Method and algorithm for determining operation parameters of refrigerating system of cold therapy cabin

Abstract

The invention discloses a method and an algorithm for determining operation parameters of a refrigerating system of a cold therapy cabin. A sensor in the refrigerating system collects parameters, a flow sensor determines the mass composition of fluid by measuring the density of the fluid, and a pressure and temperature sensor is used for determining state parameters of the fluid. Thermodynamic parameters of the refrigerating system of the cold therapy cabin are calculated, wherein the parameters comprise the liquid-phase refrigerant density, the mass components of all gas-liquid separation components, the enthalpy value of a mixing point of each stage of condensation evaporator, the enthalpy value of each stage of condensation evaporator and the enthalpy value of the evaporator; according to thermodynamic parameters of the refrigeration system, system operation parameters are determined, and cycle components, cooling capacity and system COP are predicted; the thermodynamic efficiency of the refrigeration system is improved by determining the operation parameters of the refrigeration system of the cold therapy cabin and predicting the circulation components, the cooling capacity and the COP of the system through the algorithm, and stable and efficient operation of the refrigeration system of the cold therapy cabin is achieved according to the predicted actual operation parameters.

Description

Technical Field

[0001] This invention relates to the field of refrigeration system technology, and specifically to a method and algorithm for determining the operating parameters of a cryotherapy chamber refrigeration system. Background Technology

[0002] Determining the operating parameters of the refrigeration system allows for adjustment of the internal refrigerant composition ratio, thereby improving the thermodynamic efficiency of the refrigeration system. The energy and composition ratio of the refrigerant after passing through each electronic component are obtained based on the sensor components installed at the inlet and outlet, thus predicting the energy and composition ratio of the refrigerant when it reaches the cryotherapy chamber. This enables the refrigeration system of the cryotherapy chamber to operate stably and efficiently. Summary of the Invention

[0003] The purpose of this invention is to provide a method and algorithm for determining the operating parameters of a cryotherapy chamber's refrigeration system, in order to solve the problem mentioned in the background art of determining the operating parameters of the refrigeration system to achieve stable and efficient system operation.

[0004] To achieve the above objectives, the present invention adopts the following technical solution:

[0005] A method and algorithm for determining the operating parameters of a cryotherapy chamber's refrigeration system, comprising the following steps:

[0006] S1; Sensors within the refrigeration system collect parameters, including a flow sensor that determines the fluid's mass composition by measuring fluid density, and pressure and temperature sensors used to determine the fluid's state parameters.

[0007] S2; Calculation of thermodynamic parameters of the refrigeration system of the cryotherapy chamber, including liquid refrigerant density, mass composition of each component in gas-liquid separation, enthalpy of the mixing point of each stage of condenser-evaporator, enthalpy of each stage of condenser-evaporator, and enthalpy of the evaporator.

[0008] S3; Determine system operating parameters based on the thermodynamic parameters of the refrigeration system, predict the circulation composition, cooling capacity and system COP, and achieve stable and efficient operation of the refrigeration system of the cryotherapy chamber based on the predicted actual operating parameters.

[0009] The density of the liquid refrigerant was used to evaluate the thermodynamic properties of the non-azeotropic refrigerants R-290 / R-23 / R-14 based on the Refprop10 refrigerant property database; the equations for determining the property parameters using the Refprop10 database are as follows:

[0010] (h,ρ,x,t…..)=f('p1','p2',Z) Formula 1

[0011] Where Z represents the mass composition of the non-azeotropic refrigerant, based on the refrigerant charge G. R290 / G R23 / G R14 =ZR290_initial / Z R23_initial / Z R14_initial The parameters p1 and p2 to be determined are obtained through system sensors; p1 and p2 are the collected temperature and pressure parameters, respectively.

[0012] The parameters of the mass composition of each component in the gas-liquid separation are determined. Phase separation in the gas-liquid separator can be calculated using Bell & Deiters correlation, according to the separation rules provided in Refprop 10. The mass composition of the saturated liquid and vapor in equilibrium is determined by the pressure of the gas-liquid separator and the mass composition at the inlet.

[0013] [Z l,GLS Z g,GLS ]=f(p i Formula 2 (Z)

[0014] Z l,GLS Z represents the mass composition of the liquid phase fluid output from the bottom outlet L of the gas-liquid separator; where Z g,GLS The mass composition of the liquid fluid output from the bottom outlet G of the gas-liquid separator;

[0015] Non-azeotropic refrigerants have no chemical interactions, and the separated components satisfy mass and energy balance.

[0016]

[0017] in Liquid phase mass, Gas phase quality;

[0018] The non-azeotropic refrigerant mixture has a mass balance among its components.

[0019]

[0020]

[0021]

[0022] In this non-azeotropic refrigerant mixture, the energy of each component is balanced.

[0023]

[0024]

[0025]

[0026] The mixing point enthalpy values ​​of the various stages of condenser-evaporators in the refrigeration system are (C,mix-1), (D,mix-2), and (E,mix-3) for the high, medium, and low temperature stages of the condenser-evaporator, respectively. The mixing point (C,mix-1) is formed by the branch throttling valve TOF→(C,mix-1), the electronic expansion valve EXV-1→(C,mix-1), and the OUT_2→(C,mix-1) of the medium temperature stage condenser-evaporator CE_MTS. The mixing point (D,mix-2) is formed by the branch electromagnetic throttling valve ETOF-2→(D,mix-2), the electronic expansion valve EXV-2→(D,mix-2), and the OUT_2→(D,mix-2) of the low temperature stage condenser-evaporator CE_LTS. The system consists of two mixing points: (C, mix-2) and (D, mix-3). The mixing point (E, mix-3) is composed of the electromagnetic throttle valve ETOF-5→(E, mix-3) and the electronic expansion valve EXV-3→(D, mix-2). Different mixing points and the number of mixing points correspond to different refrigeration temperatures. For refrigeration at -40℃ cabin temperature, the mixing point in the refrigeration cycle of the refrigeration system is (C, mix-1). For refrigeration at -80℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1) and (D, mix-2). For refrigeration at -110℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1), (D, mix-2), and (E, mix-3).

[0027] The enthalpy values ​​under different refrigeration operating modes are then calculated as follows;

[0028] The cooling system at -40℃ cabin temperature involves the following branches at the mixing point (C,mix-1): throttle valve TOF → (C,mix-1) and electronic expansion valve EXV-1 → (C,mix-1).

[0029] For cooling at an internal temperature of -80℃, the branches involved in mixing at the mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate temperature stage condenser evaporator CE_MTS; the branches involved in mixing at the mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and electronic expansion valve EXV-2→(D,mix-2).

[0030] For cooling at an internal temperature of -110℃, the branches involved in mixing at mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate-temperature condenser-evaporator CE_MTS; the branches involved in mixing at mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and OUT_2→(D,mix-2) of the low-temperature condenser-evaporator CE_LTS; the branches involved in mixing at mixing point (E,mix-3) are: electromagnetic throttle valve ETOF-5→(E,mix-3) and EXV-3→(D,mix-2).

[0031] For the electronic expansion valves EXV-1→(C,mix-1), EXV-1→(D,mix-2), and EXV-1→(D,mix-2) in different branches, their enthalpy values ​​are the enthalpy values ​​of the evaporative heat exchanger EHX passing through the state point (F,o). There is no mass loss and the enthalpy value remains unchanged before and after the electronic expansion valves EXV-1 / EXV-2 / EXV-3. For the throttling valves TOF→(C,mix-1) and ETOF-2→(D,mix-2) in different branches, their enthalpy values ​​are as follows: The enthalpy values ​​of x-2) and electromagnetic throttle valve ETOF-5→(E,mix-3) are derived from the enthalpy values ​​of the fluid output from the bottom liquid phase outlet L of their respective upstream gas-liquid separator GLS; among them, OUT_2→(C,mix-1) of the branch medium-temperature stage condenser-evaporator CE_MTS is the enthalpy value of the outlet OUT_2 of the medium-temperature stage condenser-evaporator CE_MTS, and OUT_2→(D,mix-2) of the branch low-temperature stage condenser-evaporator CE_LTS is the enthalpy value of the outlet OUT_2 of the low-temperature stage condenser-evaporator CE_LTS.

[0032] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -40℃ in the cooling mode.

[0033] h C,mix-1 | -40℃ =h l,GLS-1 | -40℃ +h F,o | -40℃ ; Formula 10

[0034] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -80℃ in the cooling mode.

[0035] h C,mix-1 | -80℃ =h l,GLS-1 | -80℃ +h CE_MTS,OUT_2 | -80℃ , Formula 11

[0036] Enthalpy of the mixing point (D, mix-2)

[0037] h D,mix-2 | -80℃ =h l,GLS-2 | -80℃ +h F,o | -80℃ ; Formula 12

[0038] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -110℃ in the cooling mode.

[0039] h C,mix-1 | -110℃ =h l,GLS-1 | -110℃ +h CE_MTS,OUT_2 | -110℃ , Formula 13

[0040] Enthalpy of the mixing point (D, mix-2)

[0041] h D,mix-2 | -110℃ =h l,GLS-2 | -110℃ +h CE_LTS,OUT_2 | -110℃ Formula 14

[0042] Enthalpy of the mixing point (E, mix-3)

[0043] h E,mix-3 | -110℃ =h l,GLS-3 | -110℃ +h F,o | -110℃ Formula 15

[0044] The enthalpy values ​​of the various stages of the condenser-evaporator are as follows: the high, medium, and low temperature stage condenser-evaporators each have four ends on both sides, consisting of two pairs of inlets and outlets; one side's inlet and outlet are the condensation side, and the other side's inlet and outlet are the evaporation side; the heat exchange capacity of the condenser-evaporator is...

[0045] Q CE =K·A·Δt m , Formula 16

[0046] According to the laws of conservation of mass and energy, the heat transfer on the condensing side is Q. cd Evaporation side heat exchange Q ev ,have

[0047] Q cd =Q ev =Q CE , Formula 17

[0048] The logarithmic mean temperature difference between the condenser and evaporator is:

[0049]

[0050] Where T cd,in This refers to the condenser-side inlet temperature of the condenser-evaporator, corresponding to the IN_1 port in the high-temperature stage condenser-evaporator CE_HTS, the medium-temperature stage condenser-evaporator CE_MTS, and the low-temperature stage condenser-evaporator CE_LTS; T cd,out This refers to the condenser-side outlet temperature of the evaporator, corresponding to the OUT_1 port in CE_HTS, CE_MTS, and CE_LTS mentioned above; T ev,in This refers to the inlet temperature on the evaporator side of the condenser-evaporator, corresponding to port IN_2 in CE_HTS, CE_MTS, and CE_LTS mentioned above; T ev,out This refers to the outlet temperature on the evaporator side of the condenser evaporator, corresponding to the OUT_2 port in CE_HTS, CE_MTS, and CE_LTS mentioned above.

[0051] The heat exchanger on the condensing side

[0052] Q cd =m cd ·(h cd,in -h cd,out ), Formula 19

[0053] m cd The refrigerant mass flow rate on the condenser side of the evaporator is kg / s.

[0054] h cd,in The enthalpy of the refrigerant at the condenser side of the evaporator is expressed in kJ / kg.

[0055] h cd,out The enthalpy of the refrigerant outlet on the condenser side of the evaporator is expressed in kJ / kg.

[0056] The heat exchange on the evaporation side

[0057] Q ev =m ev ·(h ev,in -h ev,out ). Formula 20

[0058] m ev The refrigerant mass flow rate on the evaporator side of the condenser-evaporator is kg / s.

[0059] h ev,in The enthalpy of the refrigerant outlet on the evaporator side of the condenser-evaporator is expressed in kJ / kg.

[0060] h ev,out The enthalpy of the refrigerant at the evaporator inlet on the condenser-evaporator side is expressed in kJ / kg.

[0061] The enthalpy of the evaporator is

[0062] Q EHX =K·A·Δtm =m EHX ·(h EHX,in -h EHX,out ) Formula 21

[0063] S3 determines the system operating parameters based on the thermodynamic parameters of the refrigeration system. At state point (A), the compressed non-azeotropic working fluid is divided into two fluid streams, with the liquid phase composition of the fluid passing through state point (B, i-mr) being Z. B,i-mr The fluid phase composition after bypassing state point (A,bp) is Z. A,bp The liquid phase component Z bypassed by the aforementioned state point (A,bp) A,bp Based on the Refprop10 refrigerant property database, according to ρ g =f(t,p,Z), where the fluid density ρ is determined by iteratively calculating the mass composition Z of the non-azeotropic refrigerant. g ρ collected by mass flow meter rt-g By approximating each other, the mass composition Z of the non-azeotropic working fluid bypassed at the current state point (A,bp) can be obtained. A,bp The fluid composition at state point (B, i-mr) can be obtained as Z. B,i-mr =ZZ A-bp .

[0064] The component is Z B,i-mr The two-phase non-azeotropic refrigerant enters the inlet (GLS-1,i) of the gas-liquid separator GLS-1. As shown in Formula 2 above, which calculates the mass composition of each component in the gas-liquid separation process, the mass composition Z of the fluid flowing out from the liquid phase outlet L after passing through the gas-liquid separator GLS-1 is... l,GLS And the mass composition Z of the fluid flowing out from the gas phase outlet G. g,GLS This is related to the fluid temperature at the inlet (GLS-1,i) and the pressure within the gas-liquid separator GLS-1; by controlling the inlet temperature t of the gas-liquid separator GLS-1... GLS-1,i and the pressure P inside GLS-1 GLS-1 Real-time data acquisition, Z can be determined using Formula 2. l,GLS-1 and Z g,GLS-1 Non-azeotropic refrigerants do not have chemical interactions with each other, and the separated components satisfy mass and energy balance. The mass composition of each component of the non-azeotropic refrigerant mixture can be determined using formula 4-6. and The energy values ​​of non-azeotropic refrigerant mixtures are determined using formula 7-8. and

[0065] According to the thermodynamic characteristics of the throttling valve, there is no mass loss of refrigerant and the enthalpy remains unchanged before and after throttling. The pressure and temperature change before and after throttling. When the liquid phase mixture flowing out of the liquid phase outlet L of the gas-liquid separator GLS-1 passes through the throttling valve TOF, there is no mass loss and the enthalpy remains unchanged.

[0066] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0067] This invention improves the thermodynamic efficiency of the cryotherapy chamber's refrigeration system by determining its operating parameters and using algorithms to predict the circulating components, cooling capacity, and system COP. Based on the predicted operating parameters, the cryotherapy chamber's refrigeration system achieves stable and efficient operation. Attached Figure Description

[0068] Figure 1 This is one of the partial process diagrams of the present invention;

[0069] Figure 2 This is a second partial flowchart of the present invention;

[0070] Figure 3 This is a partial flowchart of the present invention.

[0071] Figure 4 This is a partial flowchart of the present invention (Figure 4).

[0072] Figure 5 This is a schematic diagram of the circuit structure of the present invention. Detailed Implementation

[0073] The technical solution of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the protection scope of the present invention.

[0074] Example 1

[0075] A method and algorithm for determining the operating parameters of a cryotherapy chamber's refrigeration system, comprising the following steps:

[0076] S1; Sensors within the refrigeration system collect parameters, including a flow sensor that determines the fluid's mass composition by measuring fluid density, and pressure and temperature sensors used to determine the fluid's state parameters.

[0077] S2; Calculation of thermodynamic parameters of the refrigeration system of the cryotherapy chamber, including liquid refrigerant density, mass composition of each component in gas-liquid separation, enthalpy of the mixing point of each stage of condenser-evaporator, enthalpy of each stage of condenser-evaporator, and enthalpy of the evaporator.

[0078] S3; Determine system operating parameters based on the thermodynamic parameters of the refrigeration system, predict the circulation composition, cooling capacity and system COP, and achieve stable and efficient operation of the refrigeration system of the cryotherapy chamber based on the predicted actual operating parameters.

[0079] The density of the liquid refrigerant was used to evaluate the thermodynamic properties of the non-azeotropic refrigerants R-290 / R-23 / R-14 based on the Refprop10 refrigerant property database; the equations for determining the property parameters using the Refprop10 database are as follows:

[0080] (h,ρ,x,t…..)=f('p1','p2',Z) Formula 1

[0081] Where Z represents the mass composition of the non-azeotropic refrigerant, based on the refrigerant charge G. R290 / G R23 / G R14 =Z R290_initial / Z R23_initial / Z R14_initial The parameters p1 and p2 to be determined are obtained through system sensors; p1 and p2 are the collected temperature and pressure parameters, respectively.

[0082] The parameters of the mass composition of each component in the gas-liquid separation are determined. Phase separation in the gas-liquid separator can be calculated using Bell & Deiters correlation, according to the separation rules provided in Refprop 10. The mass composition of the saturated liquid and vapor in equilibrium is determined by the pressure of the gas-liquid separator and the mass composition at the inlet.

[0083] [Z l , GLS Z g , GLS ]=f(p i Formula 2 (Z)

[0084] Z l,GLS Z represents the mass composition of the liquid phase fluid output from the bottom outlet L of the gas-liquid separator; where Z g,GLS The mass composition of the liquid fluid output from the bottom outlet G of the gas-liquid separator;

[0085] Non-azeotropic refrigerants have no chemical interactions, and the separated components satisfy mass and energy balance.

[0086]

[0087] in Liquid phase mass, Gas phase quality;

[0088] The non-azeotropic refrigerant mixture has a mass balance among its components.

[0089]

[0090]

[0091]

[0092] In this non-azeotropic refrigerant mixture, the energy of each component is balanced.

[0093]

[0094]

[0095]

[0096] The mixing point enthalpy values ​​of the various stages of condenser-evaporators in the refrigeration system are (C,mix-1), (D,mix-2), and (E,mix-3) for the high, medium, and low temperature stages of the condenser-evaporator, respectively. The mixing point (C,mix-1) is formed by the branch throttling valve TOF→(C,mix-1), the electronic expansion valve EXV-1→(C,mix-1), and the OUT_2→(C,mix-1) of the medium temperature stage condenser-evaporator CE_MTS. The mixing point (D,mix-2) is formed by the branch electromagnetic throttling valve ETOF-2→(D,mix-2), the electronic expansion valve EXV-2→(D,mix-2), and the OUT_2→(D,mix-2) of the low temperature stage condenser-evaporator CE_LTS. The system consists of two mixing points: (C, mix-2) and (D, mix-3). The mixing point (E, mix-3) is composed of the electromagnetic throttle valve ETOF-5→(E, mix-3) and the electronic expansion valve EXV-3→(D, mix-2). Different mixing points and the number of mixing points correspond to different refrigeration temperatures. For refrigeration at -40℃ cabin temperature, the mixing point in the refrigeration cycle of the refrigeration system is (C, mix-1). For refrigeration at -80℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1) and (D, mix-2). For refrigeration at -110℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1), (D, mix-2), and (E, mix-3).

[0097] The enthalpy values ​​under different refrigeration operating modes are then calculated as follows;

[0098] The cooling system at -40℃ cabin temperature involves the following branches at the mixing point (C,mix-1): throttle valve TOF → (C,mix-1) and electronic expansion valve EXV-1 → (C,mix-1).

[0099] For cooling at an internal temperature of -80℃, the branches involved in mixing at the mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate temperature stage condenser evaporator CE_MTS; the branches involved in mixing at the mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and electronic expansion valve EXV-2→(D,mix-2).

[0100] For cooling at an internal temperature of -110℃, the branches involved in mixing at mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate-temperature condenser-evaporator CE_MTS; the branches involved in mixing at mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and OUT_2→(D,mix-2) of the low-temperature condenser-evaporator CE_LTS; the branches involved in mixing at mixing point (E,mix-3) are: electromagnetic throttle valve ETOF-5→(E,mix-3) and EXV-3→(D,mix-2).

[0101] For the electronic expansion valves EXV-1→(C,mix-1), EXV-1→(D,mix-2), and EXV-1→(D,mix-2) in different branches, their enthalpy values ​​are the enthalpy values ​​of the evaporative heat exchanger EHX passing through the state point (F,o). There is no mass loss and the enthalpy value remains unchanged before and after the electronic expansion valves EXV-1 / EXV-2 / EXV-3. For the throttling valves TOF→(C,mix-1) and ETOF-2→(D,mix-2) in different branches, their enthalpy values ​​are as follows: The enthalpy values ​​of x-2) and electromagnetic throttle valve ETOF-5→(E,mix-3) are derived from the enthalpy values ​​of the fluid output from the bottom liquid phase outlet L of their respective upstream gas-liquid separator GLS; among them, OUT_2→(C,mix-1) of the branch medium-temperature stage condenser-evaporator CE_MTS is the enthalpy value of the outlet OUT_2 of the medium-temperature stage condenser-evaporator CE_MTS, and OUT_2→(D,mix-2) of the branch low-temperature stage condenser-evaporator CE_LTS is the enthalpy value of the outlet OUT_2 of the low-temperature stage condenser-evaporator CE_LTS.

[0102] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -40℃ in the cooling mode.

[0103] h C,mix-1 | -40℃ =h l,GLS-1 | -40℃ +h F,o | -40℃ ; Formula 10

[0104] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -80℃ in the cooling mode.

[0105] h C,mix-1 | -80℃ =h l,GLS-1 | -80℃ +h CE_MTS,OUT_2 | -80℃ , Formula 11

[0106] Enthalpy of the mixing point (D, mix-2)

[0107] h D,mix-2 | -80℃ =h l,GLS-2 | -80℃ +h F,o | -80℃ ; Formula 12

[0108] The enthalpy of the mixing point (C,mix-1) when the cabin temperature reaches -110℃ in the cooling mode.

[0109] h C,mix-1 | -110℃ =h l,GLS-1 | -110℃ +h CE_MTS,OUT_2 | -110℃ , Formula 13

[0110] Enthalpy of the mixing point (D, mix-2)

[0111] h D,min-2 | -110℃ =h l,GLS-2 | -110℃ +h CE_LTS,OUT_2 | -110℃ Formula 14

[0112] Enthalpy of the mixing point (E, mix-3)

[0113] h E,mix-3 | -110℃ =h l,GLS-3 | -110℃ +h F,o | -110℃ Formula 15

[0114] The enthalpy values ​​of the various stages of the condenser-evaporator are as follows: the high, medium, and low temperature stage condenser-evaporators each have four ends on both sides, consisting of two pairs of inlets and outlets; one side's inlet and outlet are the condensation side, and the other side's inlet and outlet are the evaporation side; the heat exchange capacity of the condenser-evaporator is...

[0115] Q CE =K·A·Δt m , Formula 16

[0116] According to the laws of conservation of mass and energy, the heat transfer on the condensing side is Q. cdEvaporation side heat exchange Q ev ,have

[0117] Q cd =Q ev =Q CE , Formula 17

[0118] The logarithmic mean temperature difference between the condenser and evaporator is:

[0119]

[0120] Where T cd,in This refers to the condenser-side inlet temperature of the condenser-evaporator, corresponding to the IN_1 port in the high-temperature stage condenser-evaporator CE_HTS, the medium-temperature stage condenser-evaporator CE_MTS, and the low-temperature stage condenser-evaporator CE_LTS; T cd,out This refers to the condenser-side outlet temperature of the evaporator, corresponding to the OUT_1 port in CE_HTS, CE_MTS, and CE_LTS mentioned above; T ev,in This refers to the inlet temperature on the evaporator side of the condenser-evaporator, corresponding to port IN_2 in CE_HTS, CE_MTS, and CE_LTS mentioned above; T ev,out This refers to the outlet temperature on the evaporator side of the condenser evaporator, corresponding to the OUT_2 port in CE_HTS, CE_MTS, and CE_LTS mentioned above.

[0121] The heat exchanger on the condensing side

[0122] Q cd =m cd ·(h cd,in -h cd,out ), Formula 19

[0123] m cd The refrigerant mass flow rate on the condenser side of the evaporator is kg / s.

[0124] h cd,in The enthalpy of the refrigerant at the condenser side of the evaporator is expressed in kJ / kg.

[0125] h cd,out The enthalpy of the refrigerant outlet on the condenser side of the evaporator is expressed in kJ / kg.

[0126] The heat exchange on the evaporation side

[0127] Q ev =m ev ·(h ev,in -h ev,out ). Formula 20

[0128] m ev The refrigerant mass flow rate on the evaporator side of the condenser-evaporator is kg / s.

[0129] h ev,in The enthalpy of the refrigerant outlet on the evaporator side of the condenser-evaporator is expressed in kJ / kg.

[0130] h ev,out The enthalpy of the refrigerant at the evaporator inlet on the condenser-evaporator side is expressed in kJ / kg.

[0131] The enthalpy of the evaporator is

[0132] Q EHX =K·A·Δt m =m EHX ·(h EHX,in -h EHX,out ) Formula 21

[0133] S3 determines the system operating parameters based on the thermodynamic parameters of the refrigeration system. At state point (A), the compressed non-azeotropic working fluid is divided into two fluid streams, with the liquid phase composition of the fluid passing through state point (B, i-mr) being Z. B,i-mr The fluid phase composition after bypassing state point (A,bp) is Z. A,bp The liquid phase component Z bypassed by the aforementioned state point (A,bp) A,bp Based on the Refprop10 refrigerant property database, according to ρ g =f(t,p,Z), where the fluid density ρ is determined by iteratively calculating the mass composition Z of the non-azeotropic refrigerant. g ρ collected by mass flow meter rt-g By approximating each other, the mass composition Z of the non-azeotropic working fluid bypassed at the current state point (A,bp) can be obtained. A,bp The fluid composition at state point (B, i-mr) can be obtained as Z. B,i-mr =ZZ A-bp .

[0134] The component is Z B,i-mr The two-phase non-azeotropic refrigerant enters the inlet (GLS-1,i) of the gas-liquid separator GLS-1. As shown in Formula 2 above, which calculates the mass composition of each component in the gas-liquid separation process, the mass composition Z of the fluid flowing out from the liquid phase outlet L after passing through the gas-liquid separator GLS-1 is... l,GLS And the mass composition Z of the fluid flowing out from the gas phase outlet G g,GLS This is related to the fluid temperature at the inlet (GLS-1,i) and the pressure within the gas-liquid separator GLS-1; by controlling the inlet temperature t of the gas-liquid separator GLS-1... GLS-1,i and the pressure P inside GLS-1 GLS-1 Real-time data acquisition, Z can be determined using Formula 2. l,GLS-1 and Z g,GLS-1Non-azeotropic refrigerants do not have chemical interactions with each other, and the separated components satisfy mass and energy balance. The mass composition of each component of the non-azeotropic refrigerant mixture can be determined using formula 4-6. and The energy values ​​of non-azeotropic refrigerant mixtures are determined using formula 7-8. and

[0135] According to the thermodynamic characteristics of the throttling valve, there is no mass loss of refrigerant and the enthalpy remains unchanged before and after throttling. The pressure and temperature change before and after throttling. When the liquid phase mixture flowing out of the liquid phase outlet L of the gas-liquid separator GLS-1 passes through the throttling valve TOF, there is no mass loss and the enthalpy remains unchanged.

[0136] During operation, the cooling temperature inside the cryotherapy chamber is determined by judging the current cooling operating mode of the refrigeration system, and the enthalpy h of the state point (C,mix-1) is determined by calculating the enthalpy values ​​at the mixing point of the high, medium, and low temperature stage condensers and evaporators. C,min-1 .

[0137] The following example uses -110℃; other temperatures will be explained later.

[0138] The enthalpy h of the obtained state point (C, mix-1) C,mix-1 The refrigerant inlet enthalpy at the inlet IN_2 of the evaporator side of the high-temperature stage condenser-evaporator CE_HTS corresponds to the enthalpy h at the evaporator side inlet during the enthalpy calculations for the high, medium, and low-temperature stage condensers-evaporators. cd,in The enthalpy of the evaporator side of the intermediate-temperature condenser-evaporator CE_MTS is calculated using Formula 20, and this is used to obtain the enthalpy h mentioned above. CE_MTS,OUT_2 | -110℃ .

[0139] When determining the enthalpy of the evaporator side of the intermediate-temperature condenser-evaporator CE_MTS, it is necessary to determine the enthalpy of the mixing point (D, mix-2). According to the flow chart, h needs to be calculated first. CE_MTS,OUT_2 | -110℃ Further requirements include obtaining the enthalpy value of the evaporator side of the condenser-evaporator CE_LTS, and then extrapolating it to the evaporator outlet temperature.

[0140] Example 2

[0141] A method and algorithm for determining the operating parameters of a cryotherapy chamber's refrigeration system, comprising the following steps;

[0142] S1; Sensors within the refrigeration system collect parameters, including a flow sensor that determines the fluid's mass composition by measuring fluid density, and pressure and temperature sensors used to determine the fluid's state parameters.

[0143] S2; Calculation of thermodynamic parameters of the refrigeration system of the cryotherapy chamber, including liquid refrigerant density, mass composition of each component in gas-liquid separation, enthalpy of the mixing point of each stage of condenser-evaporator, enthalpy of each stage of condenser-evaporator, and enthalpy of the evaporator.

[0144] S3; Determine system operating parameters based on the thermodynamic parameters of the refrigeration system, predict the circulation composition, cooling capacity and system COP, and achieve stable and efficient operation of the refrigeration system of the cryotherapy chamber based on the predicted actual operating parameters.

[0145] The system thermodynamic cycle includes the following steps;

[0146] The compressor RFC compresses the superheated non-azeotropic refrigerant vapor at state point (G,o) from low pressure to high pressure. It then enters the condenser CD via the main flow at state point (A) for partial condensation. A bypass (A,bp) at this point prevents the non-azeotropic refrigerant, after being pressurized by the compressor RFC, from having excessively high discharge pressure (Dis P) during the initial start-up or intermittent start-up of the refrigeration system. The two-phase flow of the non-azeotropic refrigerant enters the pressure and temperature control regenerator PTR via state point (B,i-mr). A bypass (B,i-bp_1 / B,i-bp_2 / B,i-bp_3) at this point controls the composition and concentration of the non-azeotropic refrigerant participating in the refrigeration cycle. The refrigerant temperature passing through the PTR via the bypass (B,i-bp_1 / B,i-bp_2 / B,i-bp_3) is lower than that of the two-phase flow of the non-azeotropic refrigerant entering via state point (B,i-mr). The PTR can further condense the non-azeotropic refrigerant entering via state point (B,i-mr). Non-azeotropic refrigerant G with initial mass ratio R290 / G R23 / G R14 =Z R290_initial / Z R23_initial / Z R14_initial The mass ratio G after bypassing (A,bp) R290 / G R23 / G R14 =Z R290_B,i-mr / Z R23_B,i-mr / Z R14_B,i-mrThe refrigerant enters the gas-liquid separator GLS-1 through state point (B,o); here it splits into two streams. The saturated vapor output from the top outlet G of GLS-1 is sent to the bypass (B,i-bp_1) of the PTR and IN_1 of the high-temperature stage condenser-evaporator CE_HTS. The liquid fluid output from the bottom outlet L of GLS-1 expands to a low pressure through the expansion valve TOF, and then mixes with the return vapor at state point (C,mix-1) before entering IN_2 of the high-temperature stage condenser-evaporator CE_HTS for condensation and subcooling of the non-azeotropic refrigerant that enters from IN_1 and exits through OUT_1 in the high-temperature stage condenser-evaporator CE_HTS. The mixed return refrigerant vapor output from OUT_2 of the high-temperature stage condenser-evaporator CE_HTS has a return mass ratio of G. R290 / G R23 / G R14 =Z R290_reflux / Z R23_reflux / Z R14_reflux The refrigerant mass ratio G that is mixed with the refrigerant vapor that is controlled to return through state point (G,i-mr) and through state point (G,i-bp) and then drawn into the compressor through state point (G,o) is G. R290 / G R23 / G R14 =Z R290_suction / Z R23_suction / Z R14_suction .

[0147] The further condensed and subcooled non-azeotropic refrigerant mixture flowing out from OUT_1 of the high-temperature stage condenser-evaporator CE_HTS passes through the gas-liquid separator GLS-2. Here, it is divided into two fluid streams. The saturated vapor output from the top outlet G of the gas-liquid separator GLS-2 is sent to the bypass (B,i-bp_2) of the PTR and the IN_1 of the medium-temperature stage condenser-evaporator CE_MTS. The liquid fluid output from the bottom outlet L of the gas-liquid separator GLS-2 can be expanded to low pressure by controlling the electromagnetic throttling valves ETOF-1 or ETOF-2 of the high-temperature stage solenoid valve group.

[0148] The refrigerant flows through state point (F,i) to the evaporative heat exchanger EHX via ETOF-1. This portion of the fluid is close to the boiling point of the liquid high-temperature refrigerant R290. Inside the evaporative heat exchanger EHX, the fluid absorbs heat from the internal space of the cryotherapy chamber and leaves EHX in a two-phase flow state at a temperature very close to that of the internal space of the cryotherapy chamber. The two-phase flow of refrigerant flowing out through state point (F,o) is controlled by the electronic expansion valve EXV-1 to ensure that the refrigerant flows back with a certain degree of superheat. At state point (C,mix-1), it mixes with the expanded low-pressure liquid refrigerant output from the bottom outlet L of the gas-liquid separator GLS-1. It is then drawn into the compressor through the above process. To avoid "liquid slugging," the fluid temperature of the refrigerant flowing back in a controlled manner at state point (G,i-bp) is controlled. After mixing with the refrigerant passing through state point (G,i-mr), the refrigerant is completely evaporated before entering the compressor.

[0149] After being mixed with the return vapor at state point (D, mix-2) via ETOF-2, the refrigerant enters IN_2 of the intermediate-temperature condenser-evaporator CE_MTS for condensation and subcooling. The non-azeotropic refrigerant entering from IN_1 and exiting via OUT_1 of the intermediate-temperature condenser-evaporator CE_MTS undergoes further condensation and subcooling. The further condensed and subcooled non-azeotropic mixture exiting OUT_1 of the intermediate-temperature condenser-evaporator CE_MTS passes through the gas-liquid separator GLS-3, where it is divided into two streams. The saturated vapor output from the top outlet G of GLS-3 is sent to the bypass (B, i-bp_3) of the PTR and to the intermediate-temperature condenser-evaporator IN_1 of CE_LTS. The liquid fluid output from the bottom outlet L of GLS-3 can be expanded to low pressure by controlling the electromagnetic throttling valves ETOF-4 or ETOF-5 of the intermediate-temperature solenoid valve group.

[0150] The refrigerant flows through state point (F,i) to the evaporative heat exchanger EHX via ETOF-4. This portion of the fluid is close to the boiling point of the liquid intermediate-temperature refrigerant R23. Inside the evaporative heat exchanger EHX, the fluid absorbs heat from the internal space of the cryotherapy chamber and leaves EHX in a two-phase flow state at a temperature very close to that of the internal space of the cryotherapy chamber. The two-phase flow of refrigerant flowing out through state point (F,o) is controlled by the electronic expansion valve EXV-2 to ensure that the refrigerant flows back with a certain degree of superheat. At state point (D,mix-2), it mixes with the expanded low-pressure liquid refrigerant output from the bottom outlet L of GLS-2. It is then drawn into the compressor through the above process. To avoid the phenomenon of "liquid slugging", the fluid temperature of the refrigerant flowing back in a controlled manner at state point (G,i-bp) is controlled so that after mixing with the refrigerant passing through state point (G,i-mr), the refrigerant is completely evaporated before entering the compressor.

[0151] After being mixed with the return vapor at state point (E,mix-3) via ETOF-5, the mixture enters the CE_LTS cryogenic condenser-evaporator IN_2 for condensation and subcooling of the non-azeotropic refrigerant that enters from IN_1 and exits via OUT_1. The further condensed and subcooled non-azeotropic mixture exiting from OUT_1 of CE_LTS results in a liquid fluid that can be controlled by the electromagnetic throttle valve ETOF-7 of the cryogenic stage solenoid valve group and flows through state point (F,i) to the evaporative heat exchanger EHX. This portion of the fluid is close to the boiling point of the liquid cryogenic refrigerant R14. Inside the evaporative heat exchanger EHX, the fluid absorbs heat from the internal space of the cryotherapy chamber and exits EHX in a two-phase flow state at a temperature very close to that of the internal space of the cryotherapy chamber. The two-phase refrigerant flowing out from state point (F,o) is controlled by the electronic expansion valve EXV-3 to ensure that the refrigerant returns at a certain superheat level, mixing with the expanded low-pressure liquid refrigerant output from the bottom outlet L of GLS-3 at state point (E,mix-3). This mixture is then drawn into the compressor through the above process. To avoid liquid slugging, the fluid temperature of the refrigerant flowing back at state point (G,i-bp) is controlled, ensuring that the refrigerant completely evaporates before entering the compressor after mixing with the refrigerant passing through state point (G,i-mr).

[0152] The refrigeration system controls the evaporation temperature of the evaporator heat exchanger by controlling the different proportions of the non-azeotropic refrigerant entering the state point (F,i) and flowing into the evaporator heat exchanger EHX, thereby controlling the refrigeration temperature in the cryotherapy chamber to provide different cooling effects.

[0153] Sensors installed within the refrigeration system collect parameters to participate in the calculation of system operating parameters. Flow sensors determine the fluid's mass composition by measuring fluid density, while pressure and temperature sensors determine the fluid's state parameters. Since the non-azeotropic refrigerants used in this system have no chemical interactions, the separated components maintain mass and energy balance.

[0154] The foregoing has shown and described the basic principles, main features, and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments. The embodiments and descriptions in the specification are merely preferred examples and are not intended to limit the invention. Various changes and modifications can be made to the present invention without departing from its novel spirit and scope, and all such changes and modifications fall within the scope of the present invention as claimed. The scope of protection of the present invention is defined by the appended claims and their equivalents.

Claims

1. A method and algorithm for determining the operating parameters of a cryotherapy chamber's refrigeration system, characterized in that, Includes the following steps: S1; Sensors within the refrigeration system collect parameters, including a flow sensor that determines the fluid's mass composition by measuring fluid density, and pressure and temperature sensors used to determine the fluid's state parameters. S2; Calculation of thermodynamic parameters of the refrigeration system of the cryotherapy chamber, including liquid refrigerant density, mass composition of each component in gas-liquid separation, enthalpy of the mixing point of each stage of condenser-evaporator, enthalpy of each stage of condenser-evaporator, and enthalpy of the evaporator. S3; Determine system operating parameters based on the thermodynamic parameters of the refrigeration system, predict the circulation composition, cooling capacity and system COP, and achieve stable and efficient operation of the refrigeration system of the cryotherapy chamber based on the predicted actual operating parameters.

2. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 1, characterized in that, The density of the liquid refrigerant is determined based on the Refprop10 refrigerant property database, which is used to evaluate the thermodynamic properties of the non-azeotropic refrigerants R-290 / R-23 / R-14. The equation for determining the property parameters using the Refprop10 database is (h,ρ,x,t…..)=f('p1','p2',Z), where Z is the mass composition of the non-azeotropic refrigerant, based on the refrigerant charge G. R290 / G R23 / G R14 =Z R290_initial / Z R23_initial / Z R14_initial The parameters p1 and p2 to be determined are obtained through system sensors; p1 and p2 are the collected temperature and pressure parameters, respectively.

3. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 1, characterized in that, The parameters of the mass composition of each component in the gas-liquid separation are determined. The phase separation in the gas-liquid separator can be calculated using Bell & Deiters correlation, according to the separation rules provided in Refprop10. The mass composition of the saturated liquid and vapor in equilibrium is determined by the pressure and inlet mass composition of the gas-liquid separator as [Z]. l,GLS Z g,GLS ]=f(p i (Z) Non-azeotropic refrigerants have no chemical interactions with each other, and the separated components satisfy mass and energy balance. Liquid phase mass, Gas phase quality; The non-azeotropic refrigerant mixture has a balanced mass of all components. In this non-azeotropic refrigerant mixture, the energy of each component is balanced.

4. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 1, characterized in that, The mixing point enthalpy values ​​of the various stages of condenser-evaporators in the refrigeration system are (C,mix-1), (D,mix-2), and (E,mix-3) for the high, medium, and low temperature stages of the condenser-evaporator, respectively. The mixing point (C,mix-1) is formed by the branch throttling valve TOF→(C,mix-1), the electronic expansion valve EXV-1→(C,mix-1), and the OUT_2→(C,mix-1) of the medium temperature stage condenser-evaporator CE_MTS. The mixing point (D,mix-2) is formed by the branch electromagnetic throttling valve ETOF-2→(D,mix-2), the electronic expansion valve EXV-2→(D,mix-2), and the OUT_2→(D,mix-2) of the low temperature stage condenser-evaporator CE_LTS. The system consists of two mixing points: (C, mix-2) and (D, mix-3). The mixing point (E, mix-3) is composed of the electromagnetic throttle valve ETOF-5→(E, mix-3) and the electronic expansion valve EXV-3→(D, mix-2). Different mixing points and the number of mixing points correspond to different refrigeration temperatures. For refrigeration at -40℃ cabin temperature, the mixing point in the refrigeration cycle of the refrigeration system is (C, mix-1). For refrigeration at -80℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1) and (D, mix-2). For refrigeration at -110℃ cabin temperature, the mixing points in the refrigeration cycle of the refrigeration system are (C, mix-1), (D, mix-2), and (E, mix-3).

5. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 4, characterized in that, The cooling system at -40℃ cabin temperature involves the following branches at the mixing point (C,mix-1): throttle valve TOF → (C,mix-1) and electronic expansion valve EXV-1 → (C,mix-1). For cooling at an internal temperature of -80℃, the branches involved in mixing at the mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate temperature stage condenser evaporator CE_MTS; the branches involved in mixing at the mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and electronic expansion valve EXV-2→(D,mix-2). For cooling at an internal temperature of -110℃, the branches involved in mixing at mixing point (C,mix-1) are: throttle valve TOF→(C,mix-1) and OUT_2→(C,mix-1) of the intermediate-temperature condenser-evaporator CE_MTS; the branches involved in mixing at mixing point (D,mix-2) are: electromagnetic throttle valve ETOF-2→(D,mix-2) and OUT_2→(D,mix-2) of the low-temperature condenser-evaporator CE_LTS; the branches involved in mixing at mixing point (E,mix-3) are: electromagnetic throttle valve ETOF-5→(E,mix-3) and EXV-3→(D,mix-2). For the electronic expansion valves EXV-1→(C,mix-1), EXV-1→(D,mix-2), and EXV-1→(D,mix-2) in different branches, their enthalpy values ​​are the enthalpy values ​​of the evaporative heat exchanger EHX passing through the state point (F,o). There is no mass loss and the enthalpy value remains unchanged before and after the electronic expansion valves EXV-1 / EXV-2 / EXV-3. For the throttling valves TOF→(C,mix-1) and ETOF-2→(D,mix-2) in different branches, their enthalpy values ​​are as follows: The enthalpy values ​​of x-2) and electromagnetic throttle valve ETOF-5→(E,mix-3) are derived from the enthalpy values ​​of the fluid output from the bottom liquid phase outlet L of their respective upstream gas-liquid separator GLS; among them, OUT_2→(C,mix-1) of the branch medium-temperature stage condenser-evaporator CE_MTS is the enthalpy value of the outlet OUT_2 of the medium-temperature stage condenser-evaporator CE_MTS, and OUT_2→(D,mix-2) of the branch low-temperature stage condenser-evaporator CE_LTS is the enthalpy value of the outlet OUT_2 of the low-temperature stage condenser-evaporator CE_LTS.

6. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 5, characterized in that, When the cabin temperature reaches -40℃ in the cooling mode, the enthalpy h of the mixing point (C,mix-1) is... C,mix-1 | -40℃ =h l,GLS-1 | -40℃ +h F,o | -40℃ When the cabin temperature reaches -80℃ in the cooling mode, the enthalpy h of the mixing point (C,mix-1) is... C,mix-1 | -80℃ =h l,GLS-1 | -80℃ +h CE_MTS,OUT_2 | -80℃ The enthalpy h of the mixing point (D, mix-2) D,mix-2 | -80℃ =h l,GLS-2 | -80℃ +h F,o | -80℃ When the cabin temperature reaches -110℃ in the cooling mode, the enthalpy h of the mixing point (C,mix-1) is... C,mix-1 | -110℃ =h l,GLS-1 | -110℃ +h CE_MTS,OUT_2 | -110℃ The enthalpy h of the mixing point (D, mix-2) D,mix-2 | -110℃ =h l,GLS-2 | -110℃ +h CE_LTS,OUT_2 | -110℃ The enthalpy h of the mixing point (E, mix-3) E,mix-3 | -110℃ =h l,GLS-3 | -110℃ +h F,o | -110℃ .

7. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 1, characterized in that, The enthalpy values ​​of the various stages of the condenser-evaporator are as follows: the high, medium, and low temperature stage condenser-evaporators each have four ends on both sides, consisting of two pairs of inlets and outlets; one side's inlet and outlet are the condensation side, and the other side's inlet and outlet are the evaporation side; the heat exchange capacity of the condenser-evaporator is Q. CE =K·A·Δt m According to the laws of conservation of mass and energy, the heat transfer on the condensing side is Q. cd Evaporation side heat exchange Q ev Q cd =Q ev =Q CE The logarithmic mean temperature difference between the condenser and evaporator is... The heat exchange on the condensing side Q cd =m cd ·(h cd,in -h cd,out The heat exchange on the evaporation side, Q ev =m ev ·(h ev,in -h ev,out ).

8. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to claim 1, characterized in that, The enthalpy of the evaporator is Q. EHX =K·A·Δt m =m EHX ·(h EHX,in -h EHX,out ).

9. The method and algorithm for determining the operating parameters of the cryotherapy chamber refrigeration system according to any one of claims 1 to 8, characterized in that, S3 determines the system operating parameters based on the thermodynamic parameters of the refrigeration system. At state point (A), the compressed non-azeotropic working fluid is divided into two fluid streams, with the liquid phase composition of the fluid passing through state point (B, i-mr) being Z. B,i-mr The fluid phase composition after bypassing state point (A,bp) is Z. A,bp ; Liquid phase component Z bypassed by the state point (A,bp) A,bp Based on the Refprop10 refrigerant property database, according to ρ g =f(t,p,Z), where the fluid density ρ is determined by iteratively calculating the mass composition Z of the non-azeotropic refrigerant. g ρ collected by mass flow meter rt-g By approximating each other, the mass composition Z of the non-azeotropic working fluid bypassed at the current state point (A,bp) can be obtained. A,bp The fluid composition at state point (B, i-mr) can be obtained as Z. B,i-mr =ZZ A-bp ; The component is Z B,i-mr The two-phase non-azeotropic refrigerant enters the inlet (GLS-1,i) of the gas-liquid separator GLS-1. Based on the formula used to calculate the mass composition of each component in the gas-liquid separation process, the mass composition Z of the fluid flowing out from the liquid phase outlet L after passing through the gas-liquid separator GLS-1 is as follows: l,GLS And the mass composition Z of the fluid flowing out from the gas phase outlet G g,GLS This is related to the fluid temperature at the inlet (GLS-1,i) and the pressure within the gas-liquid separator GLS-1; by controlling the inlet temperature t of the gas-liquid separator GLS-1... GLS-1,i and the pressure P inside GLS-1 GLS-1 Real-time data collection can determine Z. l,GLS-1 and Z g,GLS-1 Non-azeotropic refrigerants do not have chemical interactions, and the separated components satisfy mass and energy balance. Therefore, the mass composition of each component in the non-azeotropic refrigerant mixture can be determined. and Determine the energy values ​​of each non-azeotropic refrigerant mixture. and 10. As described in claim 1, characterized in that, According to the thermodynamic characteristics of the throttling valve, there is no mass loss of refrigerant and the enthalpy remains unchanged before and after throttling. The pressure and temperature change before and after throttling. When the liquid phase mixture flowing out of the liquid phase outlet L of the gas-liquid separator GLS-1 passes through the throttling valve TOF, there is no mass loss and the enthalpy remains unchanged.

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