Molten salt heat energy storage system based on mixed biomass combustion and high-temperature heat pump

Abstract

The invention discloses a fused salt heat energy storage system based on mixed biomass combustion and a high-temperature heat pump, particularly relates to the field of heat energy storage, and is used for solving the problem that latent heat recovery and utilization of an existing heat storage system are insufficient. The data acquisition module is used for acquiring flue gas temperature, flow velocity and condensable component concentration in real time and calculating dew point temperature; a condensation point determination module identifies a condensation starting point and termination point interval; the heat exchange section division module accurately divides the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induction condensation section and a low-temperature flushing section, and maps the sections to the fused salt heat storage loops with the corresponding heights; the condensate separation module controls the reverse flow direction of the flue gas in the medium-temperature induction condensation section, and condensate drops are introduced into a liquid guide groove to be discharged; the residue discharging module is used for condensing and discharging residual liquid drops and particles in the low-temperature washing section; the heat storage adjusting module calculates balance state parameters in the storage and executes heat distribution and transfer adjustment between the storage layers, and dynamic balance and efficient utilization of the high-temperature heat storage area and the medium-temperature heat storage area are achieved.

Description

Technical Field

[0001] This invention relates to the field of thermal energy storage technology, and more specifically, to a molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump. Background Technology

[0002] In combined heating scenarios involving high-temperature heat pumps driven by hybrid biomass combustion and molten salt thermal energy storage, the diversity of fuel composition and the complexity of the combustion process mean that, in addition to carrying a large amount of high-temperature sensible heat, the flue gas also contains a significant proportion of condensable components, such as water vapor, acetic acid vapor, light organic esters, and fine tar droplets. These components are in a gaseous state at high temperatures, containing not only high latent heat of phase change but also exhibiting concentration fluctuations with changes in fuel ratio, moisture content, and combustion load. When the flue gas temperature drops to near the dew point, condensable components rapidly precipitate and form liquid films or viscous deposits on the heat exchange surfaces, leading to a decrease in heat transfer coefficient, an increase in flow resistance, and an exacerbation of localized corrosion risk. To avoid heat exchanger performance degradation, existing systems typically raise the minimum heat exchange temperature to prevent most condensable components from condensing in the main heat exchange zone, thus sacrificing the opportunity for latent heat recovery. This treatment method is particularly evident under low-load conditions or in high-humidity winter environments. The available driving temperature difference for the heat pump is forced to shrink, and the COP drops significantly, resulting in a simultaneous decrease in the heat charge rate of molten salt thermal energy storage and the overall system efficiency. At the same time, due to the rapid fluctuations in flue gas flow rate and component concentration, conventional heat exchange control strategies are difficult to keep up with in a timely manner, leading to the dual problems of low latent heat utilization efficiency and increased deposition on the heat exchange surface.

[0003] Therefore, it is necessary to introduce precise control of the condensation window and heat zoning management based on the characteristics of condensable components at the system level, so that sensible heat and latent heat can be recovered in an orderly manner in different temperature zones, and efficient regulation can be achieved in molten salt stratified heat storage, thereby realizing stable and sustainable thermal energy storage and utilization. Summary of the Invention

[0004] In order to overcome the above-mentioned defects of the prior art, embodiments of the present invention provide a molten salt thermal energy storage system based on hybrid biomass combustion and high-temperature heat pump to solve the problems mentioned in the background art.

[0005] To achieve the above objectives, the present invention provides the following technical solution:

[0006] A molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump includes:

[0007] The data acquisition module is used to collect flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculate the dew point temperature, and construct a curve showing the change in condensable component concentration.

[0008] The condensation point determination module is used to determine the range between the condensation start point and the condensation end point based on the concentration change curve and the dew point temperature.

[0009] The heat exchange section division module is used to divide the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section, which are respectively mapped to the heat exchange loops of different heat storage zones.

[0010] The condensate removal module is used to control the reverse direction of flue gas flow in the medium-temperature induced condensation section and to guide the removed condensate droplets into the liquid guide tank for discharge.

[0011] The residual discharge module is used to condense residual condensable components in the low-temperature flushing section and transport the condensate and particulates to the discharge channel;

[0012] The thermal storage regulation module is used to establish a heat accumulation zone inside the reservoir and to perform heat distribution and transfer regulation between reservoirs by calculating equilibrium state parameters.

[0013] In a preferred embodiment, the data acquisition module collects flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculates the dew point temperature, and constructs a condensable component concentration change curve, specifically including:

[0014] Temperature acquisition units, flow rate acquisition units, condensable component detection units, and humidity detection units are set at several sampling points at the cross-sectional location of the flue gas outlet of the mixed biomass combustion.

[0015] Each unit collects temperature, flow rate, condensable component concentration, and humidity data at its corresponding location.

[0016] Humidity data and condensable component concentration data are converted into corresponding partial pressure values, and dew point temperatures at each time point are generated based on gas saturation conditions.

[0017] The concentration data of condensable components are interpolated and filtered to remove noise in chronological order to obtain a time-continuous concentration sequence.

[0018] Concentration change curves were established based on the concentration sequence of condensable components and imported into the condensation point determination module.

[0019] In a preferred embodiment, the condensation point determination module, specifically determining the interval between the condensation start point and the end point based on the concentration change curve and the dew point temperature, includes:

[0020] The magnitude of change in the concentration change curve of condensable components at each sampling point is calculated for adjacent time points and compared with a preset concentration change threshold.

[0021] When there are consecutive sampling points within a set range where the change in concentration is greater than or equal to the concentration change threshold and the corresponding temperature is equal to or lower than the dew point temperature, the first sampling point that meets the conditions is determined as the condensation start point.

[0022] When there are consecutive sampling points within the set sampling points after the condensation start point where the change amplitude is less than the concentration change threshold and the temperature is lower than the dew point temperature, the first sampling point that meets the conditions is determined as the condensation termination point.

[0023] Based on the flue gas velocity and heat exchanger size, the time corresponding to the above condensation start point and condensation end point is converted into a physical location interval.

[0024] In a preferred embodiment, the heat exchange section division module divides the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section, and the heat exchange loops mapped to different height heat storage sections specifically include:

[0025] Based on the collected temperature, flow rate and condensable component concentration data, the flue gas heat exchanger is divided into a high-temperature sensible heat section, a medium-temperature induced condensation section and a low-temperature flushing section along the flue gas flow direction.

[0026] The heat exchange circuit of the molten salt high-temperature layer is labeled as the first heat exchange circuit, and the heat exchange circuit of the molten salt medium-temperature layer is labeled as the second heat exchange circuit. The molten salt high-temperature layer and the molten salt medium-temperature layer correspond to the preset heat storage sections at different heights of the molten salt thermal storage device.

[0027] The high-temperature sensible heat section is mapped to the first heat exchange loop, while the medium-temperature induced condensation section and the low-temperature flushing section are mapped to the second heat exchange loop.

[0028] In a preferred embodiment, dividing the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section along the flue gas flow direction specifically includes:

[0029] For each sampling location, the rate of temperature change, the rate of flow rate change, and the rate of change of condensable component concentration are calculated, and the three types of change rates are combined into a feature data sequence according to the sampling point location.

[0030] The three types of change rates at each data collection location are numerically weighted to generate a comprehensive change index for that location.

[0031] The comprehensive change index along the flue gas flow direction is arranged in sequence, and the position where the first occurrence changes from below the average value to above the average value is taken as the dividing point between the high-temperature sensible heat section and the medium-temperature induced condensation section.

[0032] Find the next location where the flue gas flow changes from below the average value to above the average value, and use it as the dividing point between the medium-temperature induced condensation section and the low-temperature flushing section;

[0033] The boundary point is used as the partition index for the current operation, and the comprehensive change index is recalculated and the boundary point position is relocated in each operation.

[0034] In a preferred embodiment, the condensate removal module, specifically including controlling the flue gas flow direction to reverse within the medium-temperature induced condensation section and guiding the removed condensate droplets into the liquid guide tank for discharge, includes:

[0035] Switch the direction of flue gas entering the medium-temperature induced condensation section and control the flue gas flow direction to be opposite to the outlet direction of the high-temperature sensible heat section;

[0036] The length of the condensation zone is calculated based on the physical location interval between the condensation start point and the end point. The adjustment step size of the flow rate is set according to the length of the condensation zone. The flue gas velocity in the medium-temperature induced condensation section is continuously increased within a preset range according to the adjustment step size to separate the condensate droplets from the gas flow.

[0037] The separated condensate droplets are introduced into the liquid guiding tank along the wall and drained according to a preset cycle.

[0038] In a preferred embodiment, the residual discharge module specifically includes the following steps for conveying residual condensate and particulate matter to the discharge channel:

[0039] During the low-temperature flushing stage, the flue gas output from the medium-temperature induced condensation stage is received and distributed into several uniform flow paths.

[0040] The residual condensate and particulate matter are transported to the discharge channel to discharge the liquid and particulate matter.

[0041] In a preferred embodiment, the thermal storage regulation module establishes a heat accumulation zone within the reservoir and performs heat distribution and transfer regulation between reservoirs by calculating equilibrium state parameters, specifically including:

[0042] The heat from the high-temperature sensible heat section is transferred to the molten salt high-temperature layer through the first heat exchange loop, and a high-temperature heat accumulation zone is established inside the reservoir.

[0043] The heat from the medium-temperature induced condensation section and the low-temperature flushing section is transferred to the molten salt medium-temperature layer through the second heat exchange loop, and a medium-temperature heat accumulation zone is established inside the reservoir.

[0044] During operation, the heat storage distribution in the high-temperature heat accumulation zone and the medium-temperature heat accumulation zone is obtained respectively, and the offset ratio with the preset equilibrium heat storage distribution is calculated. The offset ratio is marked as the equilibrium state parameter.

[0045] Based on the equilibrium state parameters, heat distribution and transfer regulation is performed between reservoirs, and the equilibrium state parameters are fed back to the heat exchange section division module.

[0046] The technical effects and advantages of the molten salt thermal energy storage system based on hybrid biomass combustion and high-temperature heat pump of the present invention are as follows:

[0047] This solution achieves precise identification of flue gas condensation characteristics by directly collecting flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion system. Combined with dew point temperature calculation and concentration change curve construction, it enables rapid determination of the condensation start and end points under dynamic operating conditions, improving the accuracy of condensation process positioning. The flue gas heat exchanger is scientifically divided into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section through a heat exchange section division module. These sections are mapped one-to-one with the heat exchange loops of different heat storage zones, making the heat recovery process more hierarchical and rational, allowing for the separate storage and efficient utilization of high-temperature and medium-temperature heat. In the medium-temperature induced condensation section, controlling the flue gas flow direction reverses causes condensate droplets to detach from the airflow and be discharged in a concentrated manner, reducing the risk of scaling and blockage on subsequent heat exchange surfaces. The low-temperature flushing section further condenses and discharges residual condensable components and particles, achieving deep removal of condensate and solid pollutants from the exhaust gas and improving emission cleanliness. The thermal storage regulation module establishes a heat accumulation zone inside the reservoir and performs cross-reservoir heat distribution based on equilibrium state parameters, which effectively improves the heat utilization rate and stability of the energy storage system, realizes the efficient recovery and on-demand distribution of combustion waste heat, and takes into account both operating efficiency and system life. Attached Figure Description

[0048] Figure 1 This is a schematic diagram of the structure of a molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to the present invention. Detailed Implementation

[0049] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0050] Example 1

[0051] Figure 1 The present invention discloses a molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump, comprising:

[0052] The data acquisition module is used to collect flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculate the dew point temperature, and construct a curve showing the change in condensable component concentration.

[0053] The condensation point determination module is used to determine the range between the condensation start point and the condensation end point based on the concentration change curve and the dew point temperature.

[0054] The heat exchange section division module is used to divide the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section, which are respectively mapped to the heat exchange loops of different heat storage zones.

[0055] The condensate removal module is used to control the reverse direction of flue gas flow in the medium-temperature induced condensation section and to guide the removed condensate droplets into the liquid guide tank for discharge.

[0056] The residual discharge module is used to condense residual condensable components in the low-temperature flushing section and transport the condensate and particulates to the discharge channel;

[0057] The thermal storage regulation module is used to establish a heat accumulation zone inside the reservoir and to perform heat distribution and transfer regulation between reservoirs by calculating equilibrium state parameters.

[0058] The data acquisition module collects flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculates the dew point temperature, and constructs a curve showing the change in condensable component concentration.

[0059] Several cross-sectional locations are selected as sampling points in the outlet flue of the hybrid biomass combustion device. The number of sampling points should be determined based on the flue cross-sectional dimensions, flue gas velocity distribution uniformity, and thermal calculation requirements, with a default of no less than eight to ensure that the collected data reflects the overall distribution characteristics. Each sampling point is equipped with a fixed temperature acquisition unit, flow rate acquisition unit, condensable component detection unit, and humidity detection unit, each unit independently completing the acquisition of its corresponding physical quantity. The temperature acquisition unit uses a platinum resistance temperature sensor. The flow rate acquisition unit uses a Pitot tube differential pressure method or a thermal flow meter, with a built-in airflow guiding structure to ensure that the velocity vector at the measurement point is close to the axial velocity component, avoiding measurement deviations caused by vortices or secondary flows. The condensable component detection unit is used to determine the total concentration of easily condensable substances (such as water vapor, acid vapor, organic vapor, etc.) in the flue gas in real time, using online gas chromatography analysis or infrared absorption spectroscopy-based detection methods to ensure response speed and accuracy. The humidity detection unit is used to measure the relative humidity of the flue gas, using a capacitive humidity probe. By combining the data from the temperature acquisition unit, the moisture content in the flue gas can be determined. All probes in the acquisition units are fixed at the sampling points and connected to the acquisition lines via corrosion-resistant sealing connectors to prevent flue gas leakage and mixing with external air. This arrangement ensures that complete information on temperature, flow rate, condensable component concentration, and humidity distribution can be obtained at any given time, providing a solid data foundation for subsequent thermal analysis and condensation point determination.

[0060] After acquiring humidity and condensable component concentration data at each sampling point, these two types of data were converted into thermodynamically meaningful partial pressures. Humidity data essentially reflects the ratio of water vapor partial pressure to saturated water vapor pressure (i.e., relative humidity). Given the temperature at the measuring point, the corresponding saturated water vapor pressure can be obtained by consulting a water vapor saturation pressure table. Multiplying the measured relative humidity by this saturation pressure yields the water vapor partial pressure at the measuring point. Condensable component concentration data requires conversion based on the total pressure of the flue gas. Assuming the total flue gas pressure is close to atmospheric pressure, the volume fraction of the condensable component is directly multiplied by the total pressure to obtain the corresponding condensable component partial pressure. If the condensable component contains multiple substances, their concentrations can be measured separately in the analyzer, and the total condensable partial pressure can be calculated according to the principle of partial pressure superposition. The conversion of humidity data to partial pressure is based on Dalton's law of partial pressures and the water vapor saturation pressure formula, while the conversion of condensable component concentration to partial pressure is based on the conversion relationship between mole fraction and total pressure.

[0061] After obtaining the partial pressures of water vapor and condensable components, adding them together yields the total partial pressure of condensable substances. In thermodynamics, the dew point temperature is defined as the temperature at which water vapor (and other condensable substances) begins to condense when a gas is cooled to this temperature under constant pressure. The temperature value corresponding to the total condensable partial pressure is derived from the gas saturation pressure curve; this temperature is the dew point temperature at that sampling point. In practice, this dew point temperature is an engineering approximation based on the saturation curve of the main condensable component (water vapor). The condensable component concentration data is interpolated and filtered in chronological order to obtain a time-continuous concentration sequence. A concentration change curve is then established based on this sequence and imported into the condensation point determination module.

[0062] In the condensation point determination module, the interval between the condensation start point and the end point is determined based on the concentration change curve and the dew point temperature.

[0063] In the obtained concentration sequence, every two adjacent time sampling points are grouped together. The concentration difference between the later and earlier time points is calculated, and the absolute value of the difference is taken as the amplitude of change. To avoid interference from short-term large fluctuations caused by random noise, a time window smoothing process is performed before the data enters the amplitude calculation. After the amplitude calculation is completed, the results are compared point by point with a preset concentration change threshold. The concentration change threshold is a fixed value determined during the system debugging phase based on historical operating conditions and condensation characteristic curves. For example, it can be selected as the threshold by repeatedly measuring the concentration change rate under typical condensation conditions and selecting the amplitude range that can effectively distinguish between the condensation and non-condensation stages. During the comparison, if the amplitude of change at a certain adjacent time point is greater than or equal to the threshold, the concentration change at that location is considered significant.

[0064] After calculating the concentration change amplitude, the starting position of the condensation process is further identified. The condensation starting point is defined as the location where, in the time-sequential sampling points, a significant concentration change amplitude first occurs and the temperature meets the condensation conditions. In practice, firstly, in the concentration amplitude comparison results of each sampling point, a continuous set of sampling points (no less than 1 / 4 of the total number of sampling points) is retrieved, requiring that the change amplitude values ​​of these sampling points are all greater than or equal to a predetermined concentration change threshold. Occasional single-point fluctuations are excluded, limiting the identification target to stages with continuous changes. Simultaneously, cross-judgment is performed using temperature data. Temperature data is obtained from the temperature acquisition unit at the same sampling location and has been converted into a time-synchronized temperature sequence in the previous steps. To determine whether the temperature meets the condensation conditions, this embodiment uses a standard where the temperature is equal to or lower than the dew point temperature of the gas at that component concentration. During the retrieval process, when a continuous sampling segment is detected that meets both the concentration change amplitude condition and the temperature condition, the first sampling point of that continuous segment can be determined as the condensation starting point. The advantage of this definition is that it not only reflects the concentration change characteristics of condensable components at the start of condensation, but also incorporates actual temperature conditions, ensuring that the identified starting point is synchronized with the actual physical condensation process. This method allows for accurate capture of the condensation initiation point under real-world operating conditions where flue gas temperature and composition change frequently.

[0065] After determining the condensation initiation point, the search continues along the time series to determine the termination point of the condensation process. The condensation termination point is defined as the location, after the condensation initiation point, where the concentration change first significantly decreases and the temperature falls below the dew point. In practice, the search interval is limited to consecutive sampling points after the condensation initiation point (no less than 1 / 4 of the total number of sampling points). The concentration change amplitude at each point within this interval is calculated and compared with a concentration change threshold. When a continuous segment of sampling points is found to have a concentration change amplitude less than the threshold and a temperature remaining below the dew point, the first sampling point of that continuous segment can be determined as the condensation termination point. A decrease in the concentration change amplitude means that most of the condensable components have undergone phase change and settled, and the condensation process is nearing its end. A temperature consistently below the dew point indicates that the environmental conditions in this interval are still favorable for maintaining the liquid phase, but a significant phase change rate has no longer occurred. After determining the condensation initiation and termination points, this embodiment combines the flue gas velocity and the heat exchanger geometry to convert the time interval between them into a corresponding physical location interval. The specific method is as follows: the average flue gas velocity measured under the same operating conditions (provided by the velocity acquisition unit) is multiplied by the time interval between the starting point and the ending point to obtain the physical length along the flue gas flow direction.

[0066] In the heat exchange section division module, the flue gas heat exchanger is divided into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section, which are respectively mapped to heat exchange loops in different heat storage zones.

[0067] For each sampling location within the flue gas channel, calculate the rate of change of temperature, flow rate, and concentration of condensable components. These sampling locations are monitoring points spaced evenly along the flue gas flow direction or arranged according to the equipment structure. Each monitoring point is equipped with a temperature sensing unit, a flow rate detection unit, and a condensable component concentration detection unit. The data acquisition frequency for each monitoring point must be consistent to ensure that the three types of data are collected under the same time reference, thereby eliminating errors caused by time asynchrony. The rate of change is calculated by subtracting the measurement value of the previous sampling period from the measurement value at the current time point, and then dividing by the time interval between the two samplings to obtain the degree of change of the physical quantity per unit time at that location. For example, if the temperature changes from 180℃ to 190℃ within a 10-second interval, the rate of change of temperature is 1℃ / s; the same applies to flow rate and concentration. To avoid the influence of instantaneous noise, it is recommended to perform a moving average on the raw data before calculation, for example, by using the average value of 3 to 5 consecutive sampling points instead of the value at a single moment. After completing the calculation of the three types of rates of change, they need to be combined into a comprehensive rate of change index. The comprehensive change index is generated by first assigning numerical weights to three types of change rates. The weight allocation principle is based on the correlation assessment of heat exchange efficiency changes in historical operating data. In this embodiment, the weights are specifically adjusted based on the feedback of the equilibrium state parameters of the thermal storage regulation module. The sum of the three weights is fixed at 1.0 and does not change with the operating cycle. During calculation, each change rate is multiplied by its weight, and the three results are added together to obtain the comprehensive change index for that sampling location.

[0068] After obtaining the comprehensive change index at all sampling locations along the flue gas flow direction, these indices are arranged in order of physical location, with each value in the sequence corresponding to a specific monitoring point on the flue gas path. Next, the overall average value of the comprehensive change index is calculated as a reference benchmark for identifying the boundary point. This average value is obtained by summing the comprehensive change indices of all sampling locations within the current operating cycle and dividing by the total number of sampling locations, reflecting the average change level of the entire channel within this cycle. The principle for determining the boundary point is: the location where the comprehensive change index first changes from below the average to above the average is marked as the physical boundary between the high-temperature sensible heat section and the medium-temperature induced condensation section. In implementation, to avoid misjudgment due to short-term fluctuations at a single monitoring point, the determination requires at least two consecutive locations to meet this trend, i.e., the comprehensive change index of the previous location is below the average, while the comprehensive change index of the subsequent location is above the average. This ensures the continuity of the trend rather than instantaneous fluctuations. The physical significance of this dividing point is that in the high-temperature sensible heat section region before this point, the flue gas mainly exchanges heat with the heat exchanger wall through sensible heat transfer, and the rate of temperature change is relatively slow; while in the medium-temperature induced condensation section that begins from this dividing point, the changes in flue gas temperature, flow rate and concentration of condensable components show obvious acceleration characteristics, indicating that this region has entered a heat exchange stage dominated by condensation phase transformation.

[0069] After identifying the boundary between the high-temperature sensible heat section and the medium-temperature induced condensation section, the comprehensive change index sequence is analyzed downstream along the flue gas flow direction to find the boundary between the medium-temperature induced condensation section and the low-temperature flushing section. The method is similar to that for the medium-temperature induced condensation section, finding the next point where the comprehensive change index changes from below the average to above the average. This boundary point represents the end of the medium-temperature induced condensation section and the beginning of the low-temperature flushing section. Its physical significance is that before this point, condensation phase change and sensible heat transfer are still occurring, while after this point, the flue gas temperature and composition changes tend to stabilize, and the main heat exchange form shifts to low-temperature heat recovery and the condensation removal of residual condensable components. In actual operation, this boundary point has a direct impact on regulating the flow rate distribution, flushing fluid supply, and final emission quality of the low-temperature flushing section. After determining the two boundary points in each operating cycle, their location numbers are stored as the current operating zone index. This zone index contains information such as the start and end positions of the high-temperature sensible heat section, the start and end positions of the medium-temperature induced condensation section, and the starting position of the low-temperature flushing section. Since flue gas conditions and operating loads may vary significantly in different cycles, this embodiment requires that the comprehensive change index be recalculated and the boundary point be repositioned for each operation to ensure that the partition index always matches the actual operating conditions.

[0070] The heat exchange loops at different temperature levels in the molten salt thermal storage device are labeled and distinguished. A molten salt thermal storage device is a heat storage structure capable of storing a large amount of heat over a wide temperature range. It exhibits a clear temperature stratification along its height, typically with higher temperatures at the top and lower temperatures at the bottom. The loop located in the upper part of the storage device, used for storing and releasing high-temperature heat energy, is defined as the "molten salt high-temperature layer heat exchange loop" and clearly labeled as the first heat exchange loop. The loop located in the middle part of the storage device, with a medium temperature range and primarily used for absorbing and releasing medium-temperature heat energy, is defined as the "molten salt medium-temperature layer heat exchange loop" and clearly labeled as the second heat exchange loop. In practice, during the equipment installation phase, the corresponding heat exchange pipelines are arranged according to the internal structure of the thermal storage tank. The pipe openings of the high-temperature layer heat exchange circuit are arranged in the high-temperature area at the top of the thermal storage tank, where the temperature is generally higher than 400℃ (the specific value is flexibly set according to the operating temperature), for direct heat exchange with the high-temperature heat source. The pipe openings of the medium-temperature layer heat exchange circuit are arranged in the middle area of ​​the thermal storage tank, where the temperature is usually between 200℃ and 350℃ (the specific value is flexibly set according to the operating temperature), for heat exchange with the medium-temperature heat source or waste heat recovery section.

[0071] After completing the labeling of the high-temperature and medium-temperature heat exchange loops, the corresponding heat storage sections within the molten salt thermal storage device and their mapping relationship with the flue gas heat exchange section are further clarified. In the design of the molten salt thermal storage device, the heat distribution along the height is relatively stable. The upper part is the high-temperature heat storage zone, corresponding to the heat exchange tube group of the first heat exchange loop, and the lower part is the medium-temperature heat storage zone, corresponding to the heat exchange tube group of the second heat exchange loop. Subsequently, it is necessary to establish a mapping relationship between the different temperature sections already partitioned in the flue gas heat exchanger and the molten salt heat storage sections. Specifically, the high-temperature sensible heat section, as the area with the highest flue gas temperature, directly inputs its recovered heat into the high-temperature heat storage section through the first heat exchange loop to achieve high-grade thermal energy storage; the recovered heat from the medium-temperature induced condensation section and the low-temperature flushing section is input into the medium-temperature heat storage section through the second heat exchange loop for the accumulation of medium-temperature thermal energy. This mapping relationship is achieved through pipeline layout and heat exchanger connections. Heat at different temperature ranges is stored separately in the most suitable temperature layers, avoiding the mixing of high-temperature and medium-temperature heat energy, which would prevent subsequent heat extraction from effectively matching different heating needs. For example, the high-temperature layer can be used to drive high-temperature heat pumps or industrial heating processes, while the medium-temperature layer can be used for heating or low-temperature industrial heating. Through this highly corresponding and segmented mapping strategy, hierarchical management and precise allocation can be achieved in the energy storage system, thereby significantly improving heat utilization efficiency and the overall performance of the energy storage system.

[0072] In the condensate removal module, the flue gas flow direction is reversed in the medium-temperature induced condensation section, and the removed condensate droplets are introduced into the liquid guide tank for discharge.

[0073] After sensible heat recovery in the high-temperature sensible heat section, the flue gas is guided into the medium-temperature induced condensation section to achieve a significant condensation effect. To improve condensation efficiency and control the distribution of condensation points, the flue gas flow direction is switched so that its flow direction upon entering the medium-temperature induced condensation section is opposite to the outlet direction of the high-temperature sensible heat section. This flow direction switching is typically achieved mechanically through a switching mechanism with guide vanes or an S-shaped pipe structure. The guide vanes or bends change the direction of flue gas propulsion during the switching action, enabling the fluid to flow in reverse within the medium-temperature section. The reason for using reverse flow is based on the coupling mechanism of heat exchange and condensation: reverse flow allows the flue gas to encounter a relatively low-temperature heat exchange surface at the inlet of the medium-temperature section, thereby accelerating the temperature drop and reaching the condensable components' condensation conditions as quickly as possible, shortening the condensation delay distance, and improving the overall heat exchange utilization rate of the medium-temperature section. Furthermore, from a fluid dynamics perspective, reverse flow creates a local recirculation zone within the flow field of the intermediate temperature section. This recirculation zone prolongs the residence time of the flue gas, allowing aerosol droplets more time to grow to a separable particle size, thereby increasing the probability of droplet separation. In actual implementation, the switching of flue gas flow direction is automatically triggered in conjunction with operating conditions. When the outlet temperature of the high-temperature sensible heat section drops to a specific switching condition value and the flow rate stabilizes, the flow direction is switched, and the reverse flow state is maintained after the switch is completed until the condensation process in the intermediate temperature section ends.

[0074] After the flue gas enters the intermediate-temperature induced condensation section, the physical location range between the condensation start point and the termination point is a crucial basis for determining the spatial distribution of the condensation process. In this embodiment, the condensation start point and termination point have been obtained through the condensation point determination module, and the distance between them is the physical length of the condensation zone. Determining this length is one of the core parameters for flow rate control, because the formation and detachment of condensed droplets require a certain airflow shear force and time distribution. In specific implementation, the positions of the condensation start point and termination point within the intermediate-temperature section are first quantified using length units, such as measuring the axial distance of the heat exchange pipe or the number of heat exchange units, and then the total length of the interval is calculated. Subsequently, the step size for flue gas flow rate adjustment is set according to the length of the condensation zone. Here, the step size refers to the rate increase amplitude during each flow rate adjustment process. For example, when the condensation zone is long, the flow rate step size can be relatively small to ensure that the droplets have a longer formation time within the condensation zone; while when the condensation zone is short, the flow rate step size is set larger to quickly generate sufficient shear force within the limited condensation space to cause the droplets to detach. The step size can be set by referring to empirical data or optimized through multiple trial runs during the commissioning phase. For example, when the condensation zone length is 1.5 meters, the step size can be set to an increment of 0.05 meters per second; while when the condensation zone length is 0.8 meters, the step size can be increased to an increment of 0.1 meters per second. This step size control, correlated with the condensation zone length, ensures that the droplet generation and separation process remains optimal under different condensation zone distribution conditions, thereby significantly improving the condensation efficiency and heat exchange capacity of the intermediate temperature section. The flow rate is adjusted by configuring axial flow fans with adjustable blade angles and matching flow regulating valves at both the inlet and outlet ends of the intermediate temperature induced condensation section. The axial flow fan on the inlet side provides forward thrust or reverse pull, and its blade angle can be continuously adjusted between 0° and 35°. By changing the blade angle, the gas flow rate through the condensation section is adjusted, thereby achieving precise flow rate control. The flow regulating valve on the outlet side adopts a high-temperature and corrosion-resistant butterfly valve structure. Its opening degree can be changed step by step within the range of 20% to 100%. The flow rate can be adjusted by controlling the outlet back pressure in conjunction with the inlet fan.

[0075] After setting the flow rate step size, the actual flow rate control and droplet separation process begins. In this embodiment, the flue gas velocity in the intermediate-temperature induced condensation section is gradually increased according to the set step size value. The increase range is limited to a preset upper and lower limit range, which is determined by the equipment design parameters and operational safety requirements. For example, the flow rate can be controlled between 1.5 m / s and 3.0 m / s. During the gradual increase of the flow rate, the droplets formed in the condensation zone gradually detach from the attached state to the free-floating state under the shearing action of the airflow. When the droplets reach a certain size, they will deviate from the main airflow path and approach the heat exchange wall due to gravity and inertia, eventually contacting the wall to form a liquid film flowing downwards along the wall. In this embodiment, a liquid guiding channel is provided below the wall of the intermediate-temperature section. The inlet shape of the liquid guiding channel matches the flow direction of the liquid film on the wall, which can efficiently collect the condensate sliding down the wall. After entering the liquid guiding tank, the condensate is guided to the collection and discharge path. During this process, to prevent the liquid from accumulating in the liquid guiding tank for a long time, which may affect the heat exchange efficiency or cause corrosion, the liquid is drained according to a preset cycle. For example, it can be set to automatically open the drain valve every 15 minutes of operation or when the liquid level reaches 80% of the capacity of the liquid guiding tank, so as to discharge the condensate to an external collection container.

[0076] In the residual discharge module, condensate and particulate matter are transported to the discharge channel.

[0077] During the start-up of the cryogenic flushing stage, the flue gas output from the intermediate-temperature induced condensation stage is received through the guide interface at the inlet of the cryogenic flushing section. After preliminary condensation and separation in the intermediate-temperature section, this flue gas still contains a certain proportion of condensable components and tiny droplets. To ensure efficient capture and condensation of the remaining condensable components during the cryogenic flushing process, the airflow is rationally diverted at the inlet. The inlet of the cryogenic flushing section is equipped with a multi-channel diversion structure, which consists of a circular cross-section inlet main pipe and multiple radially distributed diversion branches. The cross-sectional dimensions, distribution angles, and inlet flow resistance of the diversion branches are precisely calculated and experimentally determined to ensure uniform distribution of flue gas flow rate and velocity in each diversion path. When the airflow enters the diversion structure, guide vanes are installed on the inner wall of the inlet main pipe. The inclination angle of the guide vanes is set to 15°–25° according to the airflow rotation characteristics, which can effectively weaken the residual rotating vortices in the outlet airflow of the intermediate-temperature section and avoid uneven condensation caused by excessive flow in one branch. The length and bending radius of the diversion branches are kept consistent to prevent uneven flow distribution caused by differences in path resistance. Each stream of flue gas, after being distributed, leads to an independent cryogenic heat exchange unit. These units are arranged in parallel and together form the main body of the cryogenic flushing section. The internal channel cross-section of each cryogenic heat exchange unit is a flat rectangular shape, which facilitates increasing the contact area with the cooling surface, thereby improving heat transfer efficiency.

[0078] After the airflow is evenly distributed, the flue gas flows along the cooling surfaces of each cryogenic heat exchange unit. Under the action of the cooling medium (such as cryogenic circulating water or cryogenic heat transfer oil), the gas temperature rapidly drops to a level far below the dew point temperature of the condensable components. At this point, the remaining condensable components in the flue gas, such as water vapor, acid vapor, and organic vapor, undergo phase change, forming droplets that deposit on the heat exchange surfaces. Because the inner walls of the cryogenic flushing section heat exchange units are treated with a hydrophobic and oleophobic coating, the condensed droplets quickly converge into a liquid film and flow downwards along the wall under gravity. Simultaneously, tiny particles entrained in the flue gas, due to the reduced flow velocity and the trapping effect of the liquid film, adhere to the liquid film or directly impact the cooling surfaces and are trapped. These particles include combustion residues, dust, and some crystalline substances, with particle sizes generally ranging from 0.1 micrometers to tens of micrometers. Because the cooling conditions in the cryogenic flushing section are stable and the liquid film formation is highly continuous, the efficiency of particle trapping can reach a high level. A liquid-solid separation chamber is located at the bottom of the heat exchange unit, containing a gravity settling tank and a multi-stage filter. After the liquid film flows into the settling tank, larger solid particles settle at the bottom, while smaller particles are trapped by the multi-stage filter. The separated clear liquid flows through a corrosion-resistant drainage pipe into a centralized liquid guiding pipeline, ultimately entering the discharge channel. The discharge channel is a closed-loop structure to prevent secondary pollution or corrosion of the external structure caused by contact between the condensate and the outside environment during transport. Solid particles are periodically discharged from the bottom of the settling tank through a slag discharge port equipped with a controllable, sealed valve, allowing for solid discharge without interrupting the operation of the low-temperature flushing section. For condensate requiring recovery, a liquid collection tank can be added to the discharge channel, allowing for on-demand recovery or discharge via a level control valve; for solid particles, their composition can be selected for recycling or disposal as waste.

[0079] In the thermal storage regulation module, a heat accumulation zone is established inside the reservoir, and heat distribution and transfer regulation is performed between reservoirs by calculating equilibrium state parameters.

[0080] During operation, the flue gas from the high-temperature sensible heat section outlet flows through the pre-established first heat exchange loop, directly transferring heat to the liquid molten salt in the high-temperature layer of the molten salt thermal storage device. The high-temperature layer is located in the upper space of the reservoir, and its structure has been pre-designed with sufficient volume and insulation measures during reservoir construction to ensure long-term stable heat retention at high temperatures. The first heat exchange loop rapidly transfers the sensible heat energy from the high-temperature flue gas to the molten salt, raising the temperature of this layer to the designed high-temperature range, forming a high-temperature heat accumulation zone. Within this zone, heat exhibits a vertical temperature gradient distribution, with higher temperatures at the top and lower at the bottom. Controlled circulation guided by natural convection and local baffles maintains temperature uniformity in the accumulation zone, preventing localized hotspots or excessively thick temperature stratification. Simultaneously, the flue gas from the outlets of the medium-temperature induced condensation section and the low-temperature flushing section enters the pre-established second heat exchange loop, transferring the remaining heat from the medium- and low-temperature sections to the medium-temperature layer of the reservoir. Located in the lower middle part of the reservoir, the medium-temperature layer efficiently absorbs the heat energy from the medium- and low-temperature flue gas. During heat exchange in the second heat exchange loop, the heat released by the flue gas causes the temperature of the molten salt in the intermediate temperature layer to rise, forming an independent intermediate temperature heat accumulation zone.

[0081] The thermal storage status of the high-temperature and medium-temperature heat accumulation zones is continuously monitored. Specifically, multiple sets of high-temperature resistant temperature sensors and molten salt level sensors are deployed at different heights within the high-temperature and medium-temperature layers. The temperature sensors measure the real-time temperature of the molten salt at each location, while the level sensors measure the volume change of the molten salt in different accumulation zones. By combining the measured temperature data with known specific heat capacity and density data of the molten salt, the total heat value of each accumulation zone can be calculated without directly interfering with the molten salt flow. "Heat storage distribution" refers to the proportion of total heat storage occupied by the high-temperature and medium-temperature accumulation zones at the current moment. For example, during the design phase, a preset balanced heat storage ratio can be set based on the system's energy demand characteristics, such as the high-temperature layer accounting for 60% of the total heat storage and the medium-temperature layer accounting for 40%. In actual operation, the system calculates the ratio of the measured heat storage in the high-temperature layer to that in the medium-temperature layer and compares it with the preset ratio to obtain the difference, i.e., the offset ratio. The magnitude and sign of the offset ratio directly reflect the degree of deviation between the current thermal storage state and the design equilibrium state. This offset ratio is defined as an equilibrium state parameter, which serves as the core basis for regulating heat distribution and transfer between reservoirs during actual operation. To ensure the stability of the calculation results, temperature and liquid level data are filtered within a certain time window during operation to remove calculation deviations caused by instantaneous fluctuations.

[0082] When the equilibrium parameters show a significant deviation between the thermal storage ratio of the high-temperature layer and the medium-temperature layer and the preset equilibrium value, heat distribution and transfer regulation between the reservoirs is implemented to prevent insufficient or excessive thermal storage in a certain area from affecting the stability of subsequent energy supply. Specific regulation methods include two types: first, partial molten salt fluid exchange between the high-temperature layer and the medium-temperature layer is achieved through hot salt diversion channels within the reservoir; second, the heat input rate entering different reservoirs is dynamically adjusted by changing the flow ratio of the first and second heat exchange loops. In the first type of regulation, a controllable hot salt connecting pipe is installed inside the reservoir. The inlet of the connecting pipe is located below the high-temperature layer, and the outlet is located above the medium-temperature layer, with the flow rate controlled by a high-temperature corrosion-resistant valve. When the thermal storage of the high-temperature layer is significantly higher than that of the medium-temperature layer, an appropriate amount of high-temperature molten salt flows into the medium-temperature layer through the connecting pipe, raising the temperature of the medium-temperature layer and supplementing its insufficient heat; conversely, when the heat of the medium-temperature layer is too high, some medium-temperature molten salt can be introduced into the high-temperature layer for temperature equalization. To avoid temperature shocks and excessively thick mixed layers, the flow rate is adjusted by gradual changes in opening to ensure a smooth and controllable heat transfer process. In the second type of adjustment, the equilibrium parameters are fed back to the heat exchange section division module in real time. By adjusting the speed of the circulating pumps or the opening of the flow control valves in the first and second heat exchange loops, the ratio of heat power input from the flue gas to the high-temperature and medium-temperature layers is changed. For example, when the heat in the high-temperature layer is insufficient, the flow rate of the first heat exchange loop is appropriately increased or its flue gas residence time is extended, thereby increasing the heat input to the high-temperature layer; when the heat in the medium-temperature layer is insufficient, similar adjustment measures are taken for the second heat exchange loop.

[0083] The above formulas are all dimensionless calculations. The formulas are derived from software simulations based on a large amount of collected data to obtain the most recent real-world results. The preset parameters and thresholds in the formulas are set by those skilled in the art according to the actual situation.

[0084] The above embodiments can be implemented, in whole or in part, by software, hardware, firmware, or any other combination thereof. When implemented using software, the above embodiments can be implemented, in whole or in part, as a computer program product. The computer program product includes one or more computer instructions or computer programs. When the computer instructions or computer programs are loaded or executed on a computer, all or part of the processes or functions described in the embodiments of this application are generated. The computer can be a general-purpose computer, a special-purpose computer, a computer network, or other programmable device. The computer instructions can be stored in a computer-readable storage medium or transmitted from one computer-readable storage medium to another. For example, the computer instructions can be transmitted from one website, computer, server, or data center to another website, computer, server, or data center via wired (e.g., infrared, wireless, microwave, etc.) means. The computer-readable storage medium can be any available medium that a computer can access or a data storage device such as a server or data center that includes one or more sets of available media. The available medium can be a magnetic medium (e.g., floppy disk, hard disk, magnetic tape), an optical medium (e.g., DVD), or a semiconductor medium. A semiconductor medium can be a solid-state drive.

[0085] Those skilled in the art will recognize that the modules and algorithm steps of the various examples described in conjunction with the embodiments disclosed herein can be implemented in electronic hardware, or a combination of computer software and electronic hardware. Whether these functions are implemented in hardware or software depends on the specific application and design constraints of the technical solution. Those skilled in the art can use different methods to implement the described functions for each specific application, but such implementation should not be considered beyond the scope of this application.

[0086] Those skilled in the art will understand that, for the sake of convenience and brevity, the specific working processes of the systems, devices, and modules described above can be referred to the corresponding processes in the foregoing method embodiments, and will not be repeated here.

[0087] In the several embodiments provided in this application, it should be understood that the disclosed systems, apparatuses, and methods can be implemented in other ways. For example, the apparatus embodiments described above are merely illustrative; for instance, the division of modules is only a logical functional division, and in actual implementation, there may be other division methods. For example, multiple modules or components may be combined or integrated into another system, or some features may be ignored or not executed. Furthermore, the coupling or direct coupling or communication connection shown or discussed may be through some interfaces; the indirect coupling or communication connection between apparatuses or modules may be electrical, mechanical, or other forms.

[0088] The modules described as separate components may or may not be physically separate. The components shown as modules may or may not be physical modules; they may be located in one place or distributed across multiple network modules. Some or all of the modules can be selected to achieve the purpose of this embodiment according to actual needs.

[0089] In addition, the functional modules in the various embodiments of this application can be integrated into one processing module, or each module can exist physically separately, or two or more modules can be integrated into one module.

[0090] If the aforementioned functions are implemented as software functional modules and sold or used as independent products, they can be stored in a computer-readable storage medium. Based on this understanding, the technical solution of this application, in essence, or the part that contributes to the prior art, or a portion of the technical solution, can be embodied in the form of a software product. This computer software product is stored in a storage medium and includes several instructions to cause a computer device (which may be a personal computer, server, or network device, etc.) to execute all or part of the steps of the methods described in the various embodiments of this application. The aforementioned storage medium includes various media capable of storing program code, such as USB flash drives, portable hard drives, read-only memory (ROM), random access memory (RAM), magnetic disks, or optical disks.

[0091] The above description is merely a specific embodiment of this application, but the scope of protection of this application is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in this application should be included within the scope of protection of this application. Therefore, the scope of protection of this application should be determined by the scope of the claims.

[0092] In conclusion, the above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump, characterized in that, include: The data acquisition module is used to collect flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculate the dew point temperature, and construct a curve showing the change in condensable component concentration. The condensation point determination module is used to determine the range between the condensation start point and the condensation end point based on the concentration change curve and the dew point temperature. The heat exchange section division module is used to divide the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section, which are respectively mapped to the heat exchange loops of different heat storage zones. The condensate removal module is used to control the reverse direction of flue gas flow in the medium-temperature induced condensation section and to guide the removed condensate droplets into the liquid guide tank for discharge. The residual discharge module is used to condense residual condensable components in the low-temperature flushing section and transport the condensate and particulates to the discharge channel; The thermal storage regulation module is used to establish a heat accumulation zone inside the reservoir and to perform heat distribution and transfer regulation between reservoirs by calculating equilibrium state parameters.

2. The molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, The data acquisition module collects flue gas temperature, flow rate, and condensable component concentration at the outlet of the mixed biomass combustion, calculates the dew point temperature, and constructs a condensable component concentration change curve. Specifically, this includes: Temperature acquisition units, flow rate acquisition units, condensable component detection units, and humidity detection units are set at several sampling points at the cross-sectional location of the flue gas outlet of the mixed biomass combustion. Each unit collects temperature, flow rate, condensable component concentration, and humidity data at its corresponding location. Humidity data and condensable component concentration data are converted into corresponding partial pressure values, and dew point temperatures at each time point are generated based on gas saturation conditions. The concentration data of condensable components are interpolated and filtered to remove noise in chronological order to obtain a time-continuous concentration sequence. Concentration change curves were established based on the concentration sequence of condensable components and imported into the condensation point determination module.

3. The molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, In the condensation point determination module, the specific range for determining the condensation start and end points based on the concentration change curve and dew point temperature includes: The magnitude of change in the concentration change curve of condensable components at each sampling point is calculated for adjacent time points and compared with a preset concentration change threshold. When there are consecutive sampling points within a set range where the change in concentration is greater than or equal to the concentration change threshold and the corresponding temperature is equal to or lower than the dew point temperature, the first sampling point that meets the conditions is determined as the condensation start point. When there are consecutive sampling points within the set sampling points after the condensation start point where the change amplitude is less than the concentration change threshold and the temperature is lower than the dew point temperature, the first sampling point that meets the conditions is determined as the condensation termination point. Based on the flue gas velocity and heat exchanger size, the time corresponding to the above condensation start point and condensation end point is converted into a physical location interval.

4. The molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, In the heat exchange section division module, the flue gas heat exchanger is divided into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section. The heat exchange loops mapped to different height heat storage sections specifically include: Based on the collected temperature, flow rate and condensable component concentration data, the flue gas heat exchanger is divided into a high-temperature sensible heat section, a medium-temperature induced condensation section and a low-temperature flushing section along the flue gas flow direction. The heat exchange circuit of the molten salt high-temperature layer is labeled as the first heat exchange circuit, and the heat exchange circuit of the molten salt medium-temperature layer is labeled as the second heat exchange circuit. The molten salt high-temperature layer and the molten salt medium-temperature layer correspond to the preset heat storage sections at different heights of the molten salt thermal storage device. The high-temperature sensible heat section is mapped to the first heat exchange loop, while the medium-temperature induced condensation section and the low-temperature flushing section are mapped to the second heat exchange loop.

5. A molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 4, characterized in that, The division of the flue gas heat exchanger into a high-temperature sensible heat section, a medium-temperature induced condensation section, and a low-temperature flushing section along the flue gas flow direction specifically includes: For each sampling location, the rate of temperature change, the rate of flow rate change, and the rate of change of condensable component concentration are calculated, and the three types of change rates are combined into a feature data sequence according to the sampling point location. The three types of change rates at each data collection location are numerically weighted to generate a comprehensive change index for that location. The comprehensive change index along the flue gas flow direction is arranged in sequence, and the position where the first occurrence changes from below the average value to above the average value is taken as the dividing point between the high-temperature sensible heat section and the medium-temperature induced condensation section. Find the next location where the flue gas flow changes from below the average value to above the average value, and use it as the dividing point between the medium-temperature induced condensation section and the low-temperature flushing section; The boundary point is used as the partition index for the current operation, and the comprehensive change index is recalculated and the boundary point position is relocated in each operation.

6. The molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, In the condensate removal module, controlling the flue gas flow direction to reverse within the medium-temperature induced condensation section and guiding the removed condensate droplets into the liquid guide tank for discharge specifically includes: Switch the direction of flue gas entering the medium-temperature induced condensation section and control the flue gas flow direction to be opposite to the outlet direction of the high-temperature sensible heat section; The length of the condensation zone is calculated based on the physical location interval between the condensation start point and the end point. The adjustment step size of the flow rate is set according to the length of the condensation zone. The flue gas velocity in the medium-temperature induced condensation section is continuously increased within a preset range according to the adjustment step size to separate the condensate droplets from the gas flow. The separated condensate droplets are introduced into the liquid guiding tank along the wall and drained according to a preset cycle.

7. A molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, The residual discharge module specifically includes the following steps to transport residual condensate and particulate matter to the discharge channel: During the low-temperature flushing stage, the flue gas output from the medium-temperature induced condensation stage is received and distributed into several uniform flow paths. The residual condensate and particulate matter are transported to the discharge channel to discharge the liquid and particulate matter.

8. A molten salt thermal energy storage system based on hybrid biomass combustion and a high-temperature heat pump according to claim 1, characterized in that, The thermal storage regulation module establishes a heat accumulation zone within the reservoir and performs heat distribution and transfer regulation between reservoirs by calculating equilibrium state parameters, specifically including: The heat from the high-temperature sensible heat section is transferred to the molten salt high-temperature layer through the first heat exchange loop, and a high-temperature heat accumulation zone is established inside the reservoir. The heat from the medium-temperature induced condensation section and the low-temperature flushing section is transferred to the molten salt medium-temperature layer through the second heat exchange loop, and a medium-temperature heat accumulation zone is established inside the reservoir. During operation, the heat storage distribution in the high-temperature heat accumulation zone and the medium-temperature heat accumulation zone is obtained respectively, and the offset ratio with the preset equilibrium heat storage distribution is calculated. The offset ratio is marked as the equilibrium state parameter. Based on the equilibrium state parameters, heat distribution and transfer regulation is performed between reservoirs, and the equilibrium state parameters are fed back to the heat exchange section division module.

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