A variable-component transcritical mixed working medium refrigeration heat pump system based on adsorption separation

Abstract

The utility model discloses a variable component transcritical mixed working medium refrigeration heat pump system based on adsorption separation, including transcritical circulation structure and adsorption desorption mass transfer process unit, transcritical circulation structure includes the compressor, oil separator, oil return valve, gas cooler, back pressure valve, gas -liquid separator, electronic expansion valve and evaporimeter and second pressure regulating valve and fourth pressure regulating valve that interconnect, and adsorption desorption mass transfer process unit includes the first pressure regulating valve, third pressure regulating valve, fifth pressure regulating valve, sixth regulating valve and adsorption desorption ware that interconnect, gas cooler working medium entrance is connected with gas cooler working medium export through first communicating pipeline and this pipeline has the first coil pipe that winds on the outer surface of adsorption desorption ware, and evaporimeter working medium entrance is connected with evaporimeter working medium export through second communicating pipeline, and this pipeline has the second coil pipe that winds on the outer surface of adsorption desorption ware, the utility model discloses can improve the performance of refrigeration heat pump system significantly.

Description

Technical Field

[0001] This utility model relates to the fields of refrigeration and heating, adsorption refrigeration and heat pump technology, and in particular to a variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation. Background Technology

[0002] Currently, the carbon cycle system is bearing the brunt of the impact, with the balance between carbon sources and sinks being disrupted. The continuous accumulation of carbon in the atmosphere is causing serious climate problems such as global warming and rising sea levels. Currently, building heating, domestic hot water, and industrial and agricultural heating account for more than 30% of my country's total energy consumption. The annual carbon emissions from fossil fuel combustion alone in the industrial sector amount to 2.5 billion tons. Therefore, low-carbon heating in all industries is urgently needed.

[0003] Heat pumps are one of the key technologies for achieving zero-carbon energy systems. Among them, electric-driven heat pumps use electrical energy to efficiently "transfer" low-grade heat sources to high-grade heat sinks, thereby improving the energy quality and enabling large-scale replacement of coal-fired and gas-fired boilers, effectively achieving low-carbon production.

[0004] Carbon dioxide (CO2) as the working fluid has advantages such as zero ODP (Original Temperature Deficit Potential), a GWP (Global Warming Potential) of 1, non-toxicity, non-flammability, and good thermal properties, attracting increasing attention and anticipation. However, if only CO2 is used as the working fluid, there are significant irreversible losses on both the heat source and heat sink sides during the heat exchange process, resulting in lower heat pump performance.

[0005] Therefore, there is an urgent need to develop a technology that can solve the above-mentioned technical problems. Utility Model Content

[0006] The purpose of this invention is to address the technical deficiencies of existing technologies by providing a variable-component transcritical mixed working fluid refrigeration heat pump system and control method based on adsorption separation.

[0007] Therefore, this utility model provides a variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation, including a transcritical cycle structure and an adsorption-desorption mass transfer process unit;

[0008] The transcritical cycle structure includes: a compressor, an oil separator, an oil return valve, a gas cooler, a back pressure valve, a gas-liquid separator, an electronic expansion valve, an evaporator, a second pressure regulating valve, and a fourth pressure regulating valve;

[0009] The working fluid outlet of the evaporator is connected to the working fluid inlet of the compressor via a second pressure regulating valve;

[0010] The compressor's working fluid outlet is connected to the oil separator's working fluid inlet;

[0011] The lubricating oil outlet of the oil separator is connected to one end of the inlet of the return oil valve;

[0012] The working fluid outlet of the oil separator is connected to the working fluid inlet of the gas cooler;

[0013] The other end of the oil return valve is connected to the working fluid inlet of the compressor;

[0014] The working fluid outlet of the gas cooler is connected to one end of the inlet of the back pressure valve;

[0015] The other end of the back pressure valve is connected to the working fluid inlet of the gas-liquid separator;

[0016] The liquid working fluid outlet of the gas-liquid separator is connected to one end of the inlet of the fourth pressure regulating valve;

[0017] The other end of the fourth pressure regulating valve is connected to one end of the electronic expansion valve.

[0018] The other end of the electronic expansion valve is connected to the working fluid inlet of the evaporator.

[0019] The adsorption-desorption mass transfer process unit includes: a first pressure regulating valve, a third pressure regulating valve, a fifth pressure regulating valve, a sixth regulating valve, an adsorption-desorption device, a concentration detector, a first throttle valve, a first check valve, a second throttle valve, and a second check valve.

[0020] In the transcritical cycle structure, the working fluid outlet of the evaporator is connected to the inlet of the third pressure regulating valve;

[0021] The outlet of the third pressure regulating valve is connected to the low-pressure inlet of the desorber, the low-pressure outlet of the desorber is connected to the inlet of the first pressure regulating valve, and the outlet of the first pressure regulating valve is connected to the working fluid inlet of the compressor.

[0022] The gas working fluid outlet of the gas-liquid separator is connected to the inlet of the fifth pressure regulating valve. The outlet of the fifth pressure regulating valve is connected to the high-pressure end inlet of the adsorption-desorption unit. The high-pressure end outlet of the adsorption-desorption unit is connected to the inlet of the sixth pressure regulating valve. The outlet of the sixth pressure regulating valve is connected to the inlet of the electronic expansion valve.

[0023] The working fluid inlet of the gas cooler in the transcritical cycle structure is connected to the working fluid outlet of the gas cooler through a first connecting pipe, and the first connecting pipe has a first coil wound around the outer surface of the adsorber.

[0024] The working fluid inlet of the evaporator in the transcritical cycle structure is connected to the working fluid outlet of the evaporator through a second connecting pipe, and the second connecting pipe has a second coil wound around the outer surface of the adsorber.

[0025] As can be seen from the technical solution provided by this utility model above, compared with the prior art, this utility model provides a variable component transcritical mixed working fluid refrigeration and heat pump system and control method based on adsorption separation. The design is scientific and can significantly improve the performance of the refrigeration and heat pump system, which has great practical significance.

[0026] This invention effectively improves temperature matching for heat transfer during temperature variations by employing a non-azeotropic working fluid. The non-azeotropic transcritical cycle structure of this invention allows for good matching between the supercritical temperature curve and the heat sink by adjusting the compressor's exhaust pressure. Adjusting the cycle components (i.e., the component ratios in the working fluid, such as mass percentage) actively controls the temperature slippage during evaporation to ensure temperature matching on the heat source side. This dual-degree-of-freedom coordinated control of the cycle components and exhaust pressure achieves a balance between source and sink temperature matching.

[0027] By applying this invention, the problems of source-sink temperature matching and component control in conventional heat pumps can be effectively solved. The supercritical exothermic process of the non-azeotropic working fluid replaces the condensation phase change of the non-azeotropic working fluid, thereby avoiding the heat transfer deterioration caused by mass transfer resistance near the gas-liquid interface and improving the heat exchange performance of the heat pump. Attached Figure Description

[0028] Figure 1 The present invention provides a variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation, and a curve showing the relationship between the system COP (coefficient of performance) and the mass fraction of CO2 in the cycle under specific operating conditions.

[0029] Figure 2 A schematic diagram of the structural principle of a variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation provided by this utility model;

[0030] In the diagram: 1. Compressor; 2. Oil separator; 3. Oil return valve; 4. Gas cooler; 5. Back pressure valve;

[0031] 6. Gas-liquid separator; 7. Electronic expansion valve; 8. Evaporator; 9. Concentration detector; 10. First pressure regulating valve;

[0032] 11. Second pressure regulating valve; 12. Third pressure regulating valve;

[0033] 13. First throttle valve; 14. First check valve 1; 15. Second throttle valve; 16. Second check valve; 17. Controller;

[0034] 18. Adsorption / Desorption Unit; 19. Fourth Pressure Regulating Valve; 20. Fifth Pressure Regulating Valve; 21. Sixth Pressure Regulating Valve. Detailed Implementation

[0035] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0036] In the description of this utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this utility model and simplifying the description, and are not intended to indicate or imply that the device or component referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model.

[0037] In the description of this patent, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "setting" should be interpreted broadly. For example, they can refer to a fixed connection or setting, a detachable connection or setting, or an integral connection or setting. Those skilled in the art can understand the specific meaning of the above terms in this patent according to the specific circumstances.

[0038] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this utility model, "a plurality of" means two or more, unless otherwise explicitly specified.

[0039] See Figure 1 , Figure 2 This utility model provides a variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation, including a transcritical cycle structure and an adsorption-desorption mass transfer process unit.

[0040] The transcritical cycle structure includes: compressor 1, oil separator 2, oil return valve 3, gas cooler 4, back pressure valve 5, gas-liquid separator 6, electronic expansion valve 7, evaporator 8, second pressure regulating valve 11, and fourth pressure regulating valve 19.

[0041] The working fluid outlet of the evaporator 8 is connected to the working fluid inlet of the compressor 1 through the second pressure regulating valve 11;

[0042] The working fluid outlet of compressor 1 is connected to the working fluid inlet a of oil separator 2;

[0043] The lubricating oil outlet b of the oil separator 2 is connected to one end of the inlet of the return oil valve 3;

[0044] The working fluid outlet c of oil separator 2 is connected to the working fluid inlet a of gas cooler 4;

[0045] The other end of the oil return valve 3 is connected to the working fluid inlet of the compressor 1;

[0046] The working fluid outlet b of the gas cooler 4 is connected to one end of the inlet of the back pressure valve 5;

[0047] The other end of the back pressure valve 5 is connected to the working fluid inlet a of the gas-liquid separator 6;

[0048] The liquid working fluid outlet b of the gas-liquid separator 6 is connected to one end inlet of the fourth pressure regulating valve 19;

[0049] The other end outlet of the fourth pressure regulating valve 19 is connected to one end inlet of the electronic expansion valve 7;

[0050] The other end outlet of the electronic expansion valve 7 is connected to the working fluid inlet of the evaporator 8;

[0051] It should be noted that, based on the above-mentioned transcritical cycle structure, this invention can complete the transcritical CO2 cycle operation of non-azeotropic mixed working fluids.

[0052] The adsorption-desorption mass transfer process unit (i.e., the pressure swing adsorption cycle unit of the non-azeotropic mixed working fluid) includes: a first pressure regulating valve 10, a third pressure regulating valve 13, a fifth pressure regulating valve 20, a sixth regulating valve 21, an adsorption-desorption device 18, a concentration detector 9, a first throttle valve 13, a first check valve 14, a second throttle valve 15, and a second check valve 16.

[0053] In the transcritical cycle structure, the working fluid outlet b of the evaporator 8 is connected to the inlet of the third pressure regulating valve 12;

[0054] The outlet of the third pressure regulating valve 12 is connected to the low-pressure end inlet b of the desorber 18, the low-pressure end outlet c of the desorber 18 is connected to the inlet of the first pressure regulating valve 10, and the outlet of the first pressure regulating valve 10 is connected to the working fluid inlet of the compressor 1.

[0055] The gas working medium outlet c of the gas-liquid separator 6 is connected to the inlet of the fifth pressure regulating valve 20. The outlet of the fifth pressure regulating valve 20 is connected to the high-pressure end inlet a of the adsorption-desorption unit 18. The high-pressure end outlet d of the adsorption-desorption unit 18 is connected to the inlet of the sixth pressure regulating valve 21. The outlet of the sixth pressure regulating valve 21 is connected to the inlet of the electronic expansion valve 7.

[0056] The working fluid inlet a of the gas cooler 4 in the transcritical cycle structure is connected to the working fluid outlet b of the gas cooler 4 through a first connecting pipe, and the first connecting pipe has a first coil wound around the outer surface of the adsorber 18.

[0057] The working fluid inlet a of the evaporator 8 in the transcritical cycle structure is connected to the working fluid outlet b of the evaporator 8 through a second connecting pipe, and the second connecting pipe has a second coil wound around the outer surface of the adsorber 18.

[0058] It should be noted that, for this utility model, the adsorption-desorption mass transfer process unit is divided into three parts. In the first part, the detection port of the concentration detector 9 is connected to the inlet of the third pressure regulating valve 12, the outlet of the third pressure regulating valve 12 is connected to the low-pressure inlet b of the adsorption-desorption unit 18, the low-pressure outlet c of the adsorption-desorption unit 18 is connected to the inlet of the first pressure regulating valve 10, and the outlet of the first pressure regulating valve 10 is connected to the working fluid inlet of the compressor 1. In the second part, the outlet c of the working fluid separated from the gas-liquid separator 6 is connected to the inlet of the fifth pressure regulating valve 20, and the outlet of the fifth pressure regulating valve 20 is connected to the adsorption-desorption unit 1. The high-pressure end inlet a of 8 is connected, the high-pressure end outlet d of the adsorption-desorption unit 18 is connected to the inlet of the sixth pressure regulating valve 21, and the outlet of the sixth pressure regulating valve 21 is connected to the inlet of the electronic expansion valve 7; in the third part, the working fluid at the inlet of the gas cooler 4 is separated and wound around the surface of the adsorption-desorption unit 18, and after providing the heat required for desorption, it is connected to the working fluid outlet of the gas cooler 4; the working fluid at the inlet of the evaporator 8 is separated and wound around the surface of the adsorption-desorption unit 18, and after absorbing the heat generated by adsorption, it is connected to the working fluid outlet of the evaporator 8.

[0059] It should be noted that, based on the structural design of the adsorption-desorption mass transfer process unit described above, the pressure swing adsorption cycle operation of the non-azeotropic mixed working fluid can be completed.

[0060] In this invention, specifically, the first coil in the first connecting pipe and the second coil in the second connecting pipe are spaced apart and do not contact each other.

[0061] In this utility model, specifically, the first coil in the first connecting pipe is provided with a first throttle valve 13 and a first check valve 14 in sequence on the connecting pipe between the first coil and the working fluid outlet b of the gas cooler 4.

[0062] In the second connecting pipe, the second coil is connected to the working fluid outlet b of the evaporator 8 by a second throttle valve 15 and a second check valve 16.

[0063] In this utility model, specifically, a concentration detector 9 is installed on the connecting pipe between the working fluid outlet of the evaporator 8 and the working fluid inlet of the compressor 1;

[0064] It should be noted that, in practice, the detection port of the concentration detector 9 is also connected to the inlet of the third pressure regulating valve 12.

[0065] In this utility model, specifically, the mixed working fluid heat pump system also includes a controller 17;

[0066] The controller 17 is communicatively connected to the signal control terminals of the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21, respectively, and is used to control the opening and closing states of the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 by sending control signals.

[0067] In practice, the controller 17 can be a programmable logic controller (PLC), a central processing unit (CPU), a digital signal processor (DSP), or a microcontroller (MCU).

[0068] In this invention, in specific implementation, any two interconnected devices that transfer working fluids or other substances to each other are connected by a hollow connecting pipe.

[0069] In this invention, specifically, the working fluid used in the variable component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation is a non-azeotropic mixed working fluid.

[0070] In practice, the non-azeotropic working fluid includes two components: an organic working fluid with low GWP (global warming potential) and carbon dioxide (CO2).

[0071] For example, in a non-azeotropic mixture, the mass fraction of the organic working fluid with low GWP (global warming potential) can be 0.1 (i.e., 10% by mass), and the mass fraction of carbon dioxide (CO2) can be 0.9 (i.e., 90% by mass). Among these, the preferred organic working fluid with low GWP is R1234ze(E).

[0072] It should be noted that, for this utility model, the non-azeotropic mixture of the two components, low-GWP organic working fluid and carbon dioxide (CO2), can reduce the transcritical CO2 cycle exhaust pressure and throttling loss.

[0073] It should be noted that, in this utility model, in specific implementation, the low-grade heat source can be shallow geothermal energy (referring to the heat energy in the constant temperature layer tens to hundreds of meters below the surface, such as the heat in groundwater, surface water and underground soil), industrial waste heat energy (such as industrial hot wastewater), and domestic waste heat energy (including the cold and heat resources contained in domestic sewage).

[0074] In practice, a delivery pump can be installed on the pipeline of the low-grade heat source to generate pressure and realize the directional delivery of the medium (such as water or air). (For example, when the medium being delivered is gas, the delivery pump can be an air pump; when the medium being delivered is liquid, it can be a liquid pump.)

[0075] In the specific implementation of this utility model, combined with Figure 2 As shown, the hot end of the evaporator 8 is provided with two inlets and outlets, namely inlet c and outlet d. The connection method of the evaporator 8 can include two types: circulating and direct flow.

[0076] 1. When the evaporator 8 adopts a circulating connection method, specifically: both the circulating inlet c and the circulating outlet d are connected to a low-grade heat source. The hot end inlet c of the circulating system is connected to one end of the conveying pipeline of the low-grade heat source located outside. Its function is to introduce the external low-grade heat source medium (such as hot groundwater) into the evaporator 8 to provide heat for the refrigerant in the evaporator 8 which is in a low-temperature state. The hot end outlet d is connected to one end of the heat source circulation pipeline inside the building envelope (such as a building). Its function is to export the heat source medium after heat exchange to provide cooling supply to the building envelope (such as a building).

[0077] It should be noted that the building envelope refers to the walls, doors, windows, etc. that enclose the building space and can effectively resist the impact of adverse environments.

[0078] 2. When the evaporator 8 adopts a direct-flow connection, specifically: the direct-flow inlet c is connected to a low-grade heat source, and its function is to introduce the external low-grade heat source medium into the evaporator 8 to provide heat for the refrigerant in the evaporator 8 at a low temperature; one end (i.e., the inner end) of the hot end outlet d is connected to the heat exchange area of ​​the evaporator 8, and the other end (i.e., the outer end) of the hot end outlet d can be directly connected to the external environment (such as the atmosphere) or to the interior of the enclosure structure. After cooling the interior of the enclosure structure, it flows out from the enclosure structure and is discharged into the atmosphere; after heat exchange in the evaporator 8, the heat source medium with a reduced temperature is discharged through the hot end outlet d, and this low-temperature medium can be directly used to provide cooling for the space inside the enclosure structure; at this time, the heat source medium is of the type that does not need to be recovered (such as air), and the discharge process does not require an additional recovery treatment device, and can be directly discharged into the environment to complete the final treatment of the medium circulation.

[0079] Therefore, in this invention, when the evaporator 8 adopts a circulating connection method, the corresponding circulating low-grade heat source (e.g., groundwater) can be reinjected into the groundwater after cooling the building envelope, thus allowing for reuse. However, when the evaporator 8 adopts a direct-flow connection method, the corresponding direct-flow low-grade heat source (e.g., air) can be directly discharged into the atmosphere after cooling the building envelope, as low-grade heat sources like air are very common and do not require recycling. It should be noted that air contains low-grade heat energy.

[0080] In the specific implementation of this utility model, combined with Figure 2 As shown, see Figure 2 As shown, the cold end of the gas cooler 4 is provided with two inlets and outlets, namely the cold end inlet c and the cold end outlet d. The connection method of the gas cooler 4 can include two types: circulation type and direct flow type.

[0081] 1. When the gas cooler 4 adopts a circulating connection method, specifically: the circulating inlet c and outlet d are respectively connected to the two ends of the medium circulation pipeline in the heat user end. The medium in the heat user end exchanges heat with the refrigerant through the gas cooler 4, causing the refrigerant to cool down and the medium in the heat user end to heat up. The heated medium in the heat user end is connected to the heat user end through the cold end outlet d of the gas cooler 4 to provide heat to the heat user end. After being used in the heat user end and having lost heat, the low-temperature circulating medium re-enters the gas cooler 4 from the cold end inlet c through the circulation pipeline in the heat user end to repeatedly participate in the heat exchange process of the refrigerant in the gas cooler 4.

[0082] It should be noted that, in this context, the heat user end can be a building that requires heat, and the medium for heat use can be water. This water is located in a circulating pipeline within the building, and this circulating pipeline can be equipped with a liquid pump to generate pressure and achieve directional transportation of the medium (e.g., water). For example, in a heating system, the radiators in a residential home and the areas covered by the air conditioning vents in the room, as well as the area covered by the air conditioning vents in an office building, are all considered heat users. In an industrial waste heat recovery system, production process equipment that needs to utilize waste heat for heating can also be considered a heat user end.

[0083] 2. When the gas cooler 4 uses a direct-flow connection, specifically: the direct-flow inlet c is connected to one end of an external heat sink (such as a tap water pipe). The heat sink exchanges heat with the refrigerant through the gas cooler 4, causing the refrigerant to cool down and the heat sink working medium (such as tap water) to heat up. The heated heat sink working medium is then connected to the heat user end through the outlet d of the gas cooler 4 (in this case, the heat user end can be a water pipe; for example, the outlet d of the gas cooler 4 is connected to one end of a water pipe, and the other end of the water pipe is equipped with a faucet), providing heat to the heat user. For example, in a heating system, the radiators in a residential home and the area covered by the air conditioning vents in the room, as well as the area covered by the air conditioning vents in an office building, are all considered heat users; in an industrial waste heat utilization system, production equipment that needs to utilize waste heat for heating can also be considered heat users.

[0084] To better understand the technical solution of this utility model, the roles of the main components in the refrigeration cycle are described below:

[0085] Compressor 1: Used to compress the low-pressure gaseous working fluid into the oil, thereby increasing its pressure and temperature to form a high-temperature and high-pressure gaseous working fluid, which is then delivered to the oil separator 2.

[0086] Oil separator 2: Used to process the high-temperature and high-pressure gaseous working fluid from compressor 1, separating the lubricating oil carried in it, and allowing the high-temperature and high-pressure working fluid to be transported to gas cooler 4, so as to prevent the lubricating oil from entering the subsequent circulation and affecting the heat exchange effect. The separated lubricating oil can be returned to compressor 1 through oil return valve 3, etc., to ensure compressor lubrication.

[0087] Oil return valve 3: Used to control the return path of lubricating oil separated from oil separator 2, sending the lubricating oil back to compressor 1 to ensure normal operation.

[0088] Gas cooler 4: Used to receive high-temperature and high-pressure gaseous working fluid from oil separator 2, cool it down by exchanging heat with heat sink, and turn it into low-temperature and low-pressure working fluid, and then deliver it to back pressure valve 5.

[0089] Back pressure valve 5: Used to maintain a suitable pressure on the gas cooler side, after which the working fluid is delivered to the gas-liquid separator 6.

[0090] Gas-liquid separator 6: Used to separate the incoming working fluid into liquid and gaseous working fluids. The liquid working fluid enters the electronic expansion valve 7, while the gaseous working fluid is prevented from entering the electronic expansion valve 7, which would affect the throttling effect.

[0091] Electronic expansion valve 7: used to regulate the flow rate and throttling pressure of the liquid working fluid from the gas-liquid separator 6, regulate the superheat of the evaporator, and deliver the working fluid to the evaporator 8.

[0092] Evaporator 8: Used to exchange heat between the low-pressure, low-temperature gas-liquid mixture working fluid from the electronic expansion valve 7 and a low-grade heat source (such as groundwater as a low-grade heat source). The working fluid absorbs heat, evaporates, and is converted into a low-pressure gaseous state, which is then delivered to the compressor 1.

[0093] Concentration detector 9: Used to detect the mass fraction of the working fluid in the circulation process during the transport of the mixed working fluid from the evaporator 8 to the compressor 1, and transmits the detection signal to the controller 17 to provide a basis for the controller to adjust the system operation.

[0094] First pressure regulating valve 10, second pressure regulating valve 11, third pressure regulating valve 12, fourth pressure regulating valve 19, fifth pressure regulating valve 20, and sixth pressure regulating valve 21: are used to regulate the working fluid pressure in their respective branches according to the system pressure requirements, maintain a specific pressure range, and allow the fluid with regulated pressure to be delivered to adjacent compatible components.

[0095] First throttle valve 13 and second throttle valve 15: used to throttle and reduce the pressure of the working fluid, allowing the fluid to be delivered to subsequent components at a lower pressure.

[0096] First check valve 14 and second check valve 16: used to control the unidirectional flow of fluid, prevent backflow, and maintain circulation sequence and stability.

[0097] Controller 17: Used to receive signals from concentration detector 9, and send control commands to each pressure regulating valve according to preset programs and system operating parameters, and coordinate the operation of each component of the refrigeration cycle.

[0098] Adsorption-desorption unit 18: Used for adsorption or desorption processes to change the mass fraction of the working fluid in the cycle.

[0099] In this invention, a mixed working fluid composed of a low-GWP organic working fluid and a natural working fluid CO2 is used to reduce the throttling loss in the transcritical CO2 refrigeration cycle. A concentration detector monitors component deviations, and a pressure regulating valve is used to change the pressure of the adsorber / desorber. The CO2 mass fraction is adjusted by the selective adsorption or desorption of the working fluid components by the adsorbent. Source and sink temperatures are matched and balanced through dual-degree-of-freedom coordinated control of the circulating components and exhaust pressure (i.e., the component ratio in the mixed working fluid and the compressor exhaust pressure). Supercritical heat release prevents heat transfer deterioration. Simultaneously, two sets of coils are wound around the surface of the adsorber / desorber 18. One coil (the second coil) uses the low-temperature working fluid from the evaporator 8 inlet. During adsorption, the working fluid in the coil absorbs the adsorption heat generated by the adsorption in the adsorber / desorber, accelerating the adsorption rate. The other coil (the first coil) uses the high-temperature working fluid from the gas cooler 4 inlet. During desorption, the working fluid in the coil releases heat, providing the necessary heat for desorption and accelerating the desorption rate.

[0100] Based on the adsorption-separation-based variable component transcritical mixed refrigerant refrigeration and heat pump system provided by this utility model, this utility model also provides a control method for the adsorption-separation-based variable component transcritical mixed refrigerant refrigeration and heat pump system, including the following operating modes:

[0101] Step S1: Perform transcritical CO2 cycle operation of non-azeotropic working fluid;

[0102] Step S1 is specifically as follows: The low-temperature, low-pressure non-azeotropic working fluid flowing out of the working fluid outlet of the evaporator 8 is drawn into the compressor 1 and compressed to a high-temperature, high-pressure non-azeotropic working fluid. Then it enters the oil separator 2, where the oil carried by the non-azeotropic working fluid is separated and returned to the compressor 1 through the oil return valve 3. At the same time, the non-azeotropic working fluid enters the gas cooler 4 to exchange heat with the heat exchange fluid, which provides heat to the heat user. The non-azeotropic working fluid then flows through the back pressure valve 5 to maintain the pressure on the high-pressure side of the system. Then, the working fluid achieves gas-liquid separation in the gas-liquid separator 6. After the working fluid flows through the electronic expansion valve 7 for throttling and pressure reduction, it evaporates and absorbs heat in the evaporator 8, completing the transcritical CO2 cycle operation of the non-azeotropic working fluid.

[0103] In step S1, specifically, the non-azeotropic working fluid of the system consists of R1234ze(E) and CO2.

[0104] In step S1, specifically, in the above process, the non-azeotropic working fluid preferably includes CO2 with a mass fraction of 0.9 and R1234ze(E) with a mass fraction of 0.1.

[0105] Step S2: Perform a pressure swing adsorption cycle operation on a non-azeotropic working fluid;

[0106] Step S2 specifically involves monitoring the actual circulating mass fraction C of CO2 in the non-azeotropic mixture flowing out of the evaporator 8 using a concentration detector 9. cir (i.e., actual concentration);

[0107] At a certain moment, the optimal circulating mass fraction C of CO2 is... opt The actual circulating mass fraction of CO2 at this time, C cir Deviation between |C cir -C opt | has reached (i.e., is greater than or equal to) the preset allowable deviation ε. C Then, according to C opt With C cirThe numerical values ​​of the two valves are used to perform corresponding preset adjustments on the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21. At this time, the previous operating cycle stops, and the next operating cycle begins.

[0108] For example, in step S2, the mass fraction (i.e., concentration) of CO2 in the non-azeotropic mixture flowing out of the evaporator 8 is monitored in real time by the concentration detector 9. The deviation |C| between the optimal circulating mass fraction of CO2 (0.91) and the actual circulating mass fraction of CO2 (0.9) at a certain moment is found. cir -C opt |

[0109] =0.01, |C cir -C opt The preset allowable deviation of 0.01 has been reached (i.e., greater than or equal to). At this point, the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 need to be adjusted accordingly.

[0110] In step S2, specifically, the actual circulating mass fraction C of CO2 can be directly detected and obtained in the non-azeotropic working fluid using the concentration detector 9. cir .

[0111] In this invention, specifically, the optimal circulating mass fraction C of CO2 is... opt It is the mass fraction of circulating CO2 when the system COP (coefficient of performance) reaches its maximum value (i.e., the optimal value of system COP).

[0112] It should be noted that, as Figure 1 As shown, it is a curve showing the relationship between the system's COP (coefficient of performance) and the mass fraction of CO2 in the cycle under specific operating conditions. The specific operating parameters are: heat source side inlet temperature: 20℃, heat source side outlet temperature: 10℃, heat sink side inlet temperature: 40℃, heat sink side outlet temperature: 65℃, and exhaust pressure: 9.75Mpa.

[0113] Depend on Figure 1 The curve trend shows the relationship between the system COP and the mass fraction of circulating CO2 under the above operating conditions. Figure 1 It can be seen that the system's COP first increases and then decreases with the increase of the circulating CO2 mass fraction. Therefore, there exists a circulating CO2 mass fraction that maximizes the system's COP. This CO2 mass fraction is defined as the optimal circulating mass fraction C. opt The circulating CO2 mass fraction compared to the optimal circulating mass fraction C optThe deviation can fluctuate within a certain range without significantly affecting the system's COP; this range is defined as the preset allowable deviation ε. C The optimal cycle quality fraction C at this point. opt A circulating CO2 mass fraction of 0.92 corresponds to a system COP (i.e., the optimal system COP) of 3.25. When the circulating CO2 mass fraction fluctuates to 0.91 or 0.93, the system COP is 3.215 or 3.205, respectively, relative to the optimal circulating mass fraction C. opt The COP decreased by a maximum of 1.4% at that time, which was not significant.

[0114] In specific implementation, the controller 17 is used to perform corresponding opening or closing control operations on the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20 and the sixth pressure regulating valve 21.

[0115] In specific implementation, the controller 17 is communicatively connected to the concentration detector 9, and is used to collect the actual circulating mass fraction C of CO2 in the non-azeotropic mixture flowing out of the working fluid outlet of the evaporator 8 through the concentration detector 9. cir (i.e., actual concentration), and at a certain moment, the optimal circulating mass fraction C of CO2. opt The actual circulating mass fraction of CO2 at this time, C cir Deviation between |C cir -C opt |, and the preset allowable deviation ε C A comparison is made, and if the preset allowable deviation ε has been reached (i.e., greater than or equal to), the result is considered. C Then, according to C opt With C cir The numerical values ​​of the two valves are used to perform corresponding preset adjustment operations on the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 (specifically, corresponding opening or closing control operations, the specific control methods are described below).

[0116] In step S2, specifically, the adsorbent used in the adsorbent-desorber 11 is solid activated carbon with a porosity of 0.37.

[0117] In step S2, specifically, the detection interval of the concentration detector 9 is 1 minute, that is, it detects once every 1 minute.

[0118] In step S2, specifically, according to C opt With C cirBased on the numerical values ​​of the two valves, corresponding preset adjustment operations are performed on the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21. Specifically, these operations include the following:

[0119] If C cir <C opt Then, the first pressure regulating valve 10, the third pressure regulating valve 12, and the fourth pressure regulating valve 19 open, while the second pressure regulating valve 11, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 close. The pressure in the adsorbent-desorber 18 decreases. Simultaneously, the first coil on the gas cooler 4 side operates, and the working fluid in the first coil provides the heat required for desorption, accelerating the desorption rate. All the working fluids in the heat pump cycle are desorbed by the adsorbent in the adsorbent-desorber 18. However, because the change in CO2 desorption is greater than (specifically, significantly greater than) that of another non-azeotropic working fluid in the non-azeotropic mixture, the actual circulating mass fraction of CO2, C, is lower. cir Increase until |C is satisfied. cir -C opt |<ε C At this time, the second pressure regulating valve 11 and the fourth pressure regulating valve 19 are opened, and the first pressure regulating valve 10, the third pressure regulating valve 12, the fifth pressure regulating valve 20 and the sixth pressure regulating valve 21 are closed, and the regulation is terminated.

[0120] If C cir >C opt Then, the second pressure regulating valve 11, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 open, while the first pressure regulating valve 10, the third pressure regulating valve 12, and the fourth pressure regulating valve 19 close, causing the pressure in the adsorption-desorption unit 18 to increase. Simultaneously, the second coil on the evaporator 8 side operates, and the working fluid in the second coil absorbs the adsorption heat generated by adsorption, accelerating the adsorption rate. All the working fluids in the heat pump cycle are desorbed by the adsorbent in the adsorption-desorption unit 18. However, because the change in CO2 desorption is greater than (specifically, significantly greater than) that of another non-azeotropic working fluid in the non-azeotropic mixture, the actual circulating mass fraction of CO2, C, is lower. cir Decrease until |C cir -C opt |<ε C At this time, the second pressure regulating valve 11 and the fourth pressure regulating valve 19 are opened, and the first pressure regulating valve 10, the third pressure regulating valve 12, the fifth pressure regulating valve 20 and the sixth pressure regulating valve 21 are closed, and the regulation is terminated.

[0121] It should be noted that, for this utility model, after the above-mentioned preset adjustment operation, the heat pump can operate stably under the new circulation component ratio (i.e., the new mass fraction ratio of the two working substances in the mixed working fluid). When the mass fraction (i.e., concentration) of CO2 in the non-azeotropic mixed working fluid is monitored by the concentration detector 9 and deviation analysis is performed, |C] reappears. cir -C opt |>ε C If the pressure swing adsorption cycle ends, the current cycle is terminated, and the next cycle is started again by the action of multiple pressure regulating valves to ensure continuous control of the circulating components. This process is repeated to complete the pressure swing adsorption cycle of the non-azeotropic working fluid.

[0122] In specific implementation, another preferred non-azeotropic working fluid in the non-azeotropic mixture is R1234ze(E).

[0123] In terms of specific implementation, the concentration detector 9 is a carbon dioxide concentration detector.

[0124] To better understand the technical solution of this utility model, the working principle of this utility model will be explained below with reference to the embodiments.

[0125] Example

[0126] In the embodiments, the non-azeotropic working fluid specifically includes CO2 with a mass fraction of 0.9 and R1234ze(E) with a mass fraction of 0.1.

[0127] This utility model provides a control method for a variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation, including the following operating modes:

[0128] Step S1: Perform transcritical CO2 cycle operation of non-azeotropic working fluid;

[0129] Step S1 is specifically as follows: The low-temperature, low-pressure non-azeotropic working fluid flowing out of the working fluid outlet of the evaporator 8 is drawn into the compressor 1 and compressed to a high-temperature, high-pressure non-azeotropic working fluid. Then it enters the oil separator 2, where the oil carried by the non-azeotropic working fluid is separated and returned to the compressor 1 through the oil return valve 3. At the same time, the non-azeotropic working fluid enters the gas cooler 4 to exchange heat with the heat exchange fluid, which provides heat to the heat user. The non-azeotropic working fluid then flows through the back pressure valve 5 to maintain the pressure on the high-pressure side of the system. Then, the working fluid achieves gas-liquid separation in the gas-liquid separator 6. After the working fluid flows through the electronic expansion valve 7 for throttling and pressure reduction, it evaporates and absorbs heat in the evaporator 8, completing the transcritical CO2 cycle operation of the non-azeotropic working fluid.

[0130] In step S1, specifically, in heating mode, the heat source can be groundwater and the heat sink can be the heat user end; in cooling mode, the heat source can be the building envelope and the heat sink can be industrial wastewater. The operating temperature range of the gas cooler 4 is 10 to 140°C, the evaporation temperature range of the evaporator 8 is -40 to 10°C, the suction pressure range of the compressor 1 is 1 to 4 MPa, and the discharge pressure range is 6 to 13 MPa.

[0131] In step S1, specifically, when the evaporator 8 exchanges heat with the external fluid, the narrow temperature difference range is 3 to 5°C, and the fluid superheat range at the working fluid outlet of the evaporator 8 is 2 to 5°C.

[0132] The inlet water temperature range of the heat source is 20 to 40℃, and the outlet water temperature range is -5 to 15℃.

[0133] In step S1, specifically, the water supply temperature range of the gas cooler 4 is 8 to 18°C, and the water return temperature range of the gas cooler 4 is 45 to 65°C.

[0134] For gas cooler 4, for every 1°C increase in the supply water temperature on the heat sink side, the return water temperature increases by 2°C.

[0135] Step S2: Perform a pressure swing adsorption cycle operation on a non-azeotropic working fluid;

[0136] Step S2 specifically involves monitoring the actual circulating mass fraction C of CO2 in the non-azeotropic mixture flowing out of the evaporator 8 using a concentration detector 9. cir (i.e., actual concentration);

[0137] When the optimal circulating mass fraction C of CO2 is at a certain moment opt (Specifically equal to 0.91) and the actual circulating mass fraction of CO2 at this time, C cir The deviation between (specifically equal to 0.9) and |C cir -C opt | equals 0.01, reaching (i.e., greater than or equal to) the preset allowable deviation ε C When (specifically equal to 0.01), corresponding preset adjustment operations are performed on the first pressure regulating valve 10, the second pressure regulating valve 11, the third pressure regulating valve 12, the fourth pressure regulating valve 19, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21. Because C cir <C optSpecifically, the first pressure regulating valve 10, the third pressure regulating valve 12, and the fourth pressure regulating valve 19 are opened, while the second pressure regulating valve 11, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 are closed. This reduces the pressure in the adsorbent-desorber 18. Simultaneously, the first coil on the gas cooler 4 side operates, and the working fluid in the first coil provides the heat required for desorption, accelerating the desorption rate. The non-azeotropic working fluid composed of R1234ze(E) and CO2 circulating in the heat pump is desorbed by the adsorbent in the adsorbent-desorber 18. However, because the change in CO2 desorption is greater than (specifically, significantly greater than) that of R1234ze(E), the actual circulating mass fraction C of CO2 decreases. cir Increase until |C is satisfied. cir -C opt When |<0.01, the second pressure regulating valve 11 and the fourth pressure regulating valve 19 are opened, and the first pressure regulating valve 10, the third pressure regulating valve 12, the fifth pressure regulating valve 20 and the sixth pressure regulating valve 21 are closed, and the regulation is terminated.

[0138] In the above process, the adsorbent used in the adsorption-desorption device 11 is solid activated carbon with a porosity of 0.37; the detection interval of the concentration detector 9 is 1 minute, that is, it is detected once every 1 minute.

[0139] Then, after a period of operation, during which the actual circulating mass fraction C of CO2 flowing out of the working fluid outlet of evaporator 8 was monitored by concentration detector 9, the same method was used. cir (i.e., actual concentration), to find the optimal circulating mass fraction C of CO2 at a certain moment. opt (Specifically equal to 0.9) and the actual circulating mass fraction of CO2 at this time, C cir The deviation (specifically equal to 0.91) is 0.01, which meets the preset allowable deviation of 0.01. At this point, corresponding preset adjustment operations need to be performed on the first pressure regulating valve 10 and the second pressure regulating valve 12, because C cir >C opt Specifically, the second pressure regulating valve 11, the fifth pressure regulating valve 20, and the sixth pressure regulating valve 21 are opened, while the first pressure regulating valve 10, the third pressure regulating valve 12, and the fourth pressure regulating valve 19 are closed, causing the pressure in the adsorbent-desorber 18 to increase. Simultaneously, the second coil on the evaporator 8 side operates, and the working fluid in the second coil absorbs the adsorption heat generated by adsorption, accelerating the adsorption rate. The non-azeotropic working fluid composed of R1234ze(E) and CO2 circulating in the heat pump is desorbed by the adsorbent in the adsorbent-desorber 18. However, because the change in CO2 desorption is greater than (specifically, significantly greater than) that of R1234ze(E), the actual circulating mass fraction of CO2, C, is lower. cir Decrease until |C cir -C opt |<ε CAt this time, the second pressure regulating valve 11 and the fourth pressure regulating valve 19 are opened, and the first pressure regulating valve 10, the third pressure regulating valve 12, the fifth pressure regulating valve 20 and the sixth pressure regulating valve 21 are closed, and the regulation is terminated.

[0140] At this point, the heat pump can operate stably under the new circulation ratio (i.e., the new mass fraction ratio of the two working fluids in the mixed working fluid). When the mass fraction (i.e., concentration) of CO2 in the non-azeotropic mixed working fluid is monitored by the concentration detector 9 and deviation analysis is performed, |C| reappears. cir -C opt If the value is greater than 0.01, the current operating cycle terminates, and the next cycle is initiated by the action of multiple pressure regulating valves to ensure continuous control of the circulating components. This process is repeated to complete the pressure swing adsorption cycle operation of the non-azeotropic working fluid.

[0141] Compared with existing technologies, the variable-component transcritical mixed working fluid refrigeration and heat pump system based on adsorption separation provided by this utility model has the following beneficial effects:

[0142] 1. In order to solve the problems of source-sink temperature matching and component control in conventional heat pumps, an adsorption-desorption device is added to a conventional CO2 mixed working fluid heat pump. The pressure is controlled by the regulating valve to achieve pressurization or depressurization. The working fluid components undergo selective adsorption / desorption in the adsorbent, and the adsorption amount changes with the pressure.

[0143] 2. Compared with traditional transcritical working fluid cycles, the non-azeotropic mixed working fluid transcritical cycle operation adopted in this invention can not only ensure the matching of source and sink temperatures, but also avoid the deterioration of heat transfer due to phase change in the heat release process through supercritical heat exchange without phase change, thus significantly improving the performance of the heat pump cycle.

[0144] 3. In this utility model, the working fluid of the non-azeotropic mixed working fluid transcritical CO2 cycle is a non-azeotropic mixed working fluid composed of low GWP organic working fluid and CO2, which can reduce the exhaust pressure and throttling loss of the transcritical CO2 cycle, and will not decompose under high temperature conditions. It is safe, non-toxic, and environmentally friendly.

[0145] 4. The CO2 mixed working fluid transcritical cycle operation of this utility model has a large high and low pressure difference, short adsorption or desorption equilibrium time, fast response, and can quickly adjust the cycle components.

[0146] 5. In this utility model, by integrating the adsorption-desorption device with the main circuit of the heat pump, the system uses its own pressure difference to drive adsorption or desorption, without the need for an additional heat source or complex separation equipment. The structure is compact, with only compressor power consumption and no additional separation energy consumption, resulting in high overall system energy efficiency.

[0147] 6. In this utility model, two sets of coils are wound around the surface of the adsorption-desorption device. One set of coils (i.e., the second coil) uses the low-temperature working fluid from the inlet of the evaporator. During the adsorption process, the working fluid in the coil absorbs the adsorption heat generated by the adsorption of the working fluid in the adsorption-desorption device, thereby accelerating the adsorption rate in the adsorption-desorption device. The other set of coils (i.e., the first coil) uses the high-temperature working fluid from the inlet of the gas cooler. During the desorption process, the working fluid in the coil releases heat, providing the required heat for desorption and accelerating the desorption rate in the adsorption-desorption device.

[0148] 7. By applying this utility model, the limitations of gas-liquid phase equilibrium can be overcome, homogeneous separation can be achieved through pressure swing adsorption, the circulating components can be flexibly adjusted according to the working conditions, and the applicable heat source temperature range and heat sink temperature range are significantly broadened.

[0149] The above description is only a preferred embodiment of the present utility model. It should be noted that for those skilled in the art, several improvements and modifications can be made without departing from the principle of the present utility model, and these improvements and modifications should also be considered within the protection scope of the present utility model.

Claims

1. A variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation, characterized in that, Includes transcritical cycle structures and adsorption / desorption mass transfer process units; The transcritical cycle structure includes: a compressor (1), an oil separator (2), an oil return valve (3), a gas cooler (4), a back pressure valve (5), a gas-liquid separator (6), an electronic expansion valve (7), an evaporator (8), a second pressure regulating valve (11), and a fourth pressure regulating valve (19). The working fluid outlet of the evaporator (8) is connected to the working fluid inlet of the compressor (1) through the second pressure regulating valve (11); The working fluid outlet of the compressor (1) is connected to the working fluid inlet a of the oil separator (2); The lubricating oil outlet b of the oil separator (2) is connected to one end of the inlet of the return oil valve (3); The working fluid outlet c of the oil separator (2) is connected to the working fluid inlet a of the gas cooler (4); The other end of the oil return valve (3) is connected to the working fluid inlet of the compressor (1); The working fluid outlet b of the gas cooler (4) is connected to one end of the inlet of the back pressure valve (5); The other end outlet of the back pressure valve (5) is connected to the working fluid inlet a of the gas-liquid separator (6); The liquid working fluid outlet b of the gas-liquid separator (6) is connected to one end inlet of the fourth pressure regulating valve (19); The other end outlet of the fourth pressure regulating valve (19) is connected to one end inlet of the electronic expansion valve (7); The other end outlet of the electronic expansion valve (7) is connected to the working fluid inlet of the evaporator (8); The adsorption-desorption mass transfer process unit includes: a first pressure regulating valve (10), a third pressure regulating valve (13), a fifth pressure regulating valve (20), a sixth regulating valve (21), an adsorption-desorption device (18), a concentration detector (9), a first throttle valve (13), a first check valve (14), a second throttle valve (15), and a second check valve (16). The working fluid outlet b of the evaporator (8) in the transcritical cycle structure is connected to the inlet of the third pressure regulating valve (12); The outlet of the third pressure regulating valve (12) is connected to the low-pressure end inlet b of the desorber (18), the low-pressure end outlet c of the desorber (18) is connected to the inlet of the first pressure regulating valve (10), and the outlet of the first pressure regulating valve (10) is connected to the working fluid inlet of the compressor (1). The gas working medium outlet c of the gas-liquid separator (6) is connected to the inlet of the fifth pressure regulating valve (20), the outlet of the fifth pressure regulating valve (20) is connected to the high pressure end inlet a of the adsorption-desorption device (18), the high pressure end outlet d of the adsorption-desorption device (18) is connected to the inlet of the sixth pressure regulating valve (21), and the outlet of the sixth pressure regulating valve (21) is connected to the inlet of the electronic expansion valve (7). The working fluid inlet a of the gas cooler (4) in the transcritical cycle structure is connected to the working fluid outlet b of the gas cooler (4) through a first connecting pipe, and the first connecting pipe has a first coil wrapped around the outer surface of the adsorber (18). The working fluid inlet a of the evaporator (8) in the transcritical cycle structure is connected to the working fluid outlet b of the evaporator (8) through a second connecting pipe, and the second connecting pipe has a second coil wrapped around the outer surface of the adsorber (18).

2. The variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation as described in claim 1, characterized in that, The first coil in the first connecting pipe and the second coil in the second connecting pipe are distributed alternately.

3. The variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation as described in claim 1, characterized in that, The first coil in the first connecting pipeline is provided with a first throttle valve (13) and a first check valve (14) in sequence on the connecting pipeline between the first coil and the working fluid outlet b of the gas cooler (4). The second coil in the second connecting pipe is provided with a second throttle valve (15) and a second check valve (16) in sequence on the connecting pipe between the working fluid outlet b of the evaporator (8).

4. The variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation as described in claim 1, characterized in that, A concentration detector (9) is installed on the connecting pipe between the working fluid outlet of the evaporator (8) and the working fluid inlet of the compressor (1). The detection port of the concentration detector (9) is also connected to the inlet of the third pressure regulating valve (12).

5. The variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation as described in any one of claims 1 to 4, characterized in that, It also includes a controller (17); The controller (17) is connected to the signal control terminals of the first pressure regulating valve (10), the second pressure regulating valve (11), the third pressure regulating valve (12), the fourth pressure regulating valve (19), the fifth pressure regulating valve (20), and the sixth pressure regulating valve (21) respectively, and is used to control the opening and closing states of the first pressure regulating valve (10), the second pressure regulating valve (11), the third pressure regulating valve (12), the fourth pressure regulating valve (19), the fifth pressure regulating valve (20), and the sixth pressure regulating valve (21) by sending control signals.

6. The variable-component transcritical mixed working fluid refrigeration heat pump system based on adsorption separation as described in claim 1, characterized in that, Non-azeotropic working fluids, consisting of two components: low-GWP organic working fluids and carbon dioxide (CO2); The low GWP organic working fluid is R1234ze(E).

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