the intermediate concentration solution heat recovery heat exchanger 50 and the dilute solution heat recovery heat exchanger 49 are connected via a refrigerant water pipeline J53, the dilute solution heat recovery heat exchanger 49 and the refrigerant water pipeline C40 are connected via a refrigerant water pipeline I51, a refrigerant regulating valve C52 is arranged on the refrigerant water pipeline I51, the intermediate concentration solution heat recovery heat exchanger 50 and the refrigerant water pipeline D41 are connected via a refrigerant water pipeline K54, and the low-temperature refrigerant from the condenser 1 is connected to the refrigerant water pipeline D41. The refrigerant water is respectively sent to the refrigerant heating heat exchanger 9 and the dilute solution heat recovery heat exchanger 49 through the refrigerant liquid delivery pump 11. The low-temperature refrigerant water is heated by the high-temperature refrigerant water from the low-pressure evaporator 3 in the refrigerant heating heat exchanger 9. The low-temperature refrigerant water is heated by the dilute solution in the dilute solution heat recovery heat exchanger 49 to complete a primary heating, recover the overheated heat of the dilute solution, and reduce the flash amount of the dilute solution in the regenerator 2. The refrigerant water flowing out of the dilute solution heat recovery heat exchanger 49 enters the intermediate concentration solution heat recovery heat exchanger 50 through the refrigerant water pipeline J53. The refrigerant water is heated by the intermediate concentration solution in the intermediate concentration solution heat recovery heat exchanger 50 to complete a secondary heating, recover the overheated heat of the intermediate concentration solution, and reduce the flash amount of the intermediate concentration solution in the low-pressure absorber 4. The refrigerant water flowing out of the intermediate concentration solution heat recovery heat exchanger 50 is converged into the refrigerant water pipeline D41 through the refrigerant water pipeline K54. The refrigerant water flowing out of the refrigerant water pipeline D41 is divided into two paths. One path is sent to the low-pressure evaporator 3 through the refrigerant water pipeline E42. The refrigerant water in the low-pressure evaporator 3 absorbs the heat from the heat source water to form refrigerant steam. The refrigerant steam enters the low-pressure absorber 4 through the refrigerant steam channel B29. The other path is sent to the high-pressure evaporator 5 through the refrigerant water pipeline F43 to replenish the refrigerant liquid in the high-pressure evaporator 5. By setting the refrigerant heating heat exchanger 9, the dilute solution heat recovery heat exchanger 49, The intermediate concentration solution heat recovery heat exchanger 50 increases the temperature of the refrigerant water sent to the low-pressure evaporator 3 and the high-pressure evaporator 5, recovers the superheated heat of the solution to heat the refrigerant water, reduces the flash amount of the solution in the regenerator 2 and the low-pressure absorber 4, and adjusts the opening of the refrigerant regulating valve C52 according to the superheat of the intermediate concentration solution flowing out of the high-temperature heat exchanger 8 and the superheat of the dilute solution flowing out of the low-temperature heat exchanger 7, so as to maximize the waste heat recovery, reduce the internal heat exchange loss, realize the efficient use of the heat source water, improve the output quality and output of the steam, improve the heat exchange efficiency of the unit, and avoid energy waste.
[0024] Although the utility model has been described in detail above with general descriptions and specific embodiments, it is obvious to those skilled in the art that some modifications or improvements can be made to the utility model. Therefore, these modifications or improvements made without departing from the spirit of the utility model are within the scope of protection claimed by the utility model.
Claims
1. A high-efficiency recovery type second-class absorption heat pump, characterized in that: The invention comprises a condenser (1), a regenerator (2), a low-pressure evaporator (3), a low-pressure absorber (4), a high-pressure evaporator (5), a high-pressure absorber (6), a low-temperature heat exchanger (7), a high-temperature heat exchanger (8), a refrigerant heating heat exchanger (9), a solution pump (10), a refrigerant liquid delivery pump (11), and a flash tank (12); the condenser (1) and the regenerator (2) are connected via a refrigerant steam channel A (28); the low-pressure evaporator (3) and the low-pressure absorber (4) are connected via a refrigerant steam channel B (29); the low-pressure evaporator (3) and the low-pressure absorber (4) are arranged on the condenser ( 1) and the upper part of the regenerator (2); the high-pressure evaporator (5) and the high-pressure absorber (6) are arranged on the upper part of the low-pressure evaporator (3) and the low-pressure absorber (4); and the flash tank (12) is arranged on the upper part of the high-pressure absorber (6); the condenser (1) is connected to a cooling water inlet pipeline (19) and a cooling water outlet pipeline (20); the low-pressure evaporator (3) is connected to a heat source water inlet pipeline (21) and a heat source water pipeline (22); the regenerator (2) is connected to a heat source water pipeline (22) and a heat source water outlet pipeline (23); and the low-pressure evaporator (3) and the regenerator (2) are connected via the heat source water pipeline (22).
2. A high-efficiency recovery type second-class absorption heat pump according to claim 1, characterized in that: The regenerator (2) and the low-temperature heat exchanger (7) are connected via a concentrated solution pipeline A (31), on which a solution pump (10) is provided. The low-temperature heat exchanger (7) and the high-temperature heat exchanger (8) are connected via a concentrated solution pipeline B (32). The high-temperature heat exchanger (8) and the high-pressure absorber (6) are connected via a concentrated solution pipeline C (33) and an intermediate concentration solution pipeline A (34). The high-temperature heat exchanger (8) and the low-pressure absorber (4) are connected via a concentrated solution pipeline C (33) and an intermediate concentration solution pipeline A (34). The low-pressure absorber (4) and the low-temperature heat exchanger (7) are connected via an intermediate concentration solution pipeline B (35), the low-pressure absorber (4) and the low-temperature heat exchanger (7) are connected via a dilute solution pipeline A (36), the low-temperature heat exchanger (7) and the regenerator (2) are connected via a dilute solution pipeline B (37), no power device is configured between the high-pressure absorber (6), the high-temperature heat exchanger (8) and the low-pressure absorber (4), and no power device is configured between the low-pressure absorber (4), the low-temperature heat exchanger (7) and the regenerator (2).
3. A high-efficiency recovery type second-class absorption heat pump according to claim 2, characterized in that: An intermediate concentration solution heat recovery heat exchanger (50) is provided on the intermediate concentration solution pipeline B (35), a dilute solution heat recovery heat exchanger (49) is provided on the dilute solution pipeline B (37), the intermediate concentration solution heat recovery heat exchanger (50) and the dilute solution heat recovery heat exchanger (49) are connected via a refrigerant water pipeline J (53), the dilute solution heat recovery heat exchanger (49) and the refrigerant water pipeline C (40) are connected via a refrigerant water pipeline I (51), a refrigerant regulating valve C (52) is provided on the refrigerant water pipeline I (51), and the intermediate concentration solution heat recovery heat exchanger (50) and the refrigerant water pipeline D (41) are connected via a refrigerant water pipeline K (54).
4. A high-efficiency recovery type second-class absorption heat pump according to claim 1, characterized in that: The low-pressure absorber (4) and the high-pressure evaporator (5) are connected via a refrigerant water pipeline A (38) and a refrigerant water pipeline B (39). The low-pressure absorber (4) has refrigerant water circulating inside the tube and solution circulating outside the tube. No heat transfer tube is provided inside the high-pressure evaporator (5). The high-pressure evaporator (5) performs heat exchange by flash evaporation of refrigerant water. No power device is provided between the low-pressure absorber (4) and the high-pressure evaporator (5). The condenser (1) and the refrigerant heating heat exchanger (9) are connected via a refrigerant water pipeline C (40) and a refrigerant water pipeline H (47). A refrigerant liquid delivery pump (11) is provided on the refrigerant water pipeline C (40). The refrigerant water pipeline D (41) connected to the refrigerant heating heat exchanger (9) is divided into two paths, one of which is connected to the low-pressure evaporator (3) through the refrigerant water pipeline E (42), and the other is connected to the refrigerant water pipeline A (38) through the refrigerant water pipeline F (43). A refrigerant regulating valve A (44) is provided on the refrigerant water pipeline F (43). The low-pressure evaporator (3) and the refrigerant heating heat exchanger (9) are connected through the refrigerant water pipeline G (46). A refrigerant regulating valve B (48) is provided on the refrigerant water pipeline G (46).
5. The high-efficiency recovery type second-class absorption heat pump according to claim 1, characterized in that: The high-pressure absorber (6) and the flash tank (12) are connected via a hot water circulation pipeline A (24) and a hot water circulation pipeline B (25). No power device is arranged between the high-pressure absorber (6) and the flash tank (12). The water supply pipeline (26) is connected to the hot water circulation pipeline B (25). A water supply control valve (14) is arranged on the water supply pipeline (26). The flash tank (12) is provided with a steam pipeline (27), a pressure sensor (15), a safety discharge device (16), and a liquid level detection device A (17). A steam control valve (13) is arranged on the steam pipeline (27).
6. A high-efficiency recovery type second-class absorption heat pump according to any one of claims 2 to 5, characterized in that: The power device includes a circulation pump, a booster pump or a stepless speed regulator joint.
7. The high-efficiency recovery type second-class absorption heat pump according to claim 1, characterized in that: The low-pressure evaporator (3) and the high-pressure evaporator (5) are provided with a liquid level detection device C (45) and a liquid level detection device B (18) respectively; the condenser (1) and the regenerator (2) are arranged in two cylinders or in one cylinder; the low-pressure evaporator (3) and the low-pressure absorber (4) are arranged in two cylinders or in one cylinder.