Absorption heat pump device system driven by double-temperature-level waste heat and operation method of absorption heat pump device system

Abstract

The invention provides an absorption heat pump device system driven by double-temperature-level waste heat and an operation method of the absorption heat pump device system. The absorption heat pump device system comprises a reboiling device, a condensing device, a first evaporation device, a second evaporation device and an absorption device which are sequentially connected. The reboiling device is respectively connected with the first heat source input pipeline and the first heat source output pipeline; the first evaporation device is respectively connected with a first heat source input pipeline and a first heat source output pipeline; and the second evaporation device is respectively connected with the second heat source input pipeline and the second heat source output pipeline. The energy grade is improved through the heat pump technology, and a heat source 30 DEG C higher than medium-temperature waste heat is generated for a user to use; and different temperatures of the waste heat source are matched by adjusting the pressure of different evaporation devices, # imgabs0 # loss in the waste heat recovery process is reduced, and the system is suitable for large-scale application and popularization.

Description

Technical Field

[0001] The present invention relates to the technical field of heat pumps, and in particular to a dual-temperature waste heat driven absorption heat pump device system and an operation method thereof. Background Art

[0002] In situations where there are two heat sources, such as flue gas and cooling water in industrial systems, since flue gas generally contains sensible heat, the total amount of heat it carries is limited, while cooling water contains more heat but its temperature is lower. Using a type I heat pump for recovery often requires additional heat source or energy input, while using a type II absorption heat pump is limited by its operating range.

[0003] For waste heat of 40-60℃, although the quality can be improved by using a type I absorption heat pump and a vapor compression heat pump, it requires high-quality heat or electricity to drive. If a type II absorption heat pump is used, the evaporation pressure is low due to the low temperature of the heat source, so the single-stage temperature rise of the system is difficult to exceed 30℃. Although the two-stage cascade system can achieve a larger temperature rise, the series connection of multiple heat pump units for heat extraction will undoubtedly increase the complexity of the system and the investment cost.

[0004] Compression absorption is the current mainstream solution, which is to add a set of compressors downstream of the evaporator, and increase the steam pressure through electric drive, thereby increasing the absorption temperature. However, this method essentially increases the enthalpy of the steam upstream of the absorber through electric energy, thereby obtaining a higher absorption temperature. The performance coefficient of the second-class absorption heat pump is generally less than 1, so the heat increment brought by this part of the added electric energy is often less than the power consumption. In situations where the price ratio of electric energy to heat energy is high, this method cannot bring economic benefits.

[0005] CN108050731A discloses a flue gas driven waste heat recovery type absorption heat pump. The absorption heat pump is mainly composed of a generator, a condenser, a solution heat exchanger, an absorber and an evaporator. The flue gas first enters the generator, contacts the internal falling film heat transfer tube in the generator during its flow to release heat, and then enters the evaporator, contacts the internal falling film heat transfer tube in the evaporator, and leaves the absorption heat pump after releasing heat again. The absorption heat pump is driven by flue gas and realizes flue gas waste heat recovery at the same time. Since the evaporation temperature of the absorption heat pump is relatively low, the flue gas can be reduced to a lower temperature, thereby improving the energy utilization efficiency of various energy systems that generate flue gas. In addition, the absorption heat pump can reduce the flue gas temperature to below the dew point temperature, condense the water vapor in the flue gas, recover the condensation heat of the water vapor, and the generated condensed water can wash and purify the flue gas, thereby achieving the dual effects of energy saving and reducing pollutant emissions.

[0006] CN108397836A discloses an absorption heat pump device driven by recycling waste heat and compressing steam, which includes a waste heat recovery system, a steam compression system, and an absorption heat pump system. The waste heat is used to supply working water for low-pressure flash evaporation, and the steam compressor recompresses the steam to drive the absorption heat pump device, thereby achieving the dual effects of waste heat recovery and building air conditioning. The absorption heat pump system driven by industrial waste heat recovery is used for building air conditioning to achieve winter heating and summer cooling, which can not only meet people's comfort requirements, but also realize the comprehensive utilization of industrial waste heat and reduce environmental pollution during the heating season, effectively recovering industrial waste heat, improving energy utilization efficiency, and avoiding the environmental pollution caused by the current coal-fired heating.

[0007] CN104359103A discloses a flue gas waste heat recovery system with an absorption heat pump cycle, comprising a gas boiler, an air preheater and an absorption heat pump device, wherein the absorption heat pump device comprises an evaporator, a condenser, a throttling mechanism, an absorber, a solution pump, a generator and a throttling valve, wherein the absorber, the solution pump, the generator and the throttling valve are sequentially connected to form a loop, wherein the generator is sequentially connected to the condenser, the throttling mechanism, the evaporator, and finally connected to the absorber; the evaporator is provided with a discharge pipe for discharging flue gas and condensed water, the condenser is provided with a boiler low-temperature water supply channel and a boiler high-temperature water supply channel, and the boiler high-temperature water supply channel is connected to the gas boiler; the gas boiler is provided with a high-temperature flue gas channel and a steam branch channel.

[0008] However, the above heat pump system still has problems such as high power consumption and low quality of the generated heat source. Summary of the invention

[0009] In view of the problems existing in the prior art, the present invention provides an absorption heat pump device system driven by dual-temperature waste heat and an operation method thereof, which integrates the advantages of two types of heat pumps, namely, two-stage evaporation and compression absorption, and extracts heat from medium and low temperature waste heat sources, thereby reducing the power consumption of the entire device system and obtaining a high-temperature heat source that is 30°C higher than the medium-temperature waste heat for users to use; the device system solves the problem of limited output heat load of the heat pump system due to the limited total amount of medium-temperature waste heat.

[0010] To achieve this object, the present invention adopts the following technical solutions:

[0011] In a first aspect, the present invention provides a dual-temperature waste heat driven absorption heat pump system, the absorption heat pump system comprising a reboiling device, a condensing device, a first evaporating device, a second evaporating device and an absorbing device connected in sequence; the reboiling device is respectively connected to a first heat source input pipeline and a first heat source output pipeline;

[0012] The first evaporation device is connected to the first heat source input pipeline and the first heat source output pipeline respectively;

[0013] The second evaporation device is connected to the second heat source input pipeline and the second heat source output pipeline respectively.

[0014] The dual-temperature waste heat driven absorption heat pump device system of the present invention is aimed at occasions where low-temperature waste heat of 40-60°C and medium-temperature waste heat of >100°C are contained and the total amount of medium-temperature waste heat is limited. The heat pump technology is used to improve the energy quality and generate a heat source that is 30°C higher than the medium-temperature waste heat for users to use.

[0015] The dual-temperature waste heat driven absorption heat pump system of the present invention comprises a first evaporation device and a second evaporation device. The pressure of the evaporation devices at different levels is adjusted by multi-stage evaporation to match different waste heat source temperatures, thereby reducing the waste heat recovery process. The gas-liquid separation device in the absorption heat pump device system separates the gas-liquid two-phase working medium produced in the first evaporation device, and the gas phase is pressurized and enthalpy increased by the compression device, and the liquid phase is pressurized by the second solution pump and enthalpy increased by the medium-temperature waste heat.

[0016] In the present invention, the number of the first evaporation devices can be increased according to different temperatures and heat sources on site during actual application, so as to achieve the highest possible waste heat recovery rate.

[0017] Preferably, the absorption heat pump system further includes a distillation device.

[0018] Preferably, the distillation device is arranged between the reboiler and the condenser.

[0019] Preferably, the distillation device is cyclically connected to the reboiler.

[0020] Preferably, the absorption heat pump system further comprises a gas-liquid separation device, a gas compression device and a steam mixing device;

[0021] Wherein, the gas-liquid separation device is arranged between the first evaporation device and the second evaporation device, the gas phase outlet of the gas-liquid separation device is connected to the gas compression device, and the liquid phase outlet is connected to the second evaporation device;

[0022] The steam mixing device is arranged between the second evaporation device and the absorption device, and the outlet of the gas compression device and the outlet of the second evaporation device are connected to the inlet of the steam mixing device;

[0023] The outlet of the steam mixing device is connected to the inlet of the absorption device.

[0024] Preferably, a first solution pump is provided between the condensing device and the first evaporating device.

[0025] Preferably, a second solution pump is provided between the gas-liquid separation device and the second evaporation device.

[0026] Preferably, the absorption device is connected to the heat exchange medium input pipeline and the heat exchange medium output pipeline respectively.

[0027] Preferably, the absorption heat pump device system further comprises a heat exchange device, the outlet of the reboiler device is connected to the heat source inlet of the heat exchange device, and the heat source outlet of the heat exchange device is connected to the absorption device;

[0028] The outlet of the absorption device is connected to the cold source inlet of the heat exchange device, and the cold source outlet of the heat exchange device is connected to the inlet of the distillation device.

[0029] The evaporation temperature of the first evaporation device of the present invention is 5-10° C. lower than that of the low-temperature heat source, and the load of the first evaporation device is designed to ensure that the dryness of the outlet working medium steam is appropriate.

[0030] The evaporation temperature of the second evaporation device of the present invention is 5 to 10° C. lower than that of the medium-temperature heat source.

[0031] Preferably, a throttle valve is further provided between the heat exchange device and the distillation device.

[0032] The present invention does not limit the type of heat exchange medium, and any heat exchange medium available in the art that can take away the heat of the mixed steam entering the absorption device can be used.

[0033] In a second aspect, the present invention further provides an operating method of the dual-temperature waste heat driven absorption heat pump system as described in the first aspect, the operating method comprising:

[0034] The working fluid absorbs the heat of the first heat source in the reboiling device and becomes steam, then enters the condensing device to condense into liquid working fluid, enters the first evaporating device to absorb the heat of the first heat source and becomes a gas-liquid two-phase working fluid; the gas-liquid two-phase working fluid enters the second evaporating device to absorb the heat of the second heat source and completely evaporates into a second gas-phase working fluid; the second gas-phase working fluid enters the absorption device to release heat. The operation method of the dual-temperature waste heat driven absorption heat pump device system of the present invention is simple to operate, and through multiple heat exchanges, the waste heat of the low-temperature heat source and the medium-temperature heat source can be fully absorbed and utilized, and the waste heat in the waste heat recovery process is reduced. The heat of the absorption heat pump system of the present invention is output to the outside through the heat exchange medium passing through the heat exchange device.

[0035] The working fluid of the present invention can be ammonia water or lithium bromide water and other commonly used heat exchange working fluids in the art.

[0036] Preferably, the operation method also includes: the gas-liquid two-phase working fluid enters the gas-liquid separation device for separation, the vapor enters the gas compression device for pressurization and becomes the first gas-phase working fluid; the first gas-phase working fluid and the second gas-phase working fluid are mixed in the steam mixing device to become mixed steam; the mixed steam enters the absorption device to release heat; thereafter, enters the heat exchange device to exchange heat with the first solution output from the reboiler and then returns to the reboiler, and the first solution after heat exchange enters the absorption device.

[0037] Preferably, when the working fluid is ammonia water, the ammonia water absorbs heat from the first heat source in the reboiler to become steam and then enters the distillation device and then enters the condensation device for condensation; the solution of ammonia water after distillation in the distillation device returns to the reboiler; and the mixed steam releases heat through the absorption device, enters the heat exchange device, exchanges heat with the first solution output from the reboiler, and then returns to the distillation device, and the first solution after heat exchange enters the absorption device.

[0038] After the reboiling device of the present invention evaporates the working fluid, a dilute solution of the working fluid will be produced at the bottom; the mixed steam in the absorption device will become a concentrated solution of the working fluid after heat exchange, and the concentrated solution will return to the distillation device or the reboiling device through the heat exchange device and can be recycled.

[0039] Preferably, the temperature of the first heat source is 40-60°C, for example, it can be 40°C, 43°C, 45°C, 50°C, 55°C, 58°C or 60°C, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0040] Preferably, the temperature of the second heat source is >100°C, for example, it can be 101°C, 105°C, 110°C, 115°C, 120°C, 125°C or 130°C, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0041] Preferably, the temperature of the heat exchange medium is higher than the temperature of the second heat source by more than 30°C, for example, it may be 30°C, 35°C, 40°C, 45°C, 50°C, 55°C or 60°C, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0042] As a preferred technical solution of the present invention, the operating method includes:

[0043] The working fluid absorbs heat from the first heat source in the reboiling device and becomes steam, then enters the condensing device to condense into a liquid working fluid, and enters the first evaporating device to absorb heat from the first heat source to become a gas-liquid two-phase working fluid; the gas-liquid two-phase working fluid enters the gas-liquid separation device for separation, the steam enters the gas compression device for pressurization and becomes the first gas-phase working fluid, and the liquid enters the second evaporating device to absorb heat from the second heat source and completely evaporates to become the second gas-phase working fluid; the first gas-phase working fluid and the second gas-phase working fluid are mixed in the steam mixing device to become mixed steam; the mixed steam returns to the reboiling device after releasing heat to the heat exchange medium via the absorption device;

[0044] After the mixed steam releases heat through the absorption device, it enters the heat exchange device to exchange heat with the first solution output from the reboiler and then returns to the reboiler. The first solution after heat exchange enters the absorption device.

[0045] When the working fluid is ammonia water, the ammonia water absorbs the heat of the first heat source in the reboiling device and becomes steam, then enters the distillation device and then enters the condensation device for condensation; the solution of the ammonia water after distillation in the distillation device returns to the reboiling device; and the mixed steam releases heat in the absorption device, enters the heat exchange device, exchanges heat with the first solution output from the reboiling device, and then returns to the distillation device, and the first solution after heat exchange enters the absorption device;

[0046] The temperature of the first heat source is 40-60° C.; the temperature of the second heat source is >100° C.; the temperature of the heat exchange medium is higher than the temperature of the second heat source by more than 30° C.

[0047] Compared with the prior art, the present invention has at least the following beneficial effects:

[0048] (1) The dual-temperature waste heat-driven absorption heat pump device system provided by the present invention improves the energy quality through heat pump technology, and generates a heat source that is 30°C higher than the medium-temperature waste heat for users to use;

[0049] (2) The dual-temperature waste heat driven absorption heat pump device system provided by the present invention uses the first evaporator and the second evaporator to adjust the pressure of different levels of evaporators to match different waste heat source temperatures, thereby reducing the waste heat recovery process. Loss, suitable for large-scale promotion and application. BRIEF DESCRIPTION OF THE DRAWINGS

[0050] Figure 1 It is a schematic structural diagram of the absorption heat pump device system driven by dual-temperature waste heat in Example 1 of the present invention.

[0051] In the figure: 1-reboiling device; 2-distillation device; 3-condensing device; 4-first solution pump; 5-first evaporation device; 6-gas-liquid separation device; 7-gas compression device; 8-steam mixing device; 9-second solution pump; 10-second evaporation device; 11-absorption device; 12-heat exchange device; 13-throttle valve; 14-third solution pump. DETAILED DESCRIPTION

[0052] The technical solution of the present invention is further described below with reference to the accompanying drawings and through specific implementation methods.

[0053] The present invention is further described in detail below. However, the following examples are only simplified examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims.

[0054] It should be understood that, in the description of the present invention, the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present invention, unless otherwise specified, "multiple" means two or more.

[0055] It should be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "disposed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0056] Those skilled in the art should understand that the present invention necessarily includes necessary pipelines, conventional valves and general pump equipment for realizing a complete process, but the above content does not belong to the main inventive point of the present invention. Those skilled in the art can add layouts on their own based on the process flow and equipment structure selection, and the present invention does not make special requirements and specific limitations on this.

[0057] Example 1

[0058] This embodiment provides a dual-temperature waste heat driven absorption heat pump system, and its structural schematic diagram is as follows: Figure 1 shown.

[0059] The absorption heat pump device system comprises a reboiling device 1, a condensing device 3, a first evaporating device 5, a second evaporating device 10 and an absorbing device 11 connected in sequence;

[0060] The reboiler 1 is connected to the first heat source input pipeline and the first heat source output pipeline respectively;

[0061] The first evaporation device 5 is connected to the first heat source input pipeline and the first heat source output pipeline respectively;

[0062] The second evaporation device 10 is connected to the second heat source input pipeline and the second heat source output pipeline respectively.

[0063] The absorption heat pump device system also includes a distillation device 2;

[0064] The distillation device 2 is arranged between the reboiler 1 and the condenser 3;

[0065] The distillation device 2 is cyclically connected to the reboiler 1 .

[0066] The absorption heat pump device system also includes a gas-liquid separation device 6, a gas compression device 7 and a steam mixing device 8;

[0067] The gas-liquid separation device 6 is disposed between the first evaporation device 5 and the second evaporation device 10, the gas phase outlet of the gas-liquid separation device 6 is connected to the gas compression device 7, and the liquid phase outlet is connected to the second evaporation device 10;

[0068] The steam mixing device 8 is arranged between the second evaporation device 10 and the absorption device 11, and the outlet of the gas compression device 7 and the outlet of the second evaporation device 10 are connected to the inlet of the steam mixing device 8;

[0069] The outlet of the steam mixing device 8 is connected to the inlet of the absorption device 11 .

[0070] A first solution pump 4 is provided between the condensing device 3 and the first evaporating device 5;

[0071] A second solution pump 9 is provided between the gas-liquid separation device 6 and the second evaporation device 8;

[0072] The absorption device 11 is connected to the heat exchange medium input pipeline and the heat exchange medium output pipeline respectively.

[0073] The absorption heat pump device system further comprises a heat exchange device 12, the outlet of the reboiler 1 is connected to the heat source inlet of the heat exchange device 12, and the heat source outlet of the heat exchange device 12 is connected to the absorption device 11;

[0074] The outlet of the absorption device 11 is connected to the cold source inlet of the heat exchange device 12 , and the cold source outlet of the heat exchange device 12 is connected to the inlet of the distillation device 2 .

[0075] A throttle valve 13 is also provided between the heat exchange device 12 and the distillation device 2 .

[0076] This embodiment also provides an operation method of the above-mentioned dual-temperature waste heat driven absorption heat pump device system, wherein the working fluid used is ammonia water; the operation method comprises:

[0077] After the ammonia water absorbs the heat of the first heat source with a temperature of 50°C in the reboiling device 1 and becomes ammonia vapor, it first enters the distillation device 2 and then enters the condensing device 3 to condense into a liquid working medium. After being pressurized by the first solution pump 4, it enters the first evaporation device 5 to absorb the heat of the first heat source and become a gas-liquid two-phase working medium. The gas-liquid two-phase working medium enters the gas-liquid separation device 6 for separation, and the vapor enters the gas compression device 7 for pressurization to become the first gas phase working medium. The liquid enters the second evaporation device 10 to absorb the second heat source with a temperature of 110°C after being pressurized by the second solution pump 9. The heat of the second heat source is completely evaporated into a second gaseous working fluid; the first gaseous working fluid and the second gaseous working fluid are mixed in the steam mixing device 8 to become mixed steam; after the mixed steam releases heat to the heat exchange medium water through the absorption device 11, it enters the heat exchange device 12 and exchanges heat with the dilute ammonia solution pressurized by the third solution pump 14 from the reboiling device 1, and then returns to the distillation device 2 through the throttle valve 13, and the dilute ammonia solution after heat exchange enters the absorption device 11; the ammonia solution after distillation in the distillation device 2 returns to the reboiling device 1.

[0078] Example 2

[0079] The present embodiment provides an absorption heat pump device system driven by waste heat at two temperature levels. The absorption heat pump device system is the same as that of Embodiment 1 except that the distillation device 2 is not provided, the reboiler 1 is directly connected to the condenser 3, and the heat exchange device 12 is directly connected to the reboiler 1.

[0080] This embodiment also provides an operation method of the above-mentioned dual-temperature waste heat driven absorption heat pump device system, wherein the working fluid used is lithium bromide water; the operation method comprises:

[0081] The lithium bromide water absorbs the heat of the first heat source with a temperature of 60°C in the reboiling device 1 and becomes steam, and then enters the condensing device 3 to condense into a liquid working fluid. After being pressurized by the first solution pump 4, it enters the first evaporating device 5 to absorb the heat of the first heat source and become a gas-liquid two-phase working fluid; the gas-liquid two-phase working fluid enters the gas-liquid separation device 6 for separation, the steam enters the gas compression device 7 for pressurization and becomes the first gas-phase working fluid, and the liquid enters the second evaporating device 10 to absorb the heat of the second heat source with a temperature of 120°C after being pressurized by the second solution pump 9 and completely evaporates into the second gas-phase working fluid; the first gas-phase working fluid and the second gas-phase working fluid are mixed in the steam mixing device 8 to become mixed steam; the mixed steam releases heat through the absorption device 11 and enters the heat exchange device 12 to exchange heat with the dilute lithium bromide water solution pressurized and transported from the reboiling device 1 by the third solution pump 14, and then returns to the reboiling device 1, and the dilute lithium bromide water solution after heat exchange enters the absorption device 11.

[0082] In summary, the dual-temperature waste heat driven absorption heat pump device system provided by the present invention reduces the power consumption of the entire device system and obtains high-quality high-temperature heat sources for users by extracting heat from medium and low temperature waste heat sources.

[0083] The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above-mentioned embodiments, but the present invention is not limited to the above-mentioned detailed structural features, that is, it does not mean that the present invention must rely on the above-mentioned detailed structural features to be implemented. Those skilled in the art should understand that any improvement of the present invention, equivalent replacement of the components selected by the present invention, addition of auxiliary components, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

[0084] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, a variety of simple modifications can be made to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.

Claims

1. A dual-temperature waste heat driven absorption heat pump system, characterized in that: The absorption heat pump device system comprises a reboiling device, a condensing device, a first evaporating device, a second evaporating device and an absorbing device connected in sequence; The reboiler is connected to the first heat source input pipeline and the first heat source output pipeline respectively; The first evaporation device is connected to the first heat source input pipeline and the first heat source output pipeline respectively; The second evaporation device is connected to the second heat source input pipeline and the second heat source output pipeline respectively.

2. The absorption heat pump system according to claim 1, characterized in that: The absorption heat pump device system also includes a distillation device; The rectification device is arranged between the reboiling device and the condensing device; The distillation device is cyclically connected with the reboiler.

3. The absorption heat pump system according to claim 1 or 2, characterized in that: The absorption heat pump device system also includes a gas-liquid separation device, a gas compression device and a steam mixing device; Wherein, the gas-liquid separation device is arranged between the first evaporation device and the second evaporation device, the gas phase outlet of the gas-liquid separation device is connected to the gas compression device, and the liquid phase outlet is connected to the second evaporation device; The steam mixing device is arranged between the second evaporation device and the absorption device, and the outlet of the gas compression device and the outlet of the second evaporation device are connected to the inlet of the steam mixing device; The outlet of the steam mixing device is connected to the inlet of the absorption device.

4. The absorption heat pump system according to any one of claims 1 to 3, characterized in that: A first solution pump is provided between the condensing device and the first evaporating device; A second solution pump is provided between the gas-liquid separation device and the second evaporation device; The absorption device is connected to the heat exchange medium input pipeline and the heat exchange medium output pipeline respectively.

5. The absorption heat pump system according to any one of claims 1 to 4, characterized in that: The absorption heat pump device system also includes a heat exchange device, the outlet of the reboiler device is connected to the heat source inlet of the heat exchange device, and the heat source outlet of the heat exchange device is connected to the absorption device; The outlet of the absorption device is connected to the cold source inlet of the heat exchange device, and the cold source outlet of the heat exchange device is connected to the inlet of the distillation device.

6. The absorption heat pump system according to any one of claims 1 to 5, characterized in that: A throttle valve is also arranged between the heat exchange device and the distillation device.

7. An operating method of a dual-temperature waste heat driven absorption heat pump system according to any one of claims 1 to 6, characterized in that: The operation method comprises: The working fluid absorbs heat from the first heat source in the reboiler to become steam, then enters the condenser to be condensed into liquid working fluid, enters the first evaporator to absorb heat from the first heat source to become gas-liquid two-phase working fluid; the gas-liquid two-phase working fluid enters the second evaporator to absorb heat from the second heat source to be completely evaporated into a second gas-phase working fluid; the second gas-phase working fluid enters the absorption device to release heat.

8. The operating method according to claim 7, characterized in that: The operation method also includes: the gas-liquid two-phase working medium enters the gas-liquid separation device for separation, the vapor enters the gas compression device for pressurization, and becomes the first gas-phase working medium; the first gas-phase working medium and the second gas-phase working medium are mixed in the steam mixing device to become mixed steam; the mixed steam enters the absorption device to release heat; thereafter, enters the heat exchange device to exchange heat with the first solution output from the reboiler and then returns to the reboiler, and the first solution after heat exchange enters the absorption device.

9. The operating method according to claim 8, characterized in that: When the working fluid is ammonia water, the ammonia water absorbs the heat of the first heat source in the reboiler to become steam, and then enters the distillation device and then enters the condensation device for condensation; the solution of the ammonia water after distillation in the distillation device returns to the reboiler; and the mixed steam releases heat through the absorption device, enters the heat exchange device, exchanges heat with the first solution output from the reboiler, and then returns to the distillation device, and the first solution after heat exchange enters the absorption device.

10. The operating method according to any one of claims 7 to 9, characterized in that: The temperature of the first heat source is 40-60°C; The temperature of the second heat source is >100°C; The temperature of the heat exchange medium is higher than the temperature of the second heat source by more than 30°C.

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