CN211060434U - Injection supercharging two-stage supercooling transcritical CO2Dual temperature system - Google Patents
Injection supercharging two-stage supercooling transcritical CO2Dual temperature system Download PDFInfo
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Abstract
The utility model provides an injection pressure boost doublestage subcools transcritical CO2The dual-temperature system comprises an ejector supercharging dual-subcooler series mechanical subcooling circulation and transcritical CO which can exchange heat with each other2Circulating in a double-temperature area; the trans-critical CO2Two temperature zone cycle comprising CO2Low temperature stage steamingA hair pin; CO 22The outlets of the low-temperature evaporator are sequentially communicated with CO2Low pressure stage compressor, CO2Medium pressure stage compressor, CO2High pressure stage compressor, CO2Heat medium side of gas cooler, heat medium side of intermediate temperature stage cooling evaporator, heat medium side of low temperature stage cooling evaporator, intermediate temperature stage gas-liquid separator, low temperature stage gas-liquid separator and CO2The inlet of the low temperature stage evaporator. Injection pressure double stage supercooling transcritical CO2Dual temperature system to reduce compressor discharge pressure, CO2The pressure ratio of the compressor is reduced, the isentropic efficiency is improved, and the service life of the compressor is prolonged.
Description
Technical Field
The utility model belongs to the technical field of refrigeration and heating, heat pump, especially, relate to an it crosses critical CO to draw pressure boost doublestage subcooling2A dual temperature system.
Background
Nowadays, energy is increasingly in short supply and environmental problems are more prominent, and a feasible energy-saving and environment-friendly mode is sought in the whole society. Meanwhile, new technologies and new products with excellent performance, low price and stable operation are continuously emerging. In the aspect of energy consumption, the refrigeration air-conditioning building has a large proportion, is a large user for electricity in the building, and needs to explore a novel energy-saving refrigeration heat pump technology. For civil and commercial applications, the demand for cooling and heating in multiple temperature zones is increasing dramatically. At present, the requirements of different temperature areas are mainly met through two or more refrigeration (heat pump) devices, so that energy waste and environmental damage are caused to a great extent. Meanwhile, most of the filled refrigerants of the equipment are HFCs high GWP working media.
CO2Compared with the traditional technology, the refrigeration technology is more efficient, more energy-saving and more environment-friendly. Carbon dioxide is known as a permanent substitute with the most development potential of CFCs, HCFCs and HFCs by virtue of its excellent characteristics. Therefore, the green carbon dioxide refrigeration technology has wide development prospect. However, due to CO2The lower critical temperature (31.1 ℃) and the higher critical pressure (7.38MPa) cause the large throttle irreversible loss and the lower refrigeration efficiency, and the transcritical CO is subjected to vapor compression refrigeration circulation2CO at the outlet of the gas cooler of the refrigeration cycle2The method of cooling is known as mechanical subcooling. The throttling loss is reduced by increasing the supercooling degree, the circulating cold quantity is increased, and the CO is reduced2The high pressure of the circulation operation and the exhaust pressure of the compressor prolong the service life of the compressor and improve the COP of the circulation.
The gas-liquid two-phase fluid throttled by the conventional refrigeration system directly enters an evaporator or throttled by a gas-liquid separator and then enters a compressor for further compression, the gas-phase working medium does not participate in evaporation and heat absorption, and does not contribute to the refrigeration process, and the heat exchange effect of a heat exchanger is deteriorated or the power consumption of the compressor is increased due to the conventional treatment mode. The utility model discloses provide feasible solution to above problem.
Disclosure of Invention
In view of this, the utility model aims at providing an inject pressure boost doublestage subcools and stride critical CO2A dual temperature system to overcome the disadvantages of the prior art and reduce the discharge pressure, CO, of the compressor2The pressure ratio of the compressor is reduced, the isentropic efficiency is improved, and the service life of the compressor is prolonged.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
injection supercharging two-stage supercooling transcritical CO2The dual-temperature system comprises an ejector supercharging dual-subcooler series mechanical subcooling circulation and transcritical CO which can exchange heat with each other2Circulating in a double-temperature area;
the trans-critical CO2Two temperature zone cycle comprising CO2A low temperature stage evaporator; the CO is2The outlets of the low-temperature evaporator are sequentially communicated with CO2Low pressure stage compressor, CO2Medium pressure stage compressor, CO2High pressure stage compressor, CO2Heat medium side of gas cooler, heat medium side of intermediate temperature stage cooling evaporator, heat medium side of low temperature stage cooling evaporator, intermediate temperature stage gas-liquid separator, low temperature stage gas-liquid separator and CO2An inlet of a low temperature stage evaporator; the gas outlet of the medium-temperature stage gas-liquid separator is communicated with CO2Secondary flow inlet of ejector, CO2Main flow inlet and CO of ejector2Outlet of high pressure stage compressor connected to CO2Exit of ejector and CO2The inlets of the high-pressure stage compressors are communicated; the liquid outlet of the medium-temperature stage gas-liquid separator is also communicated with CO2The inlets of the intermediate temperature stage evaporators are communicated with each other, and CO2Inlet of intermediate temperature stage evaporator and CO2The inlets of the medium-pressure stage compressors are communicated; the air outlets of the low-temperature stage gas-liquid separator are sequentially communicated with CO2Low pressure stage parallel compressor and CO2An inlet of the intermediate-pressure stage compressor.
Furthermore, the ejector supercharging double-subcooler series mechanical subcooling cycle comprises an ejector, wherein an outlet of the ejector is sequentially communicated with a refrigerant side of the medium-temperature-stage cooling evaporator, an inlet of a common working medium compressor and an inlet of a heat medium side of the condenser; and an outlet pipeline on the heat medium side of the condenser is divided into two paths, one path is communicated with a main flow inlet of the ejector, and the other path is sequentially communicated with a refrigerant side of the low-temperature-level cooling evaporator and a secondary flow inlet of the ejector.
Further, said CO2A low-temperature evaporator fan is arranged below the low-temperature evaporator; the CO is2And a medium-temperature-stage evaporator fan is arranged below the medium-temperature-stage evaporator.
Furthermore, a second throttle valve is arranged on a connecting pipeline between a heat medium outlet of the low-temperature stage cooling evaporator and the medium-temperature stage gas-liquid separator; and a first throttle valve is arranged on a connecting pipeline between the liquid outlet of the medium-temperature stage gas-liquid separator and the liquid inlet of the low-temperature stage gas-liquid separator.
Further, said CO2Low temperature stage evaporator, CO2The medium-temperature-stage evaporator, the medium-temperature-stage cooling evaporator and the low-temperature-stage cooling evaporator respectively adopt a finned tube heat exchanger, a double-tube heat exchanger or a plate heat exchanger, and a double-tube heat exchanger or a plate heat exchanger; the CO is2The gas cooler is a double-pipe heat exchanger or a plate heat exchanger.
Further, trans-critical CO2The heat exchange fluid circulated in the two temperature zones is CO2；CO2The secondary flow of the ejector has the air suction temperature ranging from-10 ℃ to 10 ℃, the pressure ranging from 2.65 MPa to 4.50MPa, the main flow temperature ranging from 80 ℃ to 140 ℃, the pressure ranging from 7.5 MPa to 14MPa, the ejector outlet temperature ranging from 40 ℃ to 50 ℃ and the pressure ranging from 5MPa to 6 MPa.
Further, said CO2Low temperature stage evaporator, CO2The working temperature ranges of the medium-temperature-level evaporator, the medium-temperature-level cooling evaporator and the low-temperature-level cooling evaporator are-56 to-20 ℃, 10 to 10 ℃, 10 to 40 ℃ and 10 to 20 ℃ respectively; CO 22The suction pressure range of the low-pressure stage compressor is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa; CO 22The suction pressure range of the medium-pressure stage compressor is 2.65-4.50 MPa, and the exhaust pressure range is 5-6 MPa; CO 22The suction pressure range of the high-pressure stage compressor is 5-6 MPa, and the exhaust pressure isThe range is 7.5-14 MPa; CO 22The suction pressure range of the low-pressure stage parallel compressor is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa.
Furthermore, the heat exchange working medium of the ejector supercharging double subcooler series mechanical subcooling cycle is pure refrigerant or non-azeotropic mixed working medium.
Preferably, the pure refrigerant may be one of R1234ze (Z), R1234ze (E), R1233zd (E), R1224yd (Z), R1336mzz (Z), R365mfc, R1234yf, R245fa, and the like, and preferably is R1234 yf.
Preferably, the non-azeotropic mixed working medium is CO2/R1234ze(E)、CO2/R1234ze(Z)、CO2One of substances such as/R1234 yf, R41/R1234ze (E), R41/R1234ze (Z), R41/R1234yf, R32/R1234ze (E), R32/R1234ze (Z), R32/R1234yf and the like, preferably R32/R1234 zeZ.
Further, the condenser is a double-pipe heat exchanger or a plate heat exchanger.
Further, the injection supercharging two-stage supercooling transcritical CO2The dual temperature system also comprises a third throttle valve arranged on a pipeline between the outlet of the heat medium side of the condenser and the inlet of the refrigerant of the low-temperature stage cooling evaporator.
Preferably, the suction temperature range of the ordinary working medium middle-temperature stage compressor (7) is 20-50 ℃, and the exhaust temperature range is 70-120 ℃.
Preferably, the refrigerant side of the condenser and the CO2The refrigerant side of the gas cooler is respectively communicated with a heat exchange fluid source.
The utility model discloses still relate to as above draw and penetrate pressure boost doublestage subcooling and cross critical CO2The double-temperature system is applied to the fields of refrigeration and heating and heat pumps.
Compared with the prior art, the utility model relates to an inject pressure boost doublestage subcooling and stride critical CO2The dual temperature system has the following advantages:
(1) the gas-liquid phase fluid is separated by a medium-temperature stage gas-liquid separator and a low-temperature stage gas-liquid separator and flows into CO2The fluid of the intermediate-temperature and low-temperature stage evaporator is liquid fluid, the fluid is uniformly distributed in each parallel pipeline of the finned tube heat exchanger, and the heat exchange coefficient is increased, so thatThe heat exchange efficiency of the evaporator is high, the size of the evaporator can be reduced on the premise of the same heat exchange quantity, and the evaporator can be more compact and improve the space utilization rate of refrigeration equipment when used in a supermarket freezer cabinet and a refrigeration cabinet.
(2) By CO2Low-temperature-stage parallel compressor for compressing gas-phase fluid in low-temperature-stage gas-liquid separator to CO separately2Compared with the traditional throttle-first recompression process, the same exhaust pressure of the low-temperature stage compressor omits the throttle process, thereby reducing the throttle irreversible loss of the gas and CO2Compared with the prior throttling recompression process, the compression ratio of the parallel compressor is improved, the suction pressure is increased, the compression ratio is reduced, and CO is reduced2The efficiency of the parallel compressor is high.
(3) By CO2CO at the outlet of the high-pressure stage compressor2The fluid is to lead the gas-phase fluid of the medium-temperature stage gas-liquid separator to be in CO2The ejector injects the gas to the intermediate pressure, the configuration of throttling and pressure reduction of a throttle valve or pressure boosting of compressor power equipment can be omitted, the saturated gas which does not participate in refrigeration is injected to the inlet of the compressor on the premise of greatly reducing throttling loss and not introducing the power equipment, the ejector has no moving part, the equipment volume is small, and gas-phase refrigerant does not flow through CO2Medium temperature stage evaporator for reducing CO under same heat exchange amount2The heat exchange area of the intermediate temperature stage evaporator is reduced, and CO is reduced2The air suction amount of the medium-pressure stage compression reduces the volume and the manufacturing cost of the compressor. CO lift by mainstream injection2Suction pressure of high temperature stage compressor, CO2The compression ratio of the high-pressure stage compressor is reduced, and the efficiency of the compressor is improved.
(4) CO at outlet of gas cooler is realized by connecting two subcoolers in series2Two successive step cooling, conventional refrigerant evaporation and supercritical CO2The fluid temperature drop process forms good temperature matching, reduces heat transfer temperature difference, reduces heat exchange irreversible loss and irreversible throttling loss, and improves the overall energy efficiency of the system.
(5) Transcritical CO2The circulating refrigerant is natural working medium CO2. ODP is 0, GWP is 1, and the composition does not separate under high temperature conditionsIs safe, nontoxic and environment-friendly. The working medium of the flow diverter supercharging mechanical auxiliary supercooling cycle can adopt pure refrigerants such as R1234ze (Z), R1234ze (E), R1233zd (E), R1224yd (Z), R1336mzz (Z), R365mfc, R1234yf and R245fa, and can also adopt CO2/R1234ze(E)、CO2/R1234ze(Z)、CO2Non-azeotropic mixed working media such as/R1234 yf, R41/R1234ze (E), R41/R1234ze (Z), R41/R1234yf, R32/R1234ze (E), R32/R1234ze (Z), R32/R1234yf and the like. For the non-azeotropic mixed working medium, a refrigerant with the temperature slippage equivalent to the temperature difference of the inlet and the outlet of the heat exchange fluid of the evaporator is selected, and the slippage temperature difference of the evaporation and condensation processes of the non-azeotropic working medium is not large, so that the heat transfer temperature difference can be reduced, and the irreversible loss can be reduced.
(6) The system is provided with CO2The high-pressure stage compressor, the medium-pressure stage compressor and the low-pressure stage compressor have small pressure ratio and are suitable for freezing and refrigerating application at lower temperature. The multifunctional water heater can be used for manufacturing domestic medium-temperature hot water or industrial high-temperature hot water and steam, can realize multiple functions through one set of equipment, improves the utilization rate of the equipment, saves the occupied space of the equipment, can be applied to superstores, cold storages and supermarkets with lower freezing and refrigerating temperatures, and can also be used in the application fields of butcheries, food processing plants and the like which need freezing and refrigerating as well as high-temperature or medium-temperature hot water/steam.
Drawings
FIG. 1 shows that the injection supercharging two-stage supercooling transcritical CO of the utility model2The simple structure of the dual temperature system is shown schematically.
Reference numerals:
1-CO2a low temperature stage evaporator; 2-CO2A high pressure stage compressor; 3-CO2A gas cooler; 4-intermediate temperature stage cooling evaporator; 5-low temperature stage cooling evaporator; 6-a throttle valve; 7-a common working medium compressor; 8-a condenser; 9-an ejector; 10-a throttle valve; 11-low temperature stage evaporator fan; 12-medium temperature stage evaporator fan; 13-CO2A medium temperature stage evaporator; 14-CO2A low pressure stage compressor; 15-medium temperature grade gas-liquid separator; 16-CO2An ejector; 17-a throttle valve; 18-CO2A medium pressure stage compressor; 19-CO2Low pressureA stage parallel compressor; 20-low temperature grade gas-liquid separator.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which this invention belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following embodiments and accompanying drawings.
As shown in figure 1, the injection supercharging two-stage supercooling transcritical CO2The dual-temperature system comprises an ejector supercharging dual-subcooler series mechanical subcooling circulation and transcritical CO which can exchange heat with each other2And (4) circulating in a double-temperature area. Wherein: transcritical CO2Two temperature zone cycle comprising CO2Low temperature stage evaporator 1, CO2Intermediate temperature stage evaporator 13, CO2Low pressure stage compressor 14, CO2Low pressure stage parallel compressor 19, CO2Medium pressure stage compressor 18, CO2High pressure stage compressor 2, CO2A gas cooler 3, a medium-temperature stage gas-liquid separator 4, a low-temperature stage gas-liquid separator 20, and CO2An ejector 16; the ejector supercharging double-subcooler series mechanical subcooling cycle comprises a common working medium compressor, a condenser, an ejector, a high-temperature-stage evaporator and a medium-temperature-stage evaporator. Specifically, the method comprises the following steps:
the CO is2The outlet of the low-temperature evaporator 1 is sequentially communicated with CO2Low pressure stage compressor 14, CO2Medium pressure stage compressor 18, CO2High pressure stage compressor 2, CO2Heat medium side of gas cooler 3, heat medium side of intermediate temperature stage cooling evaporator 4, heat medium side of low temperature stage cooling evaporator 5, intermediate temperature stage gas-liquid separator 15, low temperature stage gas-liquid separator 20, and CO2The inlet of the low temperature stage evaporator 1; the gas outlet of the medium-temperature stage gas-liquid separator 15 is communicated with CO2Secondary flow inlet of ejector 16, CO2Main flow inlet of eductor 16 and CO2Outlet of the high pressure stage compressor 2 is connected, CO2Outlet of the eductor 16 and CO2The inlets of the high-pressure stage compressors 2 are communicated; the above-mentionedThe liquid outlet of the medium-temperature stage gas-liquid separator 15 is also communicated with CO2The inlet of the intermediate temperature stage evaporator 13 is communicated with CO2Inlet of the intermediate temperature stage evaporator 13 and CO2The inlets of the intermediate-pressure stage compressors 18 are communicated; the air outlet of the low-temperature stage gas-liquid separator 20 is sequentially communicated with CO2Low pressure stage parallel compressor 19 and CO2The inlet of the intermediate-pressure stage compressor 18.
The gas-liquid phase fluid is separated by a medium-temperature stage gas-liquid separator and a low-temperature stage gas-liquid separator and flows into CO2The fluid of the intermediate-temperature-stage evaporator and the fluid of the low-temperature-stage evaporator are both liquid fluid, and the fluid is in CO2Intermediate temperature stage evaporator and CO2The low-temperature-stage evaporators are uniformly distributed in parallel pipelines, the heat exchange coefficient is increased, the heat exchange efficiency of the evaporators is improved, the size of the evaporators can be reduced on the premise of the same heat exchange quantity, and equipment can be more compact and the space utilization rate of refrigeration equipment can be improved when the evaporator is used in supermarket freezers and refrigerated cabinets. By CO2Low-temperature-stage parallel compressor for compressing gas-phase fluid in low-temperature-stage gas-liquid separator to CO separately2Compared with the traditional throttle-first recompression process, the same exhaust pressure of the low-temperature stage compressor omits the throttle process, thereby reducing the throttle irreversible loss of the gas and CO2Compared with the prior throttling recompression process, the compression ratio of the parallel compressor is improved, the suction pressure is increased, the compression ratio is reduced, and CO is reduced2The efficiency of the parallel compressor is high. By CO2CO at the outlet of the high-pressure stage compressor2The fluid is to lead the gas-phase fluid of the medium-temperature stage gas-liquid separator to be in CO2The ejector injects the gas to the intermediate pressure, the configuration of throttling and pressure reduction of a throttle valve or pressure boosting of compressor power equipment can be omitted, the saturated gas which does not participate in refrigeration is injected to the inlet of the compressor on the premise of greatly reducing throttling loss and not introducing the power equipment, the ejector has no moving part, the equipment volume is small, and gas-phase refrigerant does not flow through CO2Medium temperature stage evaporator for reducing CO under same heat exchange amount2The heat exchange area of the intermediate temperature stage evaporator is reduced, and CO is reduced2The air suction amount of the medium-pressure stage compression reduces the volume and the manufacturing cost of the compressor. CO lift by mainstream injection2The suction pressure of the high-temperature stage compressor,make CO CO2The compression ratio of the high-pressure stage compressor is reduced, and the efficiency of the compressor is improved
In addition, two subcoolers (namely the medium-temperature-stage cooling evaporator 4 and the low-temperature-stage cooling evaporator 5) are connected in series to realize CO at the outlet of the gas cooler2Two successive step cooling, conventional refrigerant evaporation and supercritical CO2The fluid temperature drop process forms good temperature matching, reduces heat transfer temperature difference, reduces heat exchange irreversible loss and irreversible throttling loss, and improves the overall energy efficiency of the system.
The outlet of the ejector 9 is sequentially communicated with the refrigerant side of the medium-temperature stage cooling evaporator 4, the inlet of the common working medium compressor 7 and the inlet of the heat medium side of the condenser 8; an outlet pipeline on a heat medium side of the condenser 8 is divided into two paths, one path is communicated with a main flow inlet of the ejector 9, and the other path is sequentially communicated with a refrigerant side of the low-temperature-stage cooling evaporator 5 and a secondary flow inlet of the ejector 9.
As an optional embodiment of the utility model, the heat transfer working medium of ejector pressure boost double subcooler series connection machinery supercooling circulation is pure refrigerant or non-azeotropic mixture working medium. Wherein: the pure refrigerant can adopt one of R1234zeZ, R1234zeE, R1233zdE, R1224ydZ, R1336mzzZ, R365mfc, R1234yf and R245fa, and is preferably R1234 yf; the non-azeotropic mixed working medium can adopt CO2/R1234zeE、CO2/R1234zeZ、CO2One of substances such as/R1234 yf, R41/R1234zeE, R41/R1234zeZ, R41/R1234yf, R32/R1234zeE, R32/R1234zeZ, R32/R1234yf, and the like, preferably R32/R1234 zeZ. For the non-azeotropic mixed working medium, a refrigerant with the temperature slippage equivalent to the temperature difference of the inlet and the outlet of the heat exchange fluid of the evaporator is selected, and the slippage temperature difference of the evaporation and condensation processes of the non-azeotropic working medium is not large, so that the heat transfer temperature difference can be reduced, and the irreversible loss can be reduced.
As an optional embodiment of the present invention, in order to improve the evaporation efficiency, at the CO2A low-temperature evaporator fan 11 is arranged below the low-temperature evaporator 1; the CO is2A medium-temperature-stage evaporator fan 12 is installed below the medium-temperature-stage evaporator 13.
As an optional embodiment of the present invention, in order to facilitate the control of the flow rate of the heat exchange fluid in the corresponding pipeline, a second throttle valve 17 is installed on the connection pipeline between the heat medium outlet of the low-temperature stage cooling evaporator 5 and the medium-temperature stage gas-liquid separator 15; a first throttle valve 6 is arranged on a connecting pipeline between the liquid outlet of the medium-temperature stage gas-liquid separator 15 and the liquid inlet of the low-temperature stage gas-liquid separator 20.
As an optional embodiment of the present invention, the CO2Low temperature stage evaporator 1, CO2The intermediate-temperature-stage evaporator 13, the intermediate-temperature-stage cooling evaporator 4 and the low-temperature-stage cooling evaporator 5 respectively adopt a finned tube heat exchanger, a double-tube heat exchanger or a plate heat exchanger, or a double-tube heat exchanger or a plate heat exchanger; the CO is2The gas cooler 3 is a double pipe heat exchanger or a plate heat exchanger. In a more preferred embodiment, the intermediate-temperature stage cooling evaporator 4 and the low-temperature stage cooling evaporator 5 respectively adopt a double-pipe heat exchanger and a plate heat exchanger, and CO2The gas cooler 3 is a double pipe heat exchanger.
As an optional embodiment of the present invention, transcritical CO2The heat exchange fluid circulated in the two temperature zones is CO2。
As an optional embodiment of the present invention, the CO2Low temperature stage evaporator 1, CO2The working temperature ranges of the medium-temperature grade evaporator 13, the medium-temperature grade cooling evaporator 4 and the low-temperature grade cooling evaporator 5 are-56 to-20 ℃, 10 to 10 ℃, 10 to 40 ℃ and 10 to 20 ℃ respectively; CO 22The suction pressure range of the low-pressure stage compressor 14 is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa; CO 22The suction pressure range of the medium-pressure stage compressor 18 is 2.65-4.50 MPa, and the exhaust pressure range is 5-6 MPa; CO 22The suction pressure range of the high-pressure stage compressor 2 is 5-6 MPa, and the exhaust pressure range is 7.5-14 MPa; CO 22The suction pressure range of the low-pressure stage parallel compressor 19 is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa; CO 22The secondary flow of the ejector 16 has the air suction temperature ranging from-10 ℃ to 10 ℃, the pressure ranging from 2.65 MPa to 4.50MPa, the main flow temperature ranging from 80 ℃ to 140 ℃, the pressure ranging from 7.5 MPa to 14MPa, the ejector outlet temperature ranging from 40 ℃ to 50 ℃ and the pressure ranging from5-6 MPa; the suction temperature range of the ordinary working medium middle-temperature stage compressor 7 is 20-50 ℃, and the exhaust temperature range is 70-120 ℃.
As an alternative embodiment of the present invention, the condenser 8 is a double pipe heat exchanger or a plate heat exchanger, preferably a double pipe heat exchanger. Meanwhile, in order to control the flow rate of the heat exchange fluid in the pipe between the outlet on the heating medium side of the condenser 8 and the inlet of the refrigerant of the low-temperature stage cooling evaporator 5, a third throttle valve 10 is installed on the pipe between the outlet on the heating medium side of the condenser 8 and the inlet of the refrigerant of the low-temperature stage cooling evaporator 5.
As an optional embodiment of the present invention, the refrigerant side of the condenser 8 and the CO2The refrigerant side of the gas cooler 3 is respectively communicated with a heat exchange fluid source. Therefore, the heat exchange fluid can be divided into two paths, the two paths of heat exchange fluid respectively flow into the condenser 8 and the gas cooler 3, the heat exchange fluid is heated and then converged to flow into the heat exchange fluid side inlet of the condenser 8, the heat exchange fluid is heated to the temperature required by the process, the required medium-high temperature hot water or high-temperature steam is obtained, and the continuous heating process of the heat exchange fluid is completed. Wherein the heat exchange fluid may be water.
Injection pressure double stage supercooling transcritical CO2A preferred process condition for the use of the dual temperature system is: CO 22The evaporation temperature of the low-temperature stage evaporator 1 is-30 ℃, the temperature of the medium-temperature stage cooling evaporator 4 is 0 ℃, the temperature of the low-temperature stage cooling evaporator 5 is 5 ℃, and CO is in the range of2The temperature of the medium-temperature grade evaporator 13 is 0 ℃; CO 22The suction pressure of the low-temperature stage compressor 14 is 1.43MPa, and the exhaust pressure is 3.49 MPa; CO 22The suction pressure of the medium-pressure stage compressor 18 is 3.49MPa, the exhaust pressure is 5.5MPa, and CO is discharged2The suction pressure of the high-pressure stage compressor 2 is 5.5MPa, and the exhaust pressure is 10 MPa; CO 22The suction pressure of the low-pressure stage parallel compressor 19 is 1.43MPa, and the discharge pressure is 3.49 MPa. CO 22The secondary flow of the ejector 16 has the air suction temperature of 0 ℃, the pressure of 3.49MPa, the main flow temperature of 120 ℃, the pressure of 10MPa, the ejector outlet temperature of 45 ℃ and the pressure of 5.5 MPa. The working medium flowing through the refrigerant side of the intermediate-temperature stage cooling evaporator 4, the refrigerant side of the low-temperature stage cooling evaporator 5 and the heat medium side of the condenser 8 is R32/R1234 zeZ.The suction temperature of the medium-temperature stage compressor 7 in the common working medium is 30 ℃, and the exhaust temperature is 90 ℃.
Use the injection supercharging two-stage supercooling transcritical CO2The method for refrigerating and heat exchanging by a dual-temperature system, as shown in fig. 1, comprises the following steps:
the first step is as follows: CO 22Low temperature and low pressure CO at the outlet of the low temperature stage evaporator 12Fluid is CO2Working fluid compressed to medium temperature and medium pressure is sucked by the low-pressure stage compressor 14, and gas phase fluid in the low-temperature stage gas-liquid separator 20 is subjected to CO2Working fluid, CO, compressed to medium temperature and pressure by a low-pressure stage parallel compressor 192The outlet of the medium-temperature stage evaporator 13 is saturated or overheated medium-temperature medium-pressure CO after heat absorption and evaporation2Fluid, three streams of CO2The fluids are mixed and then CO is added2The intermediate stage compressor 18 takes in and compresses. Then with CO2The fluid at the outlet of the eductor 16 is mixed with CO2The high pressure stage compressor 2 sucks and compresses. The compressed fluid is divided into two paths, one path of the compressed fluid enters a nozzle 16 of the ejector as a main flow to carry out isentropic expansion, the flow rate is increased, the pressure is reduced, and CO is ejected2The gas phase fluid of the gas-liquid separator 15 enters CO through the other path2The gas cooler 3 exchanges heat with a heat exchange fluid. CO 22Fluid at the outlet of the gas cooler 3 sequentially flows through the medium-temperature-stage cooling evaporator 4 and the low-temperature-stage cooling evaporator 5, heat release is continuously carried out twice through the evaporation process of common working media or non-azeotropic working media, then the fluid flows out of the low-temperature-stage cooling evaporator 5 and enters the throttle valve 17 for throttling, the throttled working fluid enters the medium-temperature-stage gas-liquid separator 15, the outlet of the medium-temperature-stage gas-liquid separator 15 is divided into two streams, one stream is taken as secondary stream to be subjected to CO treatment, and the other stream2The fluid at the outlet of the high-pressure stage compressor 2 is injected in the injector 16. CO 22The pressure of the main flow at the nozzle outlet of the ejector 16 is lower than that of the secondary flow inlet, and the secondary flow is continuously sucked into CO by the low-pressure main flow2The suction chamber of the ejector 16 is mixed with the low-pressure main flow in the mixing chamber, the mixed fluid enters the pressure expansion chamber, the fluid speed is reduced, and the pressure is increased to be between the main flow and the secondary fluid. The other is divided into two paths, one is flowed through CO213-way intermediate temperature stage evaporatorThe intermediate temperature stage evaporator fan 12 drives the air and finned tubes (i.e., CO)2The medium temperature stage evaporator 13) releases cold energy through convection heat transfer, the other part enters the low temperature stage gas-liquid separator 20 after being throttled by the throttle valve 6, and the separated liquid phase fluid enters CO2The low temperature stage evaporator 1 drives air and finned tubes (i.e., CO) by the low temperature stage evaporator fan 112The low-temperature stage evaporator 1) releases cold energy through heat convection, and the other gas is CO2The low pressure stage is compressed in parallel with compressor 19.
The second step is that: the ordinary working medium compressor 7 compresses the ordinary working medium at the side outlet of the ordinary working medium of the high-temperature-stage evaporator 4 to high-temperature high-pressure superheated gas, then the high-temperature high-pressure superheated gas enters the condenser 8 to exchange heat with heat exchange fluid, the temperature is reduced, the high-pressure fluid at the outlet of the condenser 8 is divided into two paths, one path is a main flow, the main flow flows into the nozzle of the ejector 9 to perform isentropic expansion, and the pressure is increased.
The third step: the other path of the high-pressure fluid at the outlet of the condenser 8 is secondary flow, flows into the throttle valve 10 for throttling and pressure reduction, and then flows through the common working medium side of the medium-temperature stage evaporator 5 and CO flowing out of the high-temperature stage evaporator 42And heat exchange is carried out, the secondary flow is continuously sucked into the suction chamber of the ejector 9 by the main flow, and is mixed with the main flow in the mixing chamber, so that the pressure is increased. The mixed fluid at the outlet of the ejector 9 flows into the CO at the common working medium side of the high-temperature evaporator 4 and the outlet of the gas cooler 32And (4) exchanging heat, wherein the common working medium subjected to heat absorption and evaporation is changed into saturated gas, and the saturated gas enters a common working medium compressor 7 for compression, so that the flow diverter supercharging double subcooler series mechanical auxiliary subcooling circulation is completed.
The fourth step: the heat exchange fluid W1 is divided into two paths, which respectively flow into the condenser 8 and the gas cooler 3, the heat exchange fluid is heated and then converged to flow into the heat exchange fluid side inlet of the condenser 8, the heat exchange fluid is heated to the temperature required by the process, the required medium-high temperature hot water or high-temperature steam is obtained, and the continuous heating process of the heat exchange fluid is completed. Air flow through CO2The heat exchange fluid side of the evaporator is cooled to complete the refrigeration process.
It should be noted that the common working medium side is also called the refrigerant side.
Injection pressure double stage supercooling transcritical CO2A dual temperature system is provided with CO2The high-pressure stage compressor, the medium-pressure stage compressor and the low-pressure stage compressor have small pressure ratio and are suitable for freezing and refrigerating application at lower temperature. The multifunctional water heater can be used for manufacturing domestic medium-temperature hot water or industrial high-temperature hot water and steam, can realize multiple functions through one set of equipment, improves the utilization rate of the equipment, saves the occupied space of the equipment, can be applied to superstores, cold storages and supermarkets with lower freezing and refrigerating temperatures, and can also be used in the application fields of butcheries, food processing plants and the like which need freezing and refrigerating as well as high-temperature or medium-temperature hot water/steam.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. Injection supercharging two-stage supercooling transcritical CO2Two warm systems, its characterized in that: comprises an ejector supercharging double subcooler which can exchange heat with each other, a mechanical subcooling cycle connected in series and transcritical CO2Circulating in a double-temperature area;
the trans-critical CO2Two temperature zone cycle comprising CO2A low-temperature stage evaporator (1); the CO is2The outlets of the low-temperature evaporator (1) are sequentially communicated with CO2Low pressure stage compressor (14), CO2Medium pressure stage compressor (18), CO2High pressure stage compressor (2), CO2A heat medium side of the gas cooler (3), a heat medium side of the medium temperature stage cooling evaporator (4), a heat medium side of the low temperature stage cooling evaporator (5), a medium temperature stage gas-liquid separator (15), a low temperature stage gas-liquid separator (20) and CO2The inlet of the low-temperature stage evaporator (1); the gas outlet of the medium-temperature stage gas-liquid separator (15) is communicated with CO2Secondary inflow port of ejector (16), CO2A main flow inlet of the ejector (16) and CO2The outlet of the high-pressure stage compressor (2) is communicated with CO2Outlet of ejector (16) and CO2The inlets of the high-pressure stage compressors (2) are communicated; the liquid outlet of the medium-temperature stage gas-liquid separator (15) is also communicated with CO2The inlet of the intermediate temperature stage evaporator (13) is communicated with CO2Inlet of intermediate temperature stage evaporator (13) and CO2The inlets of the intermediate-pressure stage compressors (18) are communicated; the air outlet of the low-temperature stage gas-liquid separator (20) is communicated with CO in sequence2Low pressure stage parallel compressor (19) and CO2An inlet of the intermediate-pressure stage compressor (18).
2. The ejector two-stage subcooling transcritical CO of claim 12Two warm systems, its characterized in that: the ejector supercharging double-subcooler series mechanical subcooling cycle comprises an ejector (9), wherein an outlet of the ejector (9) is sequentially communicated with a refrigerant side of the medium-temperature-stage cooling evaporator (4), an inlet of a common working medium compressor (7) and an inlet of a heat medium side of a condenser (8); and an outlet pipeline at the heat medium side of the condenser (8) is divided into two paths, one path is communicated with a main flow inlet of the ejector (9), and the other path is sequentially communicated with a refrigerant side of the low-temperature-level cooling evaporator (5) and a secondary flow inlet of the ejector (9).
3. The ejector two-stage subcooling transcritical CO of claim 12Two warm systems, its characterized in that: the CO is2A low-temperature evaporator fan (11) is arranged below the low-temperature evaporator (1); the CO is2A medium temperature grade evaporator fan (12) is arranged below the medium temperature grade evaporator (13).
4. The injection supercharging two-stage subcooling transcritical CO according to claim 1 or 32Two warm systems, its characterized in that: a second throttle valve (17) is arranged on a connecting pipeline between a heat medium outlet of the low-temperature stage cooling evaporator (5) and the medium-temperature stage gas-liquid separator (15); a first throttle valve (6) is arranged on a connecting pipeline between the liquid outlet of the medium-temperature stage gas-liquid separator (15) and the liquid inlet of the low-temperature stage gas-liquid separator (20).
5. The injection supercharging two-stage subcooling transcritical CO according to claim 1 or 32Two warm systems, its characterized in that: the CO is2Low temperature stage evaporator (1), CO2The medium temperature stage evaporator (13), the medium temperature stage cooling evaporator (4) and the low temperature stage cooling evaporator (5) are respectively adoptedFinned tube heat exchangers, double pipe heat exchangers or plate heat exchangers; the CO is2The gas cooler (3) is a double-pipe heat exchanger or a plate heat exchanger.
6. The injection supercharging two-stage subcooling transcritical CO according to claim 1 or 32Two warm systems, its characterized in that: transcritical CO2The heat exchange fluid circulated in the two temperature zones is CO2；CO2The secondary flow of the ejector (16) has the air suction temperature ranging from-10 ℃ to 10 ℃, the pressure ranging from 2.65 MPa to 4.50MPa, the main flow temperature ranging from 80 ℃ to 140 ℃, the pressure ranging from 7.5 MPa to 14MPa, the ejector outlet temperature ranging from 40 ℃ to 50 ℃ and the pressure ranging from 5MPa to 6 MPa.
7. The injection supercharging two-stage subcooling transcritical CO according to claim 1 or 32Two warm systems, its characterized in that: the CO is2Low temperature stage evaporator (1), CO2The working temperature ranges of the medium-temperature-level evaporator (13), the medium-temperature-level cooling evaporator (4) and the low-temperature-level cooling evaporator (5) are-56 to-20 ℃, 10 to 10 ℃, 10 to 40 ℃ and 10 to 20 ℃ respectively; CO 22The suction pressure range of the low-pressure stage compressor (14) is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa; CO 22The suction pressure range of the medium-pressure stage compressor (18) is 2.65-4.50 MPa, and the exhaust pressure range is 5-6 MPa; CO 22The suction pressure range of the high-pressure stage compressor (2) is 5-6 MPa, and the exhaust pressure range is 7.5-14 MPa; CO 22The suction pressure range of the low-pressure stage parallel compressor (19) is 0.53-1.97 MPa, and the exhaust pressure range is 2.65-4.50 MPa.
8. The injection supercharging two-stage subcooling transcritical CO according to claim 1 or 22Two warm systems, its characterized in that: the heat exchange working medium of the ejector supercharging double subcoolers connected in series with the mechanical subcooling cycle is pure refrigerant or non-azeotropic mixed working medium;
the pure refrigerant is one of R1234ze (Z), R1234ze (E), R1233zd (E), R1224yd (Z), R1336mzz (Z), R365mfc, R1234yf and R245 fa;
the non-azeotropic mixed working medium is CO2/R1234ze(E)、CO2/R1234ze(Z)、CO2One of R1234yf, R41/R1234ze (E), R41/R1234ze (Z), R41/R1234yf, R32/R1234ze (E), R32/R1234ze (Z), R32/R1234 yf.
9. The ejector two-stage subcooling transcritical CO of claim 22Two warm systems, its characterized in that: the condenser (8) is a double-pipe heat exchanger or a plate heat exchanger;
the air suction temperature range of the common working medium compressor (7) is 20-50 ℃, and the exhaust temperature range is 70-120 ℃.
10. The ejector two-stage subcooling transcritical CO of claim 22Two warm systems, its characterized in that: the condenser also comprises a third throttle valve (10) arranged on a pipeline between a heat medium side outlet of the condenser (8) and a refrigerant inlet of the low-temperature stage cooling evaporator (5); refrigerant side of condenser (8) and CO2The refrigerant side of the gas cooler (3) is respectively communicated with a heat exchange fluid source.
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