CN112182849B - Method and device for analyzing heat exchange after re-submerging criticality - Google Patents
Method and device for analyzing heat exchange after re-submerging criticality Download PDFInfo
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Abstract
The disclosure belongs to the technical field of nuclear power maintenance, and particularly relates to a method and a device for analyzing heat exchange after re-submergence criticality. According to the method, the foaming area near the quenching front edge is removed from the critical post-heat exchange area, so that the complex heat exchange mechanism of the foaming area is avoided, the interference on the heat exchange analysis of other areas at the downstream of the quenching front edge is avoided, and the heat exchange condition of the downstream area of the foaming area near the quenching front edge can be analyzed more reasonably. In addition, the embodiment of the disclosure subdivides the area downstream of the foaming area near the quenching front into a plurality of sub-areas, and determines the heat exchange amount of each sub-area according to the heat exchange mode of the sub-area, so that the critical post-heat exchange can be more finely simulated, and the cladding peak temperature and the quenching front advancing rate of the re-submerging process can be more accurately simulated. The analysis method for heat exchange after re-submergence criticality is applied to the development process of the analysis program of the Chinese autonomy loss of coolant accident, and lays a foundation for analysis of loss of coolant accident of a pressurized water reactor power station.
Description
Technical Field
The invention belongs to the technical field of nuclear power maintenance, and particularly relates to a method and a device for analyzing heat exchange after re-submergence criticality.
Background
The re-submerging process of the loss-of-coolant accident of the nuclear power plant is a very important stage of the local accident of the nuclear power plant, and the re-submerging process relates to a complex two-phase flow heat exchange process, so a large amount of experimental research and model research are developed in recent decades domestically and abroad to explore the complex flow heat exchange in the re-submerging process, and large-scale system programs such as RELAP5, CATARE, COBRA-TF and the like are developed to simulate the re-submerging process of the loss-of-coolant accident.
Compared with the common two-phase flow heat exchange condition, the re-submerging process is more special and mainly embodied as follows: the working condition characteristics of low pressure and low flow, the heat exchange after critical is dominant, and the axial heat conduction importance is higher. Among these, developing a critical post heat exchange module suitable for low pressure low flow conditions is particularly important because it is directly related to estimation of the peak cladding temperature and simulation of the quench front advance process. Due to the above factors, the simulation error of the critical post-heat exchange model in the current analysis and simulation of the loss of coolant accident on the critical post-submergence heat exchange is large, so that the accuracy of the simulation on the critical post-submergence heat exchange needs to be improved urgently.
Disclosure of Invention
In order to overcome the problems in the related art, a heat exchange analysis method and a heat exchange analysis device after re-submerging criticality are provided.
According to an aspect of an embodiment of the present disclosure, there is provided a method for analyzing heat exchange after re-flooding criticality, the method including:
determining a foaming area near the quenching front edge of the inner wall of the channel to be detected according to the flow velocity of the re-submerging inlet of the channel to be detected;
determining a region of the channel to be detected, which is located at the downstream of the foaming region near the quenching front edge, as a region to be detected, wherein the region to be detected is divided into a plurality of sub-regions;
determining a heat exchange mode of each sub-region;
and aiming at each sub-region, determining the heat exchange quantity of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region.
In one possible implementation manner, determining, for each sub-region, a heat exchange mode of the sub-region includes:
for each sub-region, determining the minimum film boiling temperature corresponding to the sub-region according to the thermodynamic parameters of the inner wall of the sub-region, the thermodynamic parameters of the liquid in the control body corresponding to the sub-region and the thermodynamic parameters of the gas in the control body corresponding to the sub-region;
determining that the heat exchange mode of the sub-region is film boiling under the condition that the wall surface temperature of the sub-region is greater than or equal to the minimum film boiling temperature corresponding to the sub-region;
and under the condition that the wall surface temperature of the sub-region is less than the minimum film boiling temperature corresponding to the sub-region, determining that the heat exchange mode of the sub-region is excessive boiling.
In a possible implementation manner, for each sub-region, determining a heat exchange mode of the sub-region further includes:
under the condition that the heat exchange mode of the sub-region is in film boiling, if the void fraction of the control body corresponding to the sub-region is smaller than a first judgment threshold value, determining that the heat exchange mode of the sub-region is in reverse annular film boiling;
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than a second judgment threshold value, determining that the heat exchange mode of the sub-region is dispersion flow film boiling;
and determining a first judgment threshold according to the water conservancy equivalent diameter of the channel to be detected and the average gas film thickness under the reverse circular flow condition, wherein the second judgment threshold is larger than the first judgment threshold.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is reverse annular flow film boiling, determining the heat exchange quantity of the sub-region by adopting a Bromley relational expression;
and under the condition that the heat exchange mode of the sub-region is in a dispersed flow film boiling state, determining the heat exchange quantity of the sub-region by adopting a Forslund-Rohsenow relational expression.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than the first judgment threshold and smaller than the second judgment threshold, determining a first intermediate quantity of the sub-region by adopting a Bromley relational expression, and determining a second intermediate quantity of the sub-region by adopting a Forslund-Rohsenow relational expression;
and determining the heat exchange amount of the sub-area according to the first intermediate amount and the second intermediate amount corresponding to the sub-area.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is excessive boiling, if the geometric parameter value of the channel to be detected is greater than or equal to a preset geometric threshold value, determining the heat exchange amount of the sub-region by adopting a Weisman model;
and under the condition that the heat exchange mode of the sub-area is excessive boiling, if the geometric parameter value of the channel to be detected is smaller than a preset geometric threshold, determining the heat exchange quantity of the sub-area according to the density of liquid in the sub-area and the latent heat of vaporization of the gas.
In one possible implementation, the method further includes:
under the condition that the channel to be detected is a circular tube, the geometric parameter of the channel to be detected is the inner diameter of the circular tube;
under the condition that the channel to be detected is a ring pipe, the geometric parameter of the channel to be detected is the difference value between the outer diameter and the inner diameter of the ring pipe;
and under the condition that the channel to be detected is of a rod bundle structure, the geometric parameter of the channel to be detected is the diameter of an inscribed circle of a channel formed by a plurality of fuel rods in the rod bundle structure.
In one possible implementation manner, determining, for each sub-region, a heat exchange mode of the sub-region includes:
and under the condition that the control body corresponding to the sub-region is steam, determining that the heat exchange mode of the sub-region is single-phase steam convection heat exchange.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is smaller than a third judgment threshold, determining the heat exchange quantity of the sub-region by adopting a laminar flow model;
and under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is greater than a fourth judgment threshold, determining the heat exchange amount of the sub-region by using a Dittus-Boelter relational expression, wherein the fourth judgment threshold is greater than the third judgment threshold.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is larger than a third judgment threshold and smaller than a fourth judgment threshold, determining a third intermediate quantity of the sub-region by adopting a laminar flow model, and determining a fourth intermediate quantity of the sub-region by adopting a Dittus-Boelter relational expression;
and determining the heat exchange amount of the sub-area according to the third intermediate amount and the fourth intermediate amount corresponding to the sub-area.
In one possible implementation, determining a foaming area near a quenching front of the inner wall of the channel to be measured according to the flow rate of the re-submerging inlet of the channel to be measured comprises:
determining the length of the foaming area as a first length value under the condition that the flow velocity of the re-submerged inlet of the channel to be detected is smaller than a first flow velocity threshold value;
determining the length of a foaming area as a second length value under the condition that the flow speed of the re-submerging inlet of the channel to be detected is greater than a second flow speed threshold value, wherein the second flow speed threshold value is greater than the first flow speed threshold value, and the second length value is greater than the first length value;
and under the condition that the flow rate of the re-submerging inlet of the channel to be detected is greater than the first flow rate threshold value and less than the second flow rate threshold value, determining the length of the foaming area by adopting an interpolation method according to the flow rate of the re-submerging inlet of the channel to be detected.
According to another aspect of the embodiments of the present disclosure, there is provided a post-critical heat exchange analysis device for re-flooding, the device comprising:
the first determining module is used for determining a foaming area near the quenching front edge of the inner wall of the channel to be detected according to the flow velocity of the re-submerging inlet of the channel to be detected;
the dividing module is used for determining a region of the channel to be detected, which is located at the downstream of the foaming region near the quenching front edge, as a region to be detected, and dividing the region to be detected into a plurality of sub-regions;
the second determining module is used for determining the heat exchange mode of each sub-region;
and the third determining module is used for determining the heat exchange quantity of each sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region.
According to another aspect of the disclosed embodiments, there is provided a heavy water reactor refueling device, the device comprising:
a processor;
a memory for storing processor-executable instructions;
wherein the processor is configured to perform the method described above.
According to another aspect of embodiments of the present disclosure, there is provided a non-transitory computer-readable storage medium having stored thereon computer program instructions which, when executed by a processor, implement the above-described method.
The invention has the beneficial effects that: according to the method, the foaming area near the quenching front edge is removed from the critical post-heat exchange area, so that the complex heat exchange mechanism of the foaming area is avoided, the interference on the heat exchange analysis of other areas at the downstream of the quenching front edge is avoided, and the heat exchange condition of the downstream area of the foaming area near the quenching front edge can be analyzed more reasonably. In addition, the embodiment of the disclosure subdivides the area downstream of the foaming area near the quenching front into a plurality of sub-areas, and determines the heat exchange amount of each sub-area according to the heat exchange mode of the sub-area, so that the critical post-heat exchange can be more finely simulated, and the cladding peak temperature and the quenching front advancing rate of the re-submerging process can be more accurately simulated. The analysis method for heat exchange after re-submergence criticality is applied to the development process of the analysis program of the Chinese autonomy loss of coolant accident, and lays a foundation for analysis of loss of coolant accident of a pressurized water reactor power station.
Drawings
FIG. 1 is a flow diagram illustrating a method of post-critical heat exchange analysis for re-flooding in accordance with an exemplary embodiment.
Fig. 2 is a schematic of the quench front and the foaming zone during the re-flood process.
FIG. 3 is a block diagram illustrating a post-critical-drowning heat exchange analysis device according to an exemplary embodiment.
FIG. 4 is a block diagram illustrating a post-critical-drowning heat exchange analysis device according to an exemplary embodiment.
Detailed Description
The invention is described in further detail below with reference to the figures and the embodiments.
FIG. 1 is a flow diagram illustrating a method of post-critical heat exchange analysis for re-flooding in accordance with an exemplary embodiment. The method can be executed by a terminal device, wherein the terminal device can be a computer, for example, the terminal device can be a server, a desktop computer, a notebook computer, a tablet computer, and the like, and the terminal device can also be a user device, a vehicle-mounted device, a wearable device, and the like, and the type of the terminal device is not limited in the embodiment of the disclosure. As shown in fig. 1, the method includes:
and 103, determining the heat exchange quantity of each sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region.
According to the method, the foaming area near the quenching front edge is removed from the critical post-heat exchange area, so that the complex heat exchange mechanism of the foaming area is avoided, the interference on the heat exchange analysis of other areas at the downstream of the quenching front edge is avoided, and the heat exchange condition of the downstream area of the foaming area near the quenching front edge can be analyzed more reasonably. In addition, the embodiment of the disclosure subdivides the area downstream of the foaming area near the quenching front into a plurality of sub-areas, and determines the heat exchange amount of each sub-area according to the heat exchange mode of the sub-area, so that the critical post-heat exchange can be more finely simulated, and the cladding peak temperature and the quenching front advancing rate of the re-submerging process can be more accurately simulated. The analysis method for heat exchange after re-submergence criticality is applied to the development process of the analysis program of the Chinese autonomy loss of coolant accident, and lays a foundation for analysis of loss of coolant accident of a pressurized water reactor power station.
Fig. 2 is a schematic of the quench front and the foaming zone during the re-flood process. As shown in fig. 2, different conditions during the re-flooding process may result in different lengths of the foamed region. Generally speaking, differences in the flow rate at which the channel under test re-floods the inlet can result in differences in the length of the bubble region of the channel under test.
In one possible implementation, step 100 may include:
step 300, determining the length of a foaming area as a first length value under the condition that the flow rate of the re-submerged inlet of the channel to be detected is smaller than a first flow rate threshold value;
step 301, determining the length of a foaming area as a second length value under the condition that the flow rate of the re-submerging inlet of the channel to be tested is greater than a second flow rate threshold value, wherein the second flow rate threshold value is greater than the first flow rate threshold value, and the second length value is greater than the first length value;
and 302, under the condition that the flow rate of the to-be-detected channel re-submerging inlet is larger than the first flow rate threshold and smaller than the second flow rate threshold, determining the length of the foaming area by adopting an interpolation method according to the flow rate of the to-be-detected channel re-submerging inlet.
For example, the first flow threshold may be 2.5cm/s, the first length may be 10.0cm, the second flow threshold may be 15.0cm/s, and the second length may be 30cm, such that when the re-flood inlet flow rate is 2.5cm/s or less, the foamed region has a length of 10.0 cm; when the flow velocity of the re-submerging inlet is more than or equal to 15.0cm/s, the length of the foaming area is 30.0 cm; the length of the foamed zone is linearly interpolated between 10.0cm and 30.0cm when the flow rate of the re-flood inlet is in the interval 2.5cm/s to 15.0 cm/s.
For example, when the flow rate of the re-submerging inlet is in the interval range of 2.5cm/s to 15.0cm/s, the length L of the foaming zone can be determined according to equation 1qf。
Wherein L isqfFor the length of the foamed zone, VinThe flow rate of the inlet is re-flooded for the channel to be measured.
Because the influence of the flow velocity of the to-be-detected channel re-submerging inlet on the length of the foaming area is large, the corresponding relation between the flow velocity of the to-be-detected channel re-submerging inlet and the length of the foaming area is obtained according to experience, and the range of the foaming area near the quenching front edge can be defined more accurately according to the corresponding relation.
It should be noted that, other different corresponding relationships (e.g., functional relationships, etc.) between the flow rate of the re-submerging inlet of the channel to be measured and the length of the foaming region can also be obtained according to practical experience, which is not limited in the embodiment of the disclosure.
In a possible implementation manner, the step 101 may include, in a case that the length of the region to be measured is determined, determining a region of the channel to be measured, which is located downstream of the foaming region near the quenching front edge, as the region to be measured, and dividing the region to be measured into a plurality of sub-regions, where the plurality of sub-regions are formed by dividing the region to be measured equally according to the length of the region to be measured, where it should be noted that the lengths of the sub-regions may be completely the same, or may be partially the same or different from each other, and the dividing manner of the sub-regions is not limited in this embodiment of the disclosure.
In one possible implementation, step 102 may include:
step 400, determining the minimum film boiling temperature corresponding to each sub-region according to the thermodynamic parameters of the inner wall of the sub-region, the thermodynamic parameters of the liquid in the control body corresponding to the sub-region and the thermodynamic parameters of the gas in the control body corresponding to the sub-region;
step 401, determining that the heat exchange mode of the sub-region is film boiling under the condition that the wall surface temperature of the sub-region is greater than or equal to the minimum film boiling temperature corresponding to the sub-region;
step 402, determining that the heat exchange mode of the sub-region is excessive boiling under the condition that the wall temperature of the sub-region is less than the minimum film boiling temperature corresponding to the sub-region.
In embodiments of the present disclosure, a thermodynamic parameter may be represented as a fundamental quantity describing a state of a substance, and the thermodynamic parameter may be, for example, temperature, pressure, density, specific heat capacity at constant pressure, thermal conductivity, enthalpy, entropy, or the like. The thermodynamic parameters of the inner wall and the control body corresponding to the sub region are not limited in the embodiment of the disclosure.
For example, in step 400, for each sub-region, the first temperature of the sub-region may be determined according to formula 2, formula 3, and formula 4.
ΔPcrit3203.6-P equation 4
Wherein, Tmin1Is the first temperature, T, of the sub-regionlFor the temperature of the liquid in the control body corresponding to the sub-zone, KlFor the thermal conductivity, p, of the liquid in the control body corresponding to that sub-regionlFor the density of the liquid in the control body corresponding to the sub-region, CplIs the constant pressure specific heat capacity, K, of the liquid in the control body corresponding to the sub-regionwIs the thermal conductivity of the wall corresponding to the sub-region, pwIs the density of the wall corresponding to the sub-region, CpwIs the constant pressure specific heat capacity, T, of the wall surface corresponding to the sub-regionhnIs a first intermediate variable with the sub-area, P is the pressure value of the sub-area, Δ PcritIs the difference between the sub-region pressure value and a reference pressure value (3203.6).
Next, for each sub-region, the second temperature of the sub-region may be determined according to equation 5, equation 6.
Wherein, Tmin2Is the second temperature of the sub-region, TBIs a second intermediate variable with the sub-region, HfgFor the latent heat of vaporization of the control body corresponding to the sub-region, TsatThe saturation temperature of the corresponding control body of the sub-area, g is the gravity acceleration, rhogFor controlling the density of the gas in the gas, K, corresponding to the sub-regiongIs the thermal conductivity of the gas in the control body corresponding to the sub-region, and σ is the surface tension of the control body corresponding to the sub-region, μgThe repeated parameters in the formulas 5 and 6 and the formulas 2 to 4 have the same meaning for the viscosity of the gas in the corresponding control body of the subarea.
Finally, the maximum value of the first temperature and the second temperature corresponding to the sub-region can be used as the minimum film boiling temperature T of the sub-regionminI.e. Tmin＝max(Tmin1，Tmin2)。
In step 401, the magnitude relationship between the wall temperature of the sub-region and the minimum film boiling temperature of the sub-region may be determined, and when the wall temperature of the sub-region is greater than or equal to the minimum film boiling temperature of the sub-region, it may be determined that the heat exchange mode of the sub-region is film boiling.
In step 402, the magnitude relationship between the wall temperature of the sub-region and the minimum film boiling temperature of the sub-region may be determined, and when the wall temperature of the sub-region is less than the minimum film boiling temperature of the sub-region, it may be determined that the heat exchange mode of the sub-region is excessive boiling.
According to the heat exchange analysis method and the heat exchange analysis device, the heat exchange modes of the sub-regions are classified more finely according to the wall surface of each sub-region and the thermodynamic parameters of the control body, so that the heat exchange analysis model can more accurately fit the actual heat exchange condition of the heat exchange of the channel to be detected after the channel to be detected is critical, and more accurate simulation analysis results can be obtained.
In one possible implementation, step 102 may further include:
step 500, under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is smaller than a first judgment threshold, determining that the heat exchange mode of the sub-region is reverse annular film boiling.
The first judgment threshold value can be determined according to the water conservancy equivalent diameter of the channel to be detected and the average gas film thickness under the reverse circular flow condition. For example, the first judgment threshold value a may be determined according to equation 7.
Wherein a is a first judgment threshold value, dhTo control the bulk hydraulic equivalent diameter, dgfIs the average vapor film thickness under reverse loop flow conditions.
It should be noted that the first determination threshold may be determined when the heat exchange mode of the sub-regions is film boiling, or the first determination threshold of each sub-region may be determined in advance before the heat exchange mode of each sub-region is determined. The determination timing of the first determination threshold is not limited in the embodiments of the present disclosure.
Step 501, in a case that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is greater than a second determination threshold (where the second determination threshold is greater than the first determination threshold, and the second determination threshold may be a constant, for example, 0.8), it is determined that the heat exchange mode of the sub-region is diffusion film boiling.
Therefore, according to the void fraction of the control body of each sub-area, the hydraulic equivalent diameter of the control body and the average vapor film thickness under the reverse circulation condition, the heat exchange mode of the sub-area of which the heat exchange mode belongs to film boiling is further subdivided, so that the heat exchange model can simulate the actual heat exchange condition of the heat exchange after the critical state of the channel to be measured more vividly.
As an example of this embodiment, in step 103, in the case of classifying the heat exchange mode of each sub-region, the heat exchange amount of the sub-region may be determined according to the heat exchange model corresponding to the heat exchange mode of each sub-region.
For example, step 103 may include:
step 1030, determining the heat exchange amount of the sub-region by adopting a Bromley relational expression under the condition that the heat exchange mode of the sub-region is reverse annular flow film boiling;
and step 1031, under the condition that the heat exchange mode of the sub-region is diffusion flow film boiling, determining the heat exchange quantity of the sub-region by adopting a Forslund-Rohsenow relational expression.
Step 1032, under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is greater than the first judgment threshold and smaller than the second judgment threshold, determining a first intermediate quantity of the sub-region by adopting a Bromley relational expression, and determining a second intermediate quantity of the sub-region by adopting a forsland-Rohsenow relational expression; and determining the heat exchange amount of the sub-area according to the first intermediate amount and the second intermediate amount corresponding to the sub-area. For example, the first intermediate quantity and the second intermediate quantity of the sub-region may be processed by an interpolation method to obtain the heat exchange quantity of the sub-region, or an average value or a weighted average value of the first intermediate quantity and the second intermediate quantity of the sub-region may be used as the heat exchange quantity of the sub-region.
For example, step 103 may further include:
1033, under the condition that the heat exchange mode of the sub-region is excessive boiling, if the geometric parameter value of the channel to be detected is greater than or equal to a preset geometric threshold value, determining the heat exchange amount of the sub-region by adopting a Weisman model;
step 1034, in the case that the heat exchange mode of the sub-region is excessive boiling, if the geometric parameter value of the channel to be measured is smaller than the preset geometric threshold, determining the heat exchange amount of the sub-region according to the density of the liquid in the sub-region and the latent heat of vaporization of the gas.
In the disclosed embodiment, transition boiling is a heat exchange mode between film boiling and nucleate boiling, in which liquid droplets in the channel intermittently contact the wall surface of the channel, and thus the channel geometry greatly affects the heat exchange.
In view of this, the embodiment of the present disclosure determines the geometric parameter of the channel to be measured, and determines the heat exchange amount of the sub-region according to the geometric parameter characteristic of the channel to be measured when the heat exchange mode of the sub-region is excessive boiling, and considers the influence of the geometric characteristic of the channel on the heat exchange after critical, thereby obtaining the heat exchange amount of the sub-region more accurately.
For example, in the case that the channel to be measured is a circular tube, the geometric parameter of the channel to be measured is the inner diameter of the circular tube; under the condition that the channel to be detected is a ring pipe, the geometric parameter of the channel to be detected is the difference value between the outer diameter and the inner diameter of the ring pipe; and under the condition that the channel to be detected is of a rod bundle structure, the geometric parameter of the channel to be detected is the diameter of an inscribed circle of a channel formed by a plurality of fuel rods in the rod bundle structure.
In step 1033, the Weisman model is used to determine the heat exchange amount of the sub-region when the channel geometry of the sub-region satisfies any one of the following conditions:
1) if the channel is a circular tube, the inner diameter is greater than or equal to 3mm (an example of a preset geometric threshold, it should be noted that an applicable numerical value can be selected as the preset geometric threshold as required);
2) if the channel is a ring pipe, the difference between the outer diameter and the inner diameter is more than or equal to 3 mm;
3) if the channel is of a rod bundle structure, drawing an inscribed circle in the channel formed by the four fuel rods in the grid (for the quadrilateral grid; for a triangular grid, an inscribed circle is drawn within the channel formed by the three fuel rods. ) The diameter of the inscribed circle is more than or equal to 3 mm.
In step 1034, the "liquid meniscus extension zone transient evaporation model" is used to calculate the transition boiling heat transfer when the channel geometry of the sub-zone satisfies any of the following conditions:
1) if the channel is a round pipe, the inner diameter is less than 3 mm;
2) if the channel is a ring pipe, the difference between the outer diameter and the inner diameter is less than 3 mm;
3) if the channel is of a rod bundle structure, drawing an inscribed circle in the channel formed by the four fuel rods in the grid (for the quadrilateral grid; for a triangular grid, an inscribed circle is drawn within the channel formed by the three fuel rods. ) Drawing an inscribed circle, wherein the diameter of the inscribed circle is less than 3 mm.
The "liquid meniscus extension zone transient evaporation model" can be expressed by equation 8.
Wherein q islIs the amount of heat exchange in this sub-zone, plFor the density of the liquid in the control body corresponding to the sub-region, hfgFor the latent heat of vaporization of the control body corresponding to the sub-region, delta0Average thickness of liquid film, t, of extended area of liquid meniscus of quench precursor in channel to be measuredgrowThe growth time of the bubble in the channel to be measured, tevaporationAnd CONfra is the contact portion of the liquid in the channel to be measured and the wall surface.
In one possible implementation, step 102 may include: and under the condition that the control body corresponding to the sub-region is steam, determining that the heat exchange mode of the sub-region is single-phase steam convection heat exchange.
During the re-submerging process, steam at high temperature is likely to be in a low reynolds number flowing state because the steam temperature may be high and the reynolds number of the steam is inversely proportional to the square of the steam temperature. Under the condition that the heat exchange model of the sub-region is single-phase steam convection heat exchange, the heat exchange quantity of the sub-region needs to be determined by adopting different heat exchange models aiming at the sub-regions with different Reynolds numbers.
Step 103 may include: under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the reynolds number of the steam corresponding to the sub-region is smaller than a third judgment threshold (for example, the third judgment threshold may be 2300), determining the heat exchange amount of the sub-region by using a laminar flow model;
the laminar flow model can be expressed by equations 9 and 10:
wherein, TvSteam temperature function, V, of radial position variable r, angular position variable theta, axial position variable zvAs the flow rate of steam, CpvIs the specific heat capacity at constant pressure of steam, rhovIs the density of steam, kvFor steam thermal conductivity, Φ is the viscous dissipation term, TcladA cladding temperature function of a radial position variable r, an angular position variable theta, and an axial position variable z.
In step 103, the inner wall of the channel corresponding to the sub-region may include a plurality of positions, each position may be represented by a corresponding radial position, an angular position, and an axial position, the angular position of each position may be represented by an included angle between the position and a preset position on a radial cross section in the channel to be measured, for each position, the steam temperature and the cladding temperature corresponding to the position may be determined through formula 9 and formula 10, and the heat exchange amount at the position may be determined according to the steam temperature and the cladding temperature corresponding to the position.
Step 103 may further include: under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the reynolds number of the steam corresponding to the sub-region is greater than a fourth judgment threshold (for example, the fourth judgment threshold may be 10000), determining the heat exchange amount of the sub-region by using a Dittus-Boelter relational expression, where the fourth judgment threshold is greater than the third judgment threshold.
Step 103 may further include: under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is larger than a third judgment threshold and smaller than a fourth judgment threshold, determining a third intermediate quantity of the sub-region by adopting a laminar flow model, and determining a fourth intermediate quantity of the sub-region by adopting a Dittus-Boelter relational expression;
and determining the heat exchange amount of the sub-area according to the third intermediate amount and the fourth intermediate amount corresponding to the sub-area. For example, interpolation may be used to process the third intermediate quantity and the fourth intermediate quantity to obtain the heat exchange quantity of the sub-region.
The influence of the geometric characteristics of the channel on the heat exchange after the critical is considered in the embodiment of the disclosure; the influence of the steam thermal physical property characteristic (the steam Reynolds number is in inverse proportion to the steam temperature quadratic power) and the channel geometric characteristics on the convection heat exchange of the wall steam under the high-temperature condition is considered. Thereby more finely simulating critical post heat exchange.
FIG. 3 is a block diagram illustrating a post-critical-drowning heat exchange analysis device according to an exemplary embodiment. As shown in fig. 3, the apparatus includes:
the first determining module 31 is used for determining a foaming area near the quenching front edge of the inner wall of the channel to be measured according to the flow rate of the re-submerging inlet of the channel to be measured;
the dividing module 32 is configured to determine a region, located near the quenching front edge, of the channel to be measured downstream of the foaming region as a region to be measured, where the region to be measured is divided into a plurality of sub-regions;
a second determining module 33, configured to determine, for each sub-region, a heat exchange mode of the sub-region;
and a third determining module 34, configured to determine, for each sub-region, a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region.
In one possible implementation manner, the second determining module includes:
for each sub-region, determining the minimum film boiling temperature corresponding to the sub-region according to the thermodynamic parameters of the inner wall of the sub-region, the thermodynamic parameters of the liquid in the control body corresponding to the sub-region and the thermodynamic parameters of the gas in the control body corresponding to the sub-region;
determining that the heat exchange mode of the sub-region is film boiling under the condition that the wall surface temperature of the sub-region is greater than or equal to the minimum film boiling temperature corresponding to the sub-region;
and under the condition that the wall surface temperature of the sub-region is less than the minimum film boiling temperature corresponding to the sub-region, determining that the heat exchange mode of the sub-region is excessive boiling.
In a possible implementation manner, the second determining module further includes:
under the condition that the heat exchange mode of the sub-region is in film boiling, if the void fraction of the control body corresponding to the sub-region is smaller than a first judgment threshold value, determining that the heat exchange mode of the sub-region is in reverse annular film boiling;
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than a second judgment threshold value, determining that the heat exchange mode of the sub-region is dispersion flow film boiling;
and determining a first judgment threshold according to the water conservancy equivalent diameter of the channel to be detected and the average gas film thickness under the reverse circular flow condition, wherein the second judgment threshold is larger than the first judgment threshold.
In a possible implementation manner, for each sub-region, determining a heat exchange amount of the sub-region according to a heat exchange model corresponding to a heat exchange mode of the sub-region includes:
under the condition that the heat exchange mode of the sub-region is reverse annular flow film boiling, determining the heat exchange quantity of the sub-region by adopting a Bromley relational expression;
and under the condition that the heat exchange mode of the sub-region is in a dispersed flow film boiling state, determining the heat exchange quantity of the sub-region by adopting a Forslund-Rohsenow relational expression.
In one possible implementation, the third determining module includes:
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than the first judgment threshold and smaller than the second judgment threshold, determining a first intermediate quantity of the sub-region by adopting a Bromley relational expression, and determining a second intermediate quantity of the sub-region by adopting a Forslund-Rohsenow relational expression;
and determining the heat exchange amount of the sub-area according to the first intermediate amount and the second intermediate amount corresponding to the sub-area.
In one possible implementation, the third determining module includes:
under the condition that the heat exchange mode of the sub-region is excessive boiling, if the geometric parameter value of the channel to be detected is greater than or equal to a preset geometric threshold value, determining the heat exchange amount of the sub-region by adopting a Weisman model;
and under the condition that the heat exchange mode of the sub-area is excessive boiling, if the geometric parameter value of the channel to be detected is smaller than a preset geometric threshold, determining the heat exchange quantity of the sub-area according to the density of liquid in the sub-area and the latent heat of vaporization of the gas.
In one possible implementation, the method further includes:
under the condition that the channel to be detected is a circular tube, the geometric parameter of the channel to be detected is the inner diameter of the circular tube;
under the condition that the channel to be detected is a ring pipe, the geometric parameter of the channel to be detected is the difference value between the outer diameter and the inner diameter of the ring pipe;
and under the condition that the channel to be detected is of a rod bundle structure, the geometric parameter of the channel to be detected is the diameter of an inscribed circle of a channel formed by a plurality of fuel rods in the rod bundle structure.
In one possible implementation manner, the second determining module includes:
and under the condition that the control body corresponding to the sub-region is steam, determining that the heat exchange mode of the sub-region is single-phase steam convection heat exchange.
In one possible implementation, the third determining module includes:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is smaller than a third judgment threshold, determining the heat exchange quantity of the sub-region by adopting a laminar flow model;
and under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is greater than a fourth judgment threshold, determining the heat exchange amount of the sub-region by using a Dittus-Boelter relational expression, wherein the fourth judgment threshold is greater than the third judgment threshold.
In one possible implementation, the third determining module includes:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is larger than a third judgment threshold and smaller than a fourth judgment threshold, determining a third intermediate quantity of the sub-region by adopting a laminar flow model, and determining a fourth intermediate quantity of the sub-region by adopting a Dittus-Boelter relational expression;
and determining the heat exchange amount of the sub-area according to the third intermediate amount and the fourth intermediate amount corresponding to the sub-area.
In one possible implementation, determining a foaming area near a quenching front of the inner wall of the channel to be measured according to the flow rate of the re-submerging inlet of the channel to be measured comprises:
determining the length of the foaming area as a first length value under the condition that the flow velocity of the re-submerged inlet of the channel to be detected is smaller than a first flow velocity threshold value;
determining the length of a foaming area as a second length value under the condition that the flow speed of the re-submerging inlet of the channel to be detected is greater than a second flow speed threshold value, wherein the second flow speed threshold value is greater than the first flow speed threshold value, and the second length value is greater than the first length value;
and under the condition that the flow rate of the re-submerging inlet of the channel to be detected is greater than the first flow rate threshold value and less than the second flow rate threshold value, determining the length of the foaming area by adopting an interpolation method according to the flow rate of the re-submerging inlet of the channel to be detected.
FIG. 4 is a block diagram illustrating a post-critical-drowning heat exchange analysis device according to an exemplary embodiment. For example, the apparatus 1900 may be provided as a server. Referring to fig. 4, the device 1900 includes a processing component 1922 further including one or more processors and memory resources, represented by memory 1932, for storing instructions, e.g., applications, executable by the processing component 1922. The application programs stored in memory 1932 may include one or more modules that each correspond to a set of instructions. Further, the processing component 1922 is configured to execute instructions to perform the above-described method.
The device 1900 may also include a power component 1926 configured to perform power management of the device 1900, a wired or wireless network interface 1950 configured to connect the device 1900 to a network, and an input/output (I/O) interface 1958. The device 1900 may operate based on an operating system stored in memory 1932, such as Windows Server, Mac OS XTM, UnixTM, LinuxTM, FreeBSDTM, or the like.
In an exemplary embodiment, a non-transitory computer readable storage medium, such as the memory 1932, is also provided that includes computer program instructions executable by the processing component 1922 of the apparatus 1900 to perform the above-described methods.
The present disclosure may be systems, methods, and/or computer program products. The computer program product may include a computer-readable storage medium having computer-readable program instructions embodied thereon for causing a processor to implement various aspects of the present disclosure.
The computer readable storage medium may be a tangible device that can hold and store the instructions for use by the instruction execution device. The computer readable storage medium may be, for example, but not limited to, an electronic memory device, a magnetic memory device, an optical memory device, an electromagnetic memory device, a semiconductor memory device, or any suitable combination of the foregoing. More specific examples (a non-exhaustive list) of the computer readable storage medium would include the following: a portable computer diskette, a hard disk, a Random Access Memory (RAM), a read-only memory (ROM), an erasable programmable read-only memory (EPROM or flash memory), a Static Random Access Memory (SRAM), a portable compact disc read-only memory (CD-ROM), a Digital Versatile Disc (DVD), a memory stick, a floppy disk, a mechanical coding device, such as punch cards or in-groove projection structures having instructions stored thereon, and any suitable combination of the foregoing. Computer-readable storage media as used herein is not to be construed as transitory signals per se, such as radio waves or other freely propagating electromagnetic waves, electromagnetic waves propagating through a waveguide or other transmission medium (e.g., optical pulses through a fiber optic cable), or electrical signals transmitted through electrical wires.
The computer-readable program instructions described herein may be downloaded from a computer-readable storage medium to a respective computing/processing device, or to an external computer or external storage device via a network, such as the internet, a local area network, a wide area network, and/or a wireless network. The network may include copper transmission cables, fiber optic transmission, wireless transmission, routers, firewalls, switches, gateway computers and/or edge servers. The network adapter card or network interface in each computing/processing device receives computer-readable program instructions from the network and forwards the computer-readable program instructions for storage in a computer-readable storage medium in the respective computing/processing device.
The computer program instructions for carrying out operations of the present disclosure may be assembler instructions, Instruction Set Architecture (ISA) instructions, machine-related instructions, microcode, firmware instructions, state setting data, or source or object code written in any combination of one or more programming languages, including an object oriented programming language such as Smalltalk, C + + or the like and conventional procedural programming languages, such as the "C" programming language or similar programming languages. The computer-readable program instructions may execute entirely on the user's computer, partly on the user's computer, as a stand-alone software package, partly on the user's computer and partly on a remote computer or entirely on the remote computer or server. In the case of a remote computer, the remote computer may be connected to the user's computer through any type of network, including a Local Area Network (LAN) or a Wide Area Network (WAN), or the connection may be made to an external computer (for example, through the Internet using an Internet service provider). In some embodiments, the electronic circuitry that can execute the computer-readable program instructions implements aspects of the present disclosure by utilizing the state information of the computer-readable program instructions to personalize the electronic circuitry, such as a programmable logic circuit, a Field Programmable Gate Array (FPGA), or a Programmable Logic Array (PLA).
Various aspects of the present disclosure are described herein with reference to flowchart illustrations and/or block diagrams of methods, apparatus (systems) and computer program products according to embodiments of the disclosure. It will be understood that each block of the flowchart illustrations and/or block diagrams, and combinations of blocks in the flowchart illustrations and/or block diagrams, can be implemented by computer-readable program instructions.
These computer-readable program instructions may be provided to a processor of a general purpose computer, special purpose computer, or other programmable data processing apparatus to produce a machine, such that the instructions, which execute via the processor of the computer or other programmable data processing apparatus, create means for implementing the functions/acts specified in the flowchart and/or block diagram block or blocks. These computer-readable program instructions may also be stored in a computer-readable storage medium that can direct a computer, programmable data processing apparatus, and/or other devices to function in a particular manner, such that the computer-readable medium storing the instructions comprises an article of manufacture including instructions which implement the function/act specified in the flowchart and/or block diagram block or blocks.
The computer readable program instructions may also be loaded onto a computer, other programmable data processing apparatus, or other devices to cause a series of operational steps to be performed on the computer, other programmable apparatus or other devices to produce a computer implemented process such that the instructions which execute on the computer, other programmable apparatus or other devices implement the functions/acts specified in the flowchart and/or block diagram block or blocks.
The flowchart and block diagrams in the figures illustrate the architecture, functionality, and operation of possible implementations of systems, methods and computer program products according to various embodiments of the present disclosure. In this regard, each block in the flowchart or block diagrams may represent a module, segment, or portion of instructions, which comprises one or more executable instructions for implementing the specified logical function(s). In some alternative implementations, the functions noted in the block may occur out of the order noted in the figures. For example, two blocks shown in succession may, in fact, be executed substantially concurrently, or the blocks may sometimes be executed in the reverse order, depending upon the functionality involved. It will also be noted that each block of the block diagrams and/or flowchart illustration, and combinations of blocks in the block diagrams and/or flowchart illustration, can be implemented by special purpose hardware-based systems which perform the specified functions or acts, or combinations of special purpose hardware and computer instructions.
Having described embodiments of the present disclosure, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. The terms used herein were chosen in order to best explain the principles of the embodiments, the practical application, or technical improvements to the techniques in the marketplace, or to enable others of ordinary skill in the art to understand the embodiments disclosed herein.
Claims (13)
1. A method for analyzing heat exchange after re-flooding criticality, the method comprising:
determining a foaming area near the quenching front edge of the inner wall of the channel to be detected according to the flow velocity of the re-submerging inlet of the channel to be detected;
determining a region of the channel to be detected, which is located at the downstream of the foaming region near the quenching front edge, as a region to be detected, wherein the region to be detected is divided into a plurality of sub-regions;
determining a heat exchange mode of each sub-region;
for each sub-region, determining the heat exchange quantity of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region;
for each sub-region, determining a heat exchange mode of the sub-region, including:
for each sub-region, determining the minimum film boiling temperature corresponding to the sub-region according to the thermodynamic parameters of the inner wall of the sub-region, the thermodynamic parameters of the liquid in the control body corresponding to the sub-region and the thermodynamic parameters of the gas in the control body corresponding to the sub-region;
determining that the heat exchange mode of the sub-region is film boiling under the condition that the wall surface temperature of the sub-region is greater than or equal to the minimum film boiling temperature corresponding to the sub-region;
and under the condition that the wall surface temperature of the sub-region is less than the minimum film boiling temperature corresponding to the sub-region, determining that the heat exchange mode of the sub-region is excessive boiling.
2. The method of claim 1, wherein for each sub-region, determining a heat exchange pattern for that sub-region further comprises:
under the condition that the heat exchange mode of the sub-region is in film boiling, if the void fraction of the control body corresponding to the sub-region is smaller than a first judgment threshold value, determining that the heat exchange mode of the sub-region is in reverse annular film boiling;
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than a second judgment threshold value, determining that the heat exchange mode of the sub-region is dispersion flow film boiling;
and determining a first judgment threshold according to the water conservancy equivalent diameter of the channel to be detected and the average gas film thickness under the reverse circular flow condition, wherein the second judgment threshold is larger than the first judgment threshold.
3. The method according to claim 2, wherein for each sub-region, determining the heat exchange amount of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region comprises:
under the condition that the heat exchange mode of the sub-region is reverse annular flow film boiling, determining the heat exchange quantity of the sub-region by adopting a Bromley relational expression;
and under the condition that the heat exchange mode of the sub-region is in a dispersed flow film boiling state, determining the heat exchange quantity of the sub-region by adopting a Forslund-Rohsenow relational expression.
4. The method according to claim 2, wherein for each sub-region, determining the heat exchange amount of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region comprises:
under the condition that the heat exchange mode of the sub-region is film boiling, if the void fraction of the control body corresponding to the sub-region is larger than the first judgment threshold and smaller than the second judgment threshold, determining a first intermediate quantity of the sub-region by adopting a Bromley relational expression, and determining a second intermediate quantity of the sub-region by adopting a Forslund-Rohsenow relational expression;
and determining the heat exchange amount of the sub-area according to the first intermediate amount and the second intermediate amount corresponding to the sub-area.
5. The method according to claim 1, wherein for each sub-region, determining the heat exchange amount of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region comprises:
under the condition that the heat exchange mode of the sub-region is excessive boiling, if the geometric parameter value of the channel to be detected is greater than or equal to a preset geometric threshold value, determining the heat exchange amount of the sub-region by adopting a Weisman model;
and under the condition that the heat exchange mode of the sub-area is excessive boiling, if the geometric parameter value of the channel to be detected is smaller than a preset geometric threshold, determining the heat exchange quantity of the sub-area according to the density of liquid in the sub-area and the latent heat of vaporization of the gas.
6. The method of claim 5, further comprising:
under the condition that the channel to be detected is a circular tube, the geometric parameter of the channel to be detected is the inner diameter of the circular tube;
under the condition that the channel to be detected is a ring pipe, the geometric parameter of the channel to be detected is the difference value between the outer diameter and the inner diameter of the ring pipe;
and under the condition that the channel to be detected is of a rod bundle structure, the geometric parameter of the channel to be detected is the diameter of an inscribed circle of a channel formed by a plurality of fuel rods in the rod bundle structure.
7. The method of claim 1, wherein determining, for each sub-region, a heat exchange pattern for that sub-region comprises:
and under the condition that the control body corresponding to the sub-region is steam, determining that the heat exchange mode of the sub-region is single-phase steam convection heat exchange.
8. The method according to claim 7, wherein for each sub-region, determining the heat exchange amount of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region comprises:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is smaller than a third judgment threshold, determining the heat exchange quantity of the sub-region by adopting a laminar flow model;
and under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is greater than a fourth judgment threshold, determining the heat exchange amount of the sub-region by using a Dittus-Boelter relational expression, wherein the fourth judgment threshold is greater than the third judgment threshold.
9. The method according to claim 7, wherein for each sub-region, determining the heat exchange amount of the sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region comprises:
under the condition that the heat exchange mode of the sub-region is single-phase steam convection heat exchange, if the Reynolds number of the steam corresponding to the sub-region is larger than a third judgment threshold and smaller than a fourth judgment threshold, determining a third intermediate quantity of the sub-region by adopting a laminar flow model, and determining a fourth intermediate quantity of the sub-region by adopting a Dittus-Boelter relational expression;
and determining the heat exchange amount of the sub-area according to the third intermediate amount and the fourth intermediate amount corresponding to the sub-area.
10. The method of claim 1, wherein determining the foaming zone near the quench front of the inner wall of the channel under test based on the flow rate of the channel under test at the re-flood inlet comprises:
determining the length of the foaming area as a first length value under the condition that the flow velocity of the re-submerged inlet of the channel to be detected is smaller than a first flow velocity threshold value;
determining the length of a foaming area as a second length value under the condition that the flow speed of the re-submerging inlet of the channel to be detected is greater than a second flow speed threshold value, wherein the second flow speed threshold value is greater than the first flow speed threshold value, and the second length value is greater than the first length value;
and under the condition that the flow rate of the re-submerging inlet of the channel to be detected is greater than the first flow rate threshold value and less than the second flow rate threshold value, determining the length of the foaming area by adopting an interpolation method according to the flow rate of the re-submerging inlet of the channel to be detected.
11. A post-critical heat exchange analysis apparatus for re-flooding, the apparatus comprising:
the first determining module is used for determining a foaming area near the quenching front edge of the inner wall of the channel to be detected according to the flow velocity of the re-submerging inlet of the channel to be detected;
the dividing module is used for determining a region of the channel to be detected, which is located at the downstream of the foaming region near the quenching front edge, as a region to be detected, and dividing the region to be detected into a plurality of sub-regions;
the second determining module is used for determining the heat exchange mode of each sub-region;
the third determining module is used for determining the heat exchange quantity of each sub-region according to the heat exchange model corresponding to the heat exchange mode of the sub-region;
the second determining module includes:
the first determining submodule is used for determining the minimum film boiling temperature corresponding to each sub-region according to the thermodynamic parameters of the inner wall of the sub-region, the thermodynamic parameters of liquid in the control body corresponding to the sub-region and the thermodynamic parameters of gas in the control body corresponding to the sub-region;
the second determining submodule is used for determining that the heat exchange mode of the sub-region is film boiling under the condition that the wall surface temperature of the sub-region is greater than or equal to the minimum film boiling temperature corresponding to the sub-region;
and the third determining submodule is used for determining that the heat exchange mode of the sub-region is excessive boiling under the condition that the wall surface temperature of the sub-region is less than the minimum film boiling temperature corresponding to the sub-region.
12. A post-critical heat exchange analysis apparatus for re-flooding, the apparatus comprising:
a processor;
a memory for storing processor-executable instructions;
wherein the processor is configured to perform the method of any one of claims 1 to 10.
13. A non-transitory computer readable storage medium having stored thereon computer program instructions, wherein the computer program instructions, when executed by a processor, implement the method of any one of claims 1 to 10.
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| CN110631271A (en) * | 2019-10-25 | 2019-12-31 | 甘肃省建材科研设计院有限责任公司 | Medium-deep underground rock heat type heat supply system and heat supply method |
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