CN112287579B - Binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution - Google Patents
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Abstract
The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution is used for developing the refrigeration performance of the binary non-azeotropic mixed working medium in the condensation or evaporation process, the mass and energy transfer relational expression between the whole binary non-azeotropic mixed working medium and a gas phase and a liquid phase in the condensation or evaporation process of the two components is set according to the difference ratio between the ideal equilibrium state and the actual state of the component contents of the two components of the binary non-azeotropic mixed working medium in the condensation or evaporation process as the ratio of the condensation or evaporation rates of the two components, and finally the heat exchange coefficients of the two components of the binary non-azeotropic mixed working medium and the component distribution map in equipment are obtained; the method can be used for two-dimensional model calculation and three-dimensional model calculation, and can save the research and development cost and period of the binary non-azeotropic mixed working medium.
Description
Technical Field
The invention relates to the technical field of thermodynamics and heating ventilation air conditioners, in particular to a binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution.
Technical Field
The refrigerating working medium is blood of a refrigerating air-conditioning system, and is mainly used in the fields of heating ventilation air-conditioning such as household air-conditioning, automobile air-conditioning, water chilling unit systems and the like. The refrigeration working media mainly comprise two categories of pure working media and mixed working media, and the refrigeration working media influencing global warming gradually face to be eliminated along with the rise of environmental protection requirements in recent years; however, it is also not wise to simply pursue the effect of the refrigeration duty on global warming and ignore its refrigeration performance. Compared with pure working medium, the binary mixed working medium can not only reduce the effect of the working medium on global warming, but also maintain the refrigeration performance, so that the binary mixed working medium is selected as an excellent alternative method.
The refrigeration performance of the binary mixed working medium is obviously influenced by the mixing proportion of the binary mixed working medium, however, as the types and the mixing proportion of the mixed working medium are numerous, the refrigeration performance of the binary mixed working medium is estimated by simply adopting an experimental measurement method, so that a large amount of time and economic cost are spent, and the significance of the prediction method for researching the refrigeration performance of the binary mixed working medium is great. The binary mixed working medium comprises an azeotropic working medium and a non-azeotropic working medium, the condensation temperature and the evaporation temperature of the azeotropic working medium are the same, and when the condensation or evaporation phenomenon occurs, the content ratio of the two components in the gas phase and the liquid phase does not change and is always equal to the content ratio in the initial mixed state; the condensation temperature and the evaporation temperature of the non-azeotropic working medium are different, and the content ratio of two components in a gas phase and a liquid phase can be changed continuously when the phenomenon of condensation or evaporation occurs, so that the calculation of the condensation or evaporation rate of the two components of the binary non-azeotropic mixed working medium has certain difficulty.
In the existing scientific research and production process, a binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution is lacked, and refrigeration performance parameters such as a component distribution map, a heat exchange coefficient and the like of the binary non-azeotropic mixed working medium in equipment cannot be obtained.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution, which can calculate the rate ratio of two components in the condensation or evaporation process of a binary non-azeotropic mixed working medium mixed in any proportion, and further combines a finite element simulation technology to obtain the refrigeration performance parameters such as a component distribution diagram, a heat exchange coefficient and the like of the binary non-azeotropic mixed working medium in equipment.
In order to achieve the purpose, the invention adopts the technical scheme that:
the binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution comprises the following steps of:
1) According to the type, initial ratio and pressure of the binary non-azeotropic mixed working medium A-B, consulting and calculating software NIST to draw a 'saturation temperature-mass fraction' diagram of the binary non-azeotropic mixed working medium A-B under a certain fixed pressure;
2) When binary non-azeotropic mixture is usedWhen the temperature of the binary A-B is higher than the dew point temperature or lower than the bubble point temperature, setting the condensation or evaporation rate ratio of the binary non-azeotropic mixed working medium A-B as the mass fraction ratio of the mixed working medium in the initial filling state, wherein the condensation or evaporation amount of the component A and the component B of the binary non-azeotropic mixed working medium A-B occupies the ratio alpha of the total condensation or evaporation amount of the binary non-azeotropic mixed working medium A-B A And alpha B Respectively as follows:
α A represents the ratio of the condensation or evaporation capacity of the component A to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B, alpha B Represents the ratio of the condensation or evaporation capacity of the component B to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B, w 0 The component B occupies the mass ratio of the total binary non-azeotropic mixed working medium A to B in the initial filling state;
at the moment, the saturation temperature of the binary non-azeotropic mixed working medium A-B is set as follows:
T sat the saturated temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fraction of the component A and the component B in the initial filling state is a fixed value; when the evaporation process is calculated, the dew point temperature corresponding to the mass fractions of the component A and the component B in the initial mixing state is a fixed value; p represents the pressure of the binary non-azeotropic mixed working medium A-B and is set as a constant value in the whole calculation process;
when the temperature of the binary non-azeotropic mixed working medium A-B is lower than the dew point temperature and higher than the bubble point temperature, setting the condensation or evaporation rate ratio of the binary non-azeotropic mixed working medium A-B as delta m A /Δm B ，Δm A And Δ m B Is based on the following formula:
Δm A represents the difference between the actual mass of component A in the gas phase and the ideal equilibrium mass, Δ m B Represents the difference between the mass of component B in the gas phase in the actual state and the mass in the ideal equilibrium state, m is the total mass x of binary non-azeotropic mixed working medium A-B 3 Dryness, x, of an ideal equilibrium state 3 Is the dryness of the actual state, w 3” Is the mass fraction of component B in the gas phase at the ideal equilibrium state, w 3” Is the mass fraction of component B in the gas phase in the actual state;
the condensation or evaporation capacity of the component A and the component B of the binary non-azeotropic mixed working medium A-B occupies the ratio alpha of the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B A And alpha B Respectively as follows:
at the moment, the saturation temperature of the binary non-azeotropic mixed working medium A-B is set as follows:
T sat the saturation temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fraction of the component A and the component B in the actual calculation process is a variable; when the evaporation process is calculated, the dew point temperature corresponding to the mass fractions of the component A and the component B in the actual calculation process is a variable; w is the ratio of the component B to the total binary non-azeotropic mixed working medium A-B in the actual calculation process;
3) Obtaining alpha A And alpha B Then, combining with finite element simulation software FLUENT, selecting a component transportation model, a VOF two-phase flow model and an SST turbulence model, and using the form of source items to mix the binary non-azeotropic mixed working media A-B and the components A and A thereofThe mass and energy transfer between the components B are set according to the following formula, and the heat exchange coefficient of the binary non-azeotropic mixed working medium A-B and the component distribution diagram of the component A and the component B in the equipment are obtained by carrying out calculation.
If the temperature of the binary non-azeotropic mixed working medium A-B is higher than the saturation temperature, the mass transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula (I), the compound is shown in the specification,
represents the mass transfer of the gas phase of component a,
represents the mass transfer amount of the liquid phase of component a,
represents the mass transfer of the gas phase of component B,
represents the mass transfer of the liquid phase of component B, r the condensing evaporation coefficient is 0.01-3000000, beta l Represents the volume fraction, rho, of the liquid phase of the binary non-azeotropic mixed working medium A-B l Expressing the density of the liquid phase of the binary non-azeotropic mixed working medium A-B, T expressing the temperature of the binary non-azeotropic mixed working medium A-B, T sat Representing the saturation temperature of the binary non-azeotropic mixed working medium A-B.
If the temperature of the binary non-azeotropic mixed working medium A-B is lower than the saturation temperature, the mass transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula, beta ν Representing the volume fraction, rho, of the binary non-azeotropic mixed working medium A-B gas phase ν The density of the gas phase of the binary non-azeotropic mixed working medium A-B is shown.
The energy transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula, E A Represents the amount of energy transfer of component a,
denotes the mass transfer of the liquid phase of component A, γ A Denotes the latent heat of component A, E B Represents the amount of energy transfer of component B,
denotes the mass transfer of the liquid phase of component B, γ B The latent heat of the component B is shown, and E represents the total energy transfer of the binary non-azeotropic mixed working medium A-B.
The two components of the binary non-azeotropic mixed working medium A-B are refrigeration working media or low-temperature working media, the refrigeration working media are R22, R32, R123, R125, R134a, R152a, R161, R1234yf and R1234ze (E), and the low-temperature working media are methane, ethane, propane and butane.
The ideal equilibrium state in the step 2) refers to the state of the binary non-azeotropic mixed working medium A-B at each temperature in the saturation temperature-mass fraction graph under a certain fixed pressure in the step 1), the bubble point temperature is selected by calculation in the condensation process, and the dew point temperature is selected by calculation in the evaporation process.
The binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution is used for two-dimensional model calculation and can also be used for three-dimensional model calculation.
The invention has the beneficial effects that: the invention has wide application range, can obtain the refrigeration performance such as component distribution diagram, heat exchange coefficient and the like of the binary non-azeotropic mixed working medium in the equipment, provides reference for researching the performance of the novel binary non-azeotropic mixed working medium, and saves the research and development cost and period of the novel binary non-azeotropic mixed working medium.
Drawings
FIG. 1 is a flow chart of the present invention.
FIG. 2 is a diagram of "saturation temperature-mass fraction" of binary zeotropic mixture working fluids A-B in the examples.
Detailed Description
The invention will be described in detail below by taking the condensation and evaporation of a mixture of binary non-azeotropic mixture R1234ze (E) and R32 as an example with reference to the attached drawings.
As shown in FIG. 1, the binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution comprises the following steps:
1) According to the type, initial ratio and pressure reference calculation software NIST of the binary non-azeotropic mixed working medium A-B, drawing a 'saturation temperature-mass fraction' diagram of the binary non-azeotropic mixed working medium A-B under a certain fixed pressure, as shown in figure 2, a component A is R1234ze (E), a component B is R32, the left side of an abscissa represents the mass fraction of the component R1234ze (E), the right side represents the mass fraction of the component R32, the ordinate represents the temperature of the binary non-azeotropic mixed working medium, a solid line represents the bubble point temperature, and a dotted line represents the dew point temperature; the initial mixture ratio is 54 percent of R1234ze (E) and 46 percent of R32 by mass, and the pressure is 1.74MPa;
in FIG. 2 point 1 is superheated vapor, point 2 or 2 "is saturated vapor, point 2 'is saturated liquid, point 4 or 4' is saturated liquid, point 4" is saturated gas, and point 5 is subcooled liquid; a point 3 between the points 2 and 4 is in a gas-liquid coexisting state;
2) When the temperature of the binary non-azeotropic mixed working medium is higher than the dew point temperature, the binary non-azeotropic mixed working medium is in a superheated steam state, namely a state of point 1, and the condensation or evaporation rate ratio of A-B of the binary non-azeotropic mixed working medium is set as the mass fraction ratio (0.54/0.46) of the mixed working medium in the initial filling state; when the temperature of the binary non-azeotropic mixed refrigerant is lower than the bubble point temperature, the binary non-azeotropic mixed refrigerant is in a supercooled liquid state, namely a state of point 5, and the condensation or evaporation rate ratio of A-B of the binary non-azeotropic mixed refrigerant is set to be in an initial charging stateThe mass fraction ratio of the mixed working medium is that the condensation quantity of the component A and the component B of the binary non-azeotropic mixed working medium occupies the ratio alpha of the total condensation quantity of the binary non-azeotropic mixed working medium A And alpha B Respectively as follows:
α A represents the ratio of the condensation or evaporation capacity of the component A to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B, alpha B The ratio of the condensation or evaporation capacity of the component B to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B is expressed;
in addition, the saturation temperature of the binary non-azeotropic mixed working medium is set as follows:
T sat the saturated temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fractions of the component A and the component B in the initial filling state is a fixed value; when the evaporation process is calculated, the dew point temperature corresponding to the mass fractions of the component A and the component B in the initial filling state is a fixed value;
when the temperature of the binary non-azeotropic mixed working medium is lower than the dew point temperature and higher than the bubble point temperature, the binary non-azeotropic mixed working medium is in a gas-liquid coexisting state, namely a state of point 3, and the mass fraction ratio of the component A to the component B is changed all the time; point 3 is an ideal equilibrium state, the mass fraction of point 3 in the liquid phase is a value corresponding to point 3', and the mass fraction in the gas phase is a value corresponding to point 3 ″; however, in the actual iterative calculation process, its mass fraction in the liquid phase is a value corresponding to point 3' and its mass fraction in the gas phase is a point3”The corresponding value is not in an equilibrium state; thus setting the actual state (point) of its two components A and B3’And point3”) The ratio of the difference from the ideal equilibrium state (point 3 'and point 3') is taken as the condensation or evaporation rate of component A and component BRatio Δ m A /Δm B ，Δm A And Δ m B Is based on the following formula:
m is the total mass, x, of the binary non-azeotropic mixed working medium 3 Is the dryness, x, of an ideal equilibrium state 3 Is the dryness of the actual state, w 3” Is the mass fraction of component B in the gas phase at the ideal equilibrium state, w 3” Is the mass fraction of component B in the gas phase in the actual state; the ideal equilibrium state refers to the state of the binary non-azeotropic mixed working medium at each temperature in the saturation temperature-mass fraction diagram at the working pressure in the step 1), the bubble point temperature is selected by calculation in the condensation process, and the dew point temperature is selected by calculation in the evaporation process;
the condensation or evaporation capacity of the components A and B of the binary non-azeotropic mixed working medium A-B occupies the ratio alpha of the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B A And alpha B Respectively as follows:
Δm A represents the difference between the actual mass of component A in the gas phase and the ideal equilibrium mass, Δ m B Represents the difference between the actual state mass of component B in the gas phase and the ideal equilibrium state mass;
at this time, the saturation temperature of the binary non-azeotropic mixed working medium A-B is set to be
T sat The saturated temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fraction of the components A and B in the actual calculation process is a variable; when the evaporation process is to be calculated,the dew point temperature corresponding to the mass fraction of the components A and B in the actual calculation process is a variable; w is the ratio of the component B to the total binary non-azeotropic mixed working medium A-B in the actual calculation process;
3) Obtaining alpha A And alpha B Then, combining with finite element simulation software FLUENT, selecting a component transportation model, a VOF two-phase flow model and an SST turbulence model, and setting the binary non-azeotropic mixed working medium A-B and the mass and energy transfer between the component A and the component B thereof according to the following formula in the form of source terms:
if the temperature of the binary non-azeotropic mixed working medium is higher than the saturation temperature, the mass transfer amounts of the component A, B and the binary non-azeotropic mixed working medium gas phase and liquid phase are as follows:
in the formula (I), the compound is shown in the specification,
represents the mass transfer of the gas phase of component a,
represents the mass transfer amount of the liquid phase of component a,
represents the mass transfer of the gas phase of component B,
the mass transfer amount of the liquid phase of component B is represented, and r represents the condensation evaporation coefficient, and is usually 0.01-3000000, beta l Represents the volume fraction, rho, of the liquid phase of the binary non-azeotropic mixed working medium A-B l Expressing the density of the liquid phase of the binary non-azeotropic mixed working medium A-B, T expressing the temperature of the binary non-azeotropic mixed working medium A-B, T sat Representing the saturation temperature of the binary non-azeotropic mixed working medium A-B;
if the temperature of the binary non-azeotropic mixed working medium is lower than the saturation temperature, the mass transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B gas phase and liquid phase are as follows:
in the formula, beta ν Representing the volume fraction, rho, of the binary non-azeotropic mixed working medium A-B gas phase ν Representing the density of the gas phase of the binary non-azeotropic mixed working medium A-B;
the energy transfer capacity of the component A, B and the binary non-azeotropic mixed working medium gas phase and liquid phase is as follows:
in the formula, E A Represents the amount of energy transfer of component a,
denotes the mass transfer of the liquid phase of component A, γ A Denotes the latent heat of component A, E B Represents the amount of energy transfer of component B,
denotes the mass transfer of the liquid phase of component B, γ B The latent heat of the component B is expressed, and the E represents the total energy transfer amount of the binary non-azeotropic mixed working medium;
and carrying out calculation to obtain the heat exchange coefficient of the binary non-azeotropic mixed working medium and the component distribution diagram of the component A and the component B in the equipment.
Claims (7)
1. The binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution is characterized by comprising the following steps of:
1) According to the type, initial ratio and pressure of the binary non-azeotropic mixed working medium A-B, consulting and calculating software NIST to draw a 'saturation temperature-mass fraction' diagram of the binary non-azeotropic mixed working medium A-B under a certain fixed pressure;
2) When the temperature of the binary non-azeotropic mixed working medium A-B is higher than dewSetting the condensation or evaporation rate ratio of the binary non-azeotropic mixed working medium A-B as the mass fraction ratio of the mixed working medium in the initial filling state when the point temperature is lower than or equal to the bubble point temperature, wherein the condensation or evaporation amount of the component A and the component B of the binary non-azeotropic mixed working medium A-B occupies the ratio alpha of the total condensation or evaporation amount of the binary non-azeotropic mixed working medium A-B A And alpha B Respectively as follows:
α A represents the ratio of the condensation or evaporation capacity of the component A to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B, alpha B Represents the ratio of the condensation or evaporation capacity of the component B to the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B, w 0 The component B occupies the mass ratio of the total binary non-azeotropic mixed working medium A to B in the initial filling state;
at the moment, the saturation temperature of the binary non-azeotropic mixed working medium A-B is set as follows:
T sat the saturated temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fraction of the component A and the component B in the initial filling state is a fixed value; when the evaporation process is calculated, the dew point temperature corresponding to the mass fractions of the component A and the component B in the initial filling state is a fixed value; p represents the pressure of the binary non-azeotropic mixed working medium A-B and is set as a constant value in the whole calculation process;
when the temperature of the binary non-azeotropic mixed working medium A-B is lower than the dew point temperature and higher than the bubble point temperature, setting the condensation or evaporation rate ratio of the binary non-azeotropic mixed working medium A-B as Deltam A /Δm B ，Δm A And Δ m B Is based on the following formula:
Δm A represents the difference between the actual mass of component A in the gas phase and the ideal equilibrium mass, Δ m B Represents the difference between the actual mass of component B in the gas phase and the ideal equilibrium mass. m is the total mass of binary non-azeotropic mixed working medium A-B, x 3 Dryness, x, of an ideal equilibrium state 3 Is the dryness of the actual state, w 3” Is the mass fraction of component B in the gas phase at the ideal equilibrium state, w 3” Is the mass fraction of component B in the gas phase in the actual state;
the condensation or evaporation capacity of the component A and the component B of the binary non-azeotropic mixed working medium A-B occupies the ratio alpha of the total condensation or evaporation capacity of the binary non-azeotropic mixed working medium A-B A And alpha B Respectively as follows:
at the moment, the saturation temperature of the binary non-azeotropic mixed working medium A-B is set as follows:
T sat the saturation temperature of the binary non-azeotropic mixed working medium A-B is represented, and when the condensation process is calculated, the bubble point temperature corresponding to the mass fraction of the component A and the component B in the actual calculation process is a variable; when calculating the evaporation process, the dew point temperature corresponding to the mass fraction of the component A and the component B in the actual calculation process is a variable; w is the ratio of the component B to the total binary non-azeotropic mixed working medium A-B in the actual calculation process;
3) Obtaining alpha A And alpha B Then, combining with finite element simulation software FLUENT, selecting a component transportation model, a VOF two-phase flow model and an SST turbulence model, and mixing binary non-azeotropy in a source term modeThe working medium A-B and the mass and energy transfer between the component A and the component B are set according to the following formula, and the heat exchange coefficient of the binary non-azeotropic mixed working medium A-B and the component distribution diagram of the component A and the component B in the equipment are obtained by calculation.
2. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: if the temperature of the binary non-azeotropic mixed working medium A-B is higher than the saturation temperature, the mass transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula (I), the compound is shown in the specification,
represents the mass transfer of the gas phase of component a,
represents the mass transfer amount of the liquid phase of component a,
represents the mass transfer of the gas phase of component B,
represents the mass transfer amount of the liquid phase of component B, r the condensing evaporation coefficient is 0.01-3000000, beta l Represents the volume fraction, rho, of the liquid phase of the binary non-azeotropic mixed working medium A-B l Expressing the density of the liquid phase of the binary non-azeotropic mixed working medium A-B, T expressing the temperature of the binary non-azeotropic mixed working medium A-B, T sat Representing the saturation temperature of the binary non-azeotropic mixed working medium A-B.
3. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: if the temperature of the binary non-azeotropic mixed working medium A-B is lower than the saturation temperature, the mass transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula, beta ν Representing the volume fraction, rho, of the binary non-azeotropic mixed working medium A-B gas phase ν The density of the gas phase of the binary non-azeotropic mixed working medium A-B is shown.
4. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: the energy transfer amounts of the component A, the component B and the binary non-azeotropic mixed working medium A-B in gas phase and liquid phase are as follows:
in the formula, E A Represents the amount of energy transfer of component a,
denotes the mass transfer of the liquid phase of component A, γ A Denotes the latent heat of component A, E B Represents the amount of energy transfer of component B,
denotes the mass transfer of the liquid phase of component B, γ B The latent heat of the component B is expressed, and the E expresses the total energy transfer of the binary non-azeotropic mixed working medium A-B.
5. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: the two components of the binary non-azeotropic mixed working medium A-B are refrigeration working media or low-temperature working media, the refrigeration working media are R22, R32, R123, R125, R134a, R152a, R161, R1234yf and R1234ze (E), and the low-temperature working media are methane, ethane, propane and butane.
6. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: the ideal equilibrium state in the step 2) refers to the state of the binary non-azeotropic mixed working medium A-B at each temperature in the 'saturation temperature-mass fraction' diagram under a certain fixed pressure in the step 1), the bubble point temperature is selected in the calculation of the condensation process, and the dew point temperature is selected in the calculation of the evaporation process.
7. The binary non-azeotropic mixed working medium condensation and evaporation simulation method considering component distribution according to claim 1, wherein: the binary non-azeotropic mixed working medium condensation evaporation simulation method considering component distribution is used for two-dimensional model calculation and can also be used for three-dimensional model calculation.
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| 非共沸工质R134a/R245fa的管内冷凝换热特性研究;张永欣等;《工程热物理学报》;20200315(第03期);全文 * |
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