A cyclone heat exchange coalescing sprayer for flue gas waste heat recovery, a heat pump system comprising the sprayer and a method of operation

Abstract

The application discloses a cyclone heat exchange and spray combined sprayer for flue gas waste heat recovery, a heat pump system comprising the sprayer and an operation method, and belongs to the technical field of flue gas waste heat recovery and heat energy utilization. The sprayer adopts a tangential cyclone air inlet structure, a plurality of reinforced converging conical discs are arranged in the tower, and an initial sedimentation liquid collecting tank integrated with a sedimentation partition plate, a water quality detector and an intelligent blowdown mechanism is arranged at the bottom; the heat pump system is provided with at least two groups of the sprayer, adaptive switching of single-tower, double-tower parallel and series operation modes is realized through a three-way valve group, and an intelligent control module with a working condition soft measurement function is combined to dynamically optimize the system operation state. The application significantly strengthens the gas-liquid heat transfer and mass transfer efficiency, realizes in-situ purification of a circulating working medium and direct coupling of a heat pump evaporator, reduces system energy consumption and the risk of scaling and corrosion, improves the energy efficiency and stability in all working conditions, and is suitable for flue gas waste heat deep recovery scenes of industrial boilers, waste incineration power generation and the like.

Description

Technical Field

[0001] This invention relates to a swirl heat exchanger and agglomerating sprayer for flue gas waste heat recovery, a heat pump system including the sprayer, and an operation method thereof, belonging to the field of flue gas waste heat recovery and thermal energy utilization technology. Background Technology

[0002] For the recovery and reuse of waste heat from low-temperature, high-humidity flue gas, existing technologies have primarily focused on direct contact heat exchange with the flue gas coupled with absorption heat pumps. For example, Chinese invention patent application CN109945278A discloses a system for deep recovery of waste heat from flue gas. This system utilizes a waste heat recovery tower and a spray layer to create counter-current contact heat exchange between the circulating working fluid and the flue gas. When the exhaust gas temperature drops below the dew point, the system can simultaneously recover both sensible and latent heat, which is then upgraded by an absorption heat pump before being supplied to the heating network. This type of solution demonstrates excellent performance in improving energy efficiency and has become a typical method in the field of waste heat recovery.

[0003] However, in practical applications, traditional spray tower structures are limited by physical constraints such as low relative gas-liquid velocity, uneven flow field distribution, and short contact time. When dealing with complex operating conditions, they struggle to simultaneously meet the multiple demands of high-intensity heat and mass exchange, synergistic dust removal, and water quality control. A single spray flow field lacks efficient interphase mass transfer enhancement and droplet coalescence mechanisms, resulting in insufficient capture capacity for fine particulate matter and acidic pollutants. This leads to rapid accumulation of impurities in the circulating working fluid, severely restricting heat and mass exchange efficiency and the long-term stability of the system. Acidic components such as SO2 in flue gas readily transfer to the liquid phase during spray heat exchange. Although adding alkaline solutions (such as NaOH solution) can alleviate acid corrosion to some extent, the continuous accumulation of impurities in the circulating working fluid still leads to water quality deterioration and serious scaling and fouling risks. Because absorption heat pumps are highly sensitive to the water quality of the circulating working fluid, the system typically cannot achieve direct coupling between the circulating working fluid and the heat pump evaporator, requiring the addition of a corrosion-resistant plate heat exchanger to construct an intermediate heat exchange link. This not only causes the loss of effective temperature difference during the heat transfer process, leading to a decrease in energy extraction efficiency, but also significantly increases the difficulty of system integration and the initial construction cost.

[0004] To overcome the limitations of low gas-liquid contact efficiency in traditional spray structures, existing technologies (such as CN111457408A) introduce a swirling enhancement mechanism to improve gas-liquid heat and mass transfer efficiency. This technology utilizes the strong shear force generated by the swirling flow field to break droplets into dispersed microdroplets with extremely high specific surface areas; simultaneously, the swirling gas drives the microdroplets to rotate at high speed, enhancing internal circulation and surface renewal within the microdroplets, significantly reducing mass transfer resistance. Although existing swirling jet schemes exhibit significant enhancement characteristics at the microdynamic level and possess certain physical dust removal potential, their functional boundaries are limited to a single heat exchange target and are highly dependent on downstream liquid collection, alkali neutralization, and multi-stage water storage units, failing to fundamentally solve the problems of low system integration and complex operation and maintenance.

[0005] Furthermore, existing systems mostly operate with a fixed flow path and single tower, making it difficult to adapt to large-scale load fluctuations in boilers. Under low load conditions, this can easily lead to additional energy losses, while under high load conditions, it can easily cause excessively high system back pressure, lacking flexible adaptive flow path control methods. At the same time, existing systems generally employ open-loop control strategies, lacking the perception and closed-loop control of flue gas condition fluctuations and circulating fluid water quality status, resulting in a low level of information technology and making it difficult for the system to achieve optimal energy efficiency operation based on real-time heat load demands.

[0006] In summary, existing absorption heat pump spray recovery systems are limited by the physical bottlenecks of traditional sprayers and their low level of intelligence. They generally suffer from problems such as excessive circulating working fluid flow, continuous water quality deterioration, and poor flow path control flexibility, severely hindering the widespread application of this technology. Therefore, there is an urgent need to develop an intelligent sprayer system with multi-functional deep coupling characteristics. This system should achieve enhanced heat transfer through swirling flow, efficient droplet coalescence, in-situ physical dust removal, and improved circulating working fluid quality. Simultaneously, it should be able to achieve adaptive switching and collaborative control of the flow path under multiple operating conditions through information technology, thereby simplifying the system structure and improving operational stability and energy efficiency. Summary of the Invention

[0007] To address the problems existing in the background art, the present invention provides a swirl heat exchanger and a heat pump system including the sprayer for flue gas waste heat recovery, and an operation method thereof.

[0008] To achieve the above objectives, the present invention adopts the following technical solution: a cyclone heat exchanger and coalescing sprayer for flue gas waste heat recovery, comprising a flue gas inlet pipe, an upper tower body, a lower tower body, an underflow pipe, a solution outlet pipe, an integrated primary sedimentation collection tank, an intelligent drain valve, a drain outlet, a settling baffle, a water quality analyzer, a reinforced coalescing cone, a flue gas outlet pipe, an overflow pipe, and an atomizing nozzle assembly; the upper tower body and the lower tower body are vertically connected and fixed, the upper tower body is a cylindrical structure, and the lower tower body is a single cone structure; the upper end of the side wall of the upper tower body is connected to at least one tangentially arranged flue gas inlet pipe, and an atomizing nozzle assembly is installed inside the flue gas inlet pipe; the spray direction of all nozzles in the atomizing nozzle assembly is pointing towards the inside of the upper tower body; the upper tower body... An overflow pipe is connected to the upper end of the upper tower body, and the side wall of the overflow pipe is connected to the flue gas outlet pipe. Multiple stages of reinforced coalescence cones are installed inside the upper tower body along its height. The lower end of the lower tower body is connected to an integrated primary sedimentation collection tank via an underflow pipe. Multiple sets of sedimentation baffles are arranged inside the integrated primary sedimentation collection tank. The bottom of the integrated primary sedimentation collection tank has a conical structure that tapers towards the center, and a drain pipe is located at the end. The drain pipe is connected to an intelligent drain valve. The solution outlet pipe is located in the upper middle part of the side wall of the integrated primary sedimentation collection tank. A water quality analyzer is also sealed and fixed to the side wall of the integrated primary sedimentation collection tank. The sensor probe of the water quality analyzer extends into the supernatant area above the sedimentation baffles.

[0009] Furthermore, the upper tower body is a cylindrical structure, and the lower tower body is a conical structure.

[0010] Furthermore, the outer wall of the upper tower body is provided with multiple upper outward protrusions, and the outer wall of the lower tower body is provided with multiple lower outward protrusions, with the upper outward protrusions and lower outward protrusions corresponding and connected one-to-one.

[0011] Furthermore, the upper tower body is a prism-shaped structure, and the lower tower body is a pyramid-shaped structure.

[0012] Furthermore, the walls of both the upper and lower tower bodies have a continuous spiral corrugated structure. The spiral direction of the corrugated structure is consistent with the main swirling flow formed by the tangential intake of flue gas, and extends continuously spirally from bottom to top along the tower body axis. The crests and troughs of the corrugations are evenly distributed alternately along the tower body axis, forming a continuous spiral guide channel on the inner wall of the tower body. The flow cross section of the spiral guide channel is distributed in a periodic contraction-expansion-recontraction pattern along the spiral extension direction of the channel.

[0013] Furthermore, the settling baffle is one or more combinations of inclined zigzag plates, multi-stage sawtooth plates, or honeycomb inclined plates.

[0014] Furthermore, a demisting element is installed inside the overflow pipe.

[0015] Furthermore, the enhanced coalescence cone disk is either an annular cone disk or a baffle cone disk, and has two forms, as detailed below:

[0016] Format 1:

[0017] Multiple reinforced coalescing cones are arranged at intervals along the height of the tower, and their radial dimensions decrease from top to bottom; a vertically connected flow channel is formed between two adjacent reinforced coalescing cones, and the flow channel is tapered from top to bottom;

[0018] Form Two:

[0019] Multiple reinforced coalescing cones have the same radial dimension, and each reinforced coalescing cone has a main channel at its edge. The main channels of every two adjacent reinforced coalescing cones are staggered and alternately positioned.

[0020] This invention discloses a heat pump system including a cyclone heat exchanger and coalescing sprayer for flue gas waste heat recovery. The system comprises a circulating pump, an absorption heat pump, an intelligent control module, a three-way regulating valve, a three-way switching valve group, and at least two sets of parallel-arranged cyclone heat exchanger and coalescing sprayers. The three-way switching valve group includes a flue gas proportioning valve, a liquid distribution valve, a series-parallel switching valve, and a liquid junction valve, each equipped with a switching actuator for automatic switching between single-tower operation, dual-tower parallel operation, and dual-tower series operation modes. The absorption heat pump includes an evaporator, an absorber, a generator, and a condenser. The generator has a heating coil internally connected to an external driving heat source unit. The solution outlet pipe of the cyclone heat exchanger and coalescing sprayer is connected to the inlet of the circulating pump, and the outlet of the circulating pump is connected to the inlet of the three-way regulating valve. The first outlet of the three-way regulating valve is connected to the heat source side inlet of the evaporator, and the second outlet is connected via a bypass... The pipeline is directly connected to the inlet of the atomizing nozzle assembly; the intelligent control module integrates an operating parameter sensing unit, configured to obtain real-time status signals of the flue gas side and the working fluid side through data interaction with the external control system and water quality analyzer; the operating parameter sensing unit obtains dynamic back pressure and flow rate by monitoring the current and frequency of the circulating pump and combining it with a preset flow resistance curve to achieve soft measurement of operating conditions; the intelligent control module is used to calculate the heat exchange efficiency ratio and dynamically adjust the opening of the three-way regulating valve to optimize the distribution ratio of the circulating working fluid between the heat source side of the evaporator and the bypass pipeline; the heat source side outlet of the evaporator is connected to the atomizing nozzle assembly after merging with the bypass pipeline, the user-side return water pipe is connected to the hot water side inlet of the absorber, the hot water side outlet of the absorber is connected to the hot water side inlet of the condenser, and the hot water side outlet of the condenser is connected to the user-side water supply network, thus constructing a heat cascade enhancement path.

[0021] The present invention discloses an operation method for a heat pump system including a cyclone heat exchanger and polymer sprayer for flue gas waste heat recovery, the method comprising the following steps:

[0022] S1: The flue gas purified upstream is tangentially introduced into the upper tower of the swirl heat exchanger and agglomeration sprayer through the flue gas inlet pipe to construct a circumferential high-speed swirling field;

[0023] S2: The circulating working fluid is delivered to the atomizing nozzle assembly, where it is atomized into fine droplets and then enters the upper tower tangentially along with the flue gas.

[0024] S3: Under the synergistic effect of the swirling centrifugal field and the multi-stage enhanced coalescence cone disk, the gas and liquid phases migrate towards the tower wall and are wetted and captured, forming a dynamically renewed continuous liquid film; as the flux increases, the liquid film converges and becomes unstable and breaks down, coalescing into large-scale droplets, which overcome the airflow drag and fall back to the integrated primary sedimentation collection tank at the bottom. The multi-stage laminar flow unit composed of internal sedimentation baffles realizes the in-situ sedimentation and purification self-balance of solid and liquid impurities.

[0025] S4: The flue gas after preliminary separation continues to rise to the overflow pipe to capture the remaining droplets; the liquid phase formed by the capture is driven by gravity to fall back to the integrated primary sedimentation tank, and the flue gas after deep cooling, dehumidification and purification is discharged from the flue gas outlet pipe.

[0026] S5: The circulating working fluid collected in the integrated primary sedimentation collection tank is monitored in real time by a water quality analyzer for its pH value and conductivity, and the results are fed back to the intelligent control module. When the pH value or conductivity exceeds the preset threshold, the intelligent control module opens the intelligent drain valve to perform reduced-volume directional sewage discharge.

[0027] S6: The intelligent control module, based on the real-time flue gas flow, system back pressure, and user-side heat load demand obtained by the operating parameter sensing unit, coordinates and drives the three-way switching valve group to dynamically switch the operating mode.

[0028] S7: The purified circulating working fluid is pressurized by the circulating pump and sent to the three-way regulating valve. The intelligent control module dynamically allocates the flow rate according to the heat pump's operating characteristics. Part of the circulating working fluid enters the heat source side of the evaporator, serving as a low-grade heat source to drive the low-pressure refrigerant in the evaporator to absorb heat and evaporate, releasing heat and cooling down. The other part is directly output through the bypass pipeline. The low-temperature working fluid after heat release mixes and adjusts the temperature with the heat working fluid in the bypass branch at the junction point and is then sent to the atomizing nozzle assembly for recycling.

[0029] S8: The low-pressure refrigerant vapor generated by the evaporator of the absorption heat pump enters the absorber, is absorbed by the concentrated solution, and the released heat preheats the return water on the user side.

[0030] S9: The absorbed dilute solution enters the generator, and after being heated by an external driving heat source, high-pressure refrigerant vapor is separated. This vapor enters the condenser and releases condensation heat, which is used to reheat the preheated user-side return water.

[0031] S10: The return water from the user side flows sequentially through the hot water side of the absorber and the hot water side of the condenser. Through the stepwise absorption of heat at different energy levels, the water temperature is continuously increased and finally delivered to the user side water supply network after reaching the preset heating temperature.

[0032] Compared with the prior art, the beneficial effects of the present invention are:

[0033] 1. This invention constructs a high-speed swirling flow field by tangential swirling air intake, and uses strong shear force to induce droplet dispersion and generate high-speed rotation, which significantly thins the heat and mass transfer boundary layer, accelerates the gas-liquid interface renewal, and greatly improves the heat and mass exchange intensity per unit volume. This solves the physical limitations of traditional spray towers, such as low relative gas-liquid velocity, uneven flow field distribution, and short contact time.

[0034] 2. This invention achieves in-situ aggregation and capture of microdroplets and fine particles through the synergistic effect of a swirling centrifugal force field and a multi-stage enhanced aggregation cone disk. Combined with a multi-stage laminar flow sedimentation structure of a bottom-integrated primary sedimentation collection tank, it achieves efficient separation of solid and liquid impurities. Combined with online water quality monitoring and intelligent closed-loop control of sewage discharge, it effectively curbs the enrichment of acidic components and salts in the circulating working fluid, solves the scaling and corrosion problems caused by the deterioration of the circulating working fluid, and significantly reduces the dependence on complex downstream water treatment units.

[0035] 3. Relying on the in-situ purification capability of the swirl heat exchanger and agglomeration sprayer, this invention eliminates the redundant intermediate anti-corrosion plate heat exchanger in the traditional system, realizing direct heat exchange between the circulating working fluid and the absorption heat pump evaporator. While reducing the equipment footprint and construction cost, it effectively reduces the effective temperature difference loss during the heat exchange process, significantly improving the system integration and overall energy utilization efficiency.

[0036] 4. This invention, by setting at least two sets of parallel sprayers and cooperating with a three-way switching valve group, constructs three dynamically switchable operating modes: single tower, parallel double tower, and series double tower. It can adjust the flow path in real time according to boiler load fluctuations, flue gas flow changes, and user heat demand, avoiding the problems of excessive back pressure under high load and energy efficiency deviation from the optimal range under low load. It significantly improves the system's environmental adaptability and service life under complex flue gas conditions, and at the same time, it can realize online maintenance without shutting down the system.

[0037] 5. This invention integrates an intelligent control module with operating condition soft measurement function, which can acquire the operating status parameters of the flue gas side and the working fluid side in real time, dynamically adjust the distribution ratio of the circulating working fluid between the evaporator and the bypass pipeline, and accurately match the heat pump operating characteristics with the user's heat load demand; at the same time, it realizes targeted reduction of sewage discharge based on real-time water quality monitoring data, ensuring the long-term stable operation of the system, and solving the problems of open-loop control, low level of informatization, and mismatch between energy consumption and heat demand in traditional systems. Attached Figure Description

[0038] Figure 1 This is a schematic diagram of the structure of the swirl heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to Embodiment 1 of the present invention;

[0039] Figure 2 This is a schematic diagram of the structure of the heat pump system of the present invention, which includes a swirl heat exchanger and a coalescing sprayer for waste heat recovery of flue gas.

[0040] Figure 3 This is a schematic diagram of the structure of the swirl heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to Embodiment 2 of the present invention, wherein: (a) is the front view, (b) is the side view, and (c) is the top view;

[0041] Figure 4 This is a schematic diagram of the structure of the swirl heat exchanger agglomeration sprayer for flue gas waste heat recovery according to Embodiment 3 of the present invention, wherein: (a) is the front view, (b) is the side view, and (c) is the top view;

[0042] Figure 5 This is a schematic diagram of the structure of the swirl heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to Embodiment 4 of the present invention;

[0043] Figure 6 This is a schematic diagram of the installation structure of another demisting element of the present invention;

[0044] Figure 7 This is a schematic diagram of the installation structure of another form of the reinforced coalescing cone disk of the present invention;

[0045] Figure 8 This is a schematic diagram of the installation structure of the flue gas inlet pipe;

[0046] Figure 9 These are schematic diagrams of the installation structures of two types of settlement baffles of the present invention, wherein: (a) is a multi-level sawtooth plate, and (b) is a top view of a honeycomb inclined plate. Detailed Implementation

[0047] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the invention, not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0048] Example 1:

[0049] A cyclone heat exchanger agglomeration sprayer for flue gas waste heat recovery includes a flue gas inlet pipe 1, an upper tower body 2, a lower tower body 3, an underflow pipe 4, a solution outlet pipe 5, an integrated primary sedimentation collection tank 6, an intelligent drain valve 7, a drain outlet 8, a settling baffle 9, a water quality analyzer 10, a reinforced agglomeration cone 11, a flue gas outlet pipe 14, an overflow pipe 15, and an atomizing nozzle assembly 16.

[0050] The upper tower body 2 and the lower tower body 3 are vertically connected and integrally formed and fixed.

[0051] The upper tower body 2 is a cylindrical structure, and the lower tower body 3 is a single cone structure that contracts along the axial direction. Its cone angle (twice the angle between the generatrix of the cone and the axis of the tower) is adjustable in the range of 10° to 180°.

[0052] in:

[0053] When the cone angle is in the range of 10° to 45°, the lower tower body 3 has a longer axial swirling residence space, which is beneficial to enhance the collision and aggregation effect of fine droplets under centrifugal force.

[0054] When the included angle of the cone is in the range of 90° to 150°, the overall height of the equipment can be significantly reduced, making it suitable for retrofitting projects with limited space.

[0055] By selecting specific parameters within the aforementioned angle range, both droplet coalescence and separation effects and equipment compactness can be achieved without significantly increasing the pressure drop inside the tower.

[0056] The upper end of the side wall of the upper tower body 2 is connected to at least one tangentially arranged flue gas inlet pipe 1, and the tangential arrangement allows the flue gas to obtain a larger circumferential velocity when entering the tower body.

[0057] Multiple flue gas inlet pipes 1 can be evenly distributed along the circumference of the tower body. For example, two flue gas inlet pipes 1 spaced 180° apart along the circumference can be installed, as shown in the specific structure. Figure 8 As shown.

[0058] The angle between the axis of each flue gas inlet pipe 1 and the tangent direction at the intersection of the axis and the inner wall of the upper tower body 2 in the circumferential plane is preferably controlled within the range of 0°~30° to ensure that the flue gas has sufficient tangential momentum after entering the tower body;

[0059] When the included angle is 0°, it is a strictly tangential arrangement, which can create the most intense stable swirling field. When the included angle is greater than 0°, it is an approximately tangential arrangement, which can still form a stable swirling flow inside the tower.

[0060] An atomizing nozzle assembly 16 is installed inside the flue gas inlet pipe 1. The atomizing nozzle assembly 16 includes a liquid supply pipe arranged circumferentially along the inner wall of the flue gas inlet pipe 1 and multiple nozzles evenly distributed on the liquid supply pipe. The spray direction of all nozzles in the atomizing nozzle assembly 16 is pointing upwards into the tower body 2, which is used to atomize the circulating working medium into fine droplets and enter the swirling field inside the tower body along with the flue gas. The circulating working medium can be selected from process water, demineralized water, or a modified solution with added antifreeze and corrosion inhibitors, depending on the working conditions.

[0061] An overflow pipe 15 is connected to the upper end of the upper tower body 2. The side wall of the overflow pipe 15 is connected to the flue gas outlet pipe 14, and the flue gas outlet pipe 14 is connected to the downstream chimney.

[0062] The interior of the upper tower body 2 is equipped with reinforced coalescing cones 11 with multiple intervals along the height direction via support members. The number of layers of reinforced coalescing cones 11 can be adjusted according to the amount of flue gas to be processed and the tower diameter. By designing the number of layers as an adjustable parameter, the adaptability to different boiler loads and flue gas conditions is enhanced.

[0063] The connection between the upper tower body 2 and the reinforced coalescing cone disk 11 is as follows: a flange or support edge is provided on the outer edge of the reinforced coalescing cone disk 11, and it is fixed to the tower wall by means of brackets and bolts, clamping structure, etc.

[0064] The reinforced conical disc 11 and its supporting components are preferably made of corrosion-resistant materials such as 316L stainless steel or duplex stainless steel. The connecting bolts can be made of anti-loosening nuts or spring washers to prevent loosening and falling off during long-term operation.

[0065] The lower end of the lower tower body 3 is connected to the integrated primary sedimentation collection tank 6 through the underflow pipe 4;

[0066] The integrated primary sedimentation collection tank 6 is equipped with multiple sets of sedimentation baffles 9. The sedimentation baffles 9 divide the internal space of the collection tank into multiple micro-scale laminar flow units through a multi-level structure arranged at an angle. The increased effective sedimentation area and shortened sedimentation path significantly improve the particulate matter capture efficiency.

[0067] The integrated primary sedimentation collection tank 6 has at least one set of supporting beams horizontally arranged inside. The two ends of the supporting beams are respectively fixedly welded to the inner walls of the opposite tank. The supporting beams are equipped with positioning components for fixing the sedimentation baffles 9.

[0068] The bottom of the integrated primary sedimentation collection tank 6 is a tapered structure that tapers towards the center, and a drain pipe 8 is provided at the end. The drain pipe 8 is connected to the intelligent drain valve 7. Under operating conditions, fine particles in the dust-laden flue gas come into contact with the circulating working medium inside the tower and are captured along with the droplets, settling to the bottom of the integrated primary sedimentation collection tank 6. The solution outlet pipe 5 is located in the upper middle part of the side wall of the integrated primary sedimentation collection tank 6. The solution outlet pipe 5 is connected to an external circulation pump and is used to extract the purified supernatant and send it to the external circulation system.

[0069] The side wall of the integrated primary sedimentation collection tank 6 is also provided with an installation hole, and a water quality tester 10 is sealed and fixed thereon. The sensing probe of the water quality tester 10 extends into the supernatant area above the sedimentation baffle 9.

[0070] The water quality analyzer 10 can monitor the pH value and conductivity of the circulating working fluid in real time and transmit the monitoring data to the intelligent control module. When the monitored value reaches the set threshold, it indicates that acidic components or salts are enriched, and the intelligent drain valve 7 is opened in conjunction with the system to discharge the high solid content sludge accumulated at the bottom to the plant's sewage treatment system, thereby realizing online purification and quality control of the circulating working fluid and curbing the risk of scaling and corrosion of the downstream heat pump unit and heat exchange pipeline.

[0071] Furthermore, the settling baffle 9 is one or more combinations of inclined zigzag plates, multi-level sawtooth plates, or honeycomb inclined plates.

[0072] Specifically as follows:

[0073] Form 1: Inclined zigzag plate, wherein the settlement partition 9 extends in a corrugated or zigzag shape along the inclined direction, forming a continuous alternating turning surface;

[0074] Form 2: Multi-stage serrated plate, wherein the surface of the settling baffle 9 is provided with equally spaced serrated protrusions to construct a multi-stage nonlinear flow channel;

[0075] When the settlement diaphragm 9 is a slanted zigzag plate or a multi-stage sawtooth plate, the positioning component is a base with several equally spaced positioning slots, and the middle or edge of the settlement diaphragm 9 is embedded in the positioning slots.

[0076] Form 3: Honeycomb inclined plate, wherein the settlement partition 9 is composed of a regular hexagon or porous tubular array arranged at an incline to form a parallel constrained settlement space.

[0077] When the settlement diaphragm 9 is a honeycomb inclined plate, the positioning component is a support frame set on the support beam, which is used to lift and limit the honeycomb inclined plate.

[0078] Through structural optimization of the settling baffle 9, the integrated primary settling collection tank 6 can effectively buffer the mechanical impact of the injected liquid flow, suppress the secondary lifting of sludge at the bottom of the tank, and ensure that the upper reflux area is always a high-quality supernatant, thus achieving a balance between in-situ efficient separation of particulate matter and self-purification of system quality.

[0079] Furthermore, a demisting element is installed inside the overflow pipe 15 to capture residual mist droplets in the rising flue gas.

[0080] The demisting element is any one of the following: a combined demisting structure consisting of an overflow baffle 12 and an overflow cone 13, a baffle plate demister, a wire mesh demister, a fiber bed demister, or a cyclone demister.

[0081] An overflow cone 13 is fixedly connected to the axis of the overflow pipe 15 via a rod. An inverted cone-shaped overflow baffle 12 is installed on the inner wall of the overflow pipe 15. The overflow baffle 12 is correspondingly arranged at the lower end of the overflow cone 13. A gap is left between the overflow baffle 12 and the overflow cone 13, which can perform secondary agglomeration and capture of residual droplets in the rising flue gas, and return the captured liquid to the tower body or the integrated primary sedimentation collection tank 6.

[0082] This invention does not limit the specific form of the demisting element. In addition to the above-mentioned combined demisting structure, baffle plate demisters, wire mesh demisters, fiber bed demisters, or cyclone demisters can also be selected. As long as they can effectively capture the mist droplets rising with the flue gas and return them to the tower body, they are all within the protection scope of this invention.

[0083] Furthermore, the enhanced coalescence cone disk 11 is an annular cone disk or a baffle cone disk, and has two forms, as detailed below:

[0084] Form 1: Gradual narrowing channel type:

[0085] Multiple enhanced coalescence cones 11 are arranged at intervals along the height of the tower body, and their radial dimensions decrease from top to bottom; a vertically connected flow channel is formed between two adjacent enhanced coalescence cones 11, and the flow channel is gradually narrowed from top to bottom, which is used to enhance the collision, coalescence and separation of droplets and fine particles under the action of centrifugal force and cone guide, while guiding the uniform flow of gas and liquid phases.

[0086] Form 2: Staggered channel type:

[0087] Multiple reinforced coalescing cones 11 have the same radial dimension. Each reinforced coalescing cone 11 has a main channel at its edge. The main channels of every two adjacent reinforced coalescing cones 11 are staggered and alternately positioned.

[0088] As the gas and liquid phases rotate and rise within the tower, they pass through each layer of enhanced coalescence cone disk 11 in sequence. The fluid is continuously forced to change its flow direction at different height positions, forming a spiral and reversible three-dimensional flow path, which significantly increases the number of contacts and collision opportunities between the droplets and the cone disk surface, further enhancing the droplet coalescence and demisting effect.

[0089] To address the potential presence of acidic components in the flue gas and the quality deterioration of the circulating working fluid during continuous operation, this embodiment incorporates optimized corrosion protection design for the tower body and piping materials. Specifically, the tower shell is preferably made of carbon steel (such as Q235B or Q345R), and the entire inner surface of the tower is lined with a corrosion-resistant layer, such as an acid-resistant rubber lining, glass flake coating, or fiberglass lining, to improve its resistance to corrosion from acidic components such as SO2 and HCl, as well as the circulating working fluid.

[0090] Key components inside the tower that come into direct contact with the circulating working fluid, such as the atomizing nozzle assembly 16, the reinforced coalescence cone 11, the integrated primary sedimentation collection tank 6, and the sedimentation baffle 9, are preferably made of 316L stainless steel, 2205 duplex stainless steel, or other acid-resistant alloy materials. Solution circulation pipelines and circulation pump flow parts can be made of 316L stainless steel or carbon steel pipes lined with fluoroplastics to balance strength and corrosion resistance.

[0091] For operating conditions with high flue gas temperature or high acid gas content, wear-resistant and corrosion-resistant coatings can be locally added near the flue gas inlet pipe 1 and the lower inner wall of the lower tower body 3 to reduce the impact of fly ash erosion and flue gas condensation acid corrosion on the tower body.

[0092] The present invention provides a heat pump system including a swirl heat exchanger and a coalescing sprayer for flue gas waste heat recovery, comprising at least two sets of swirl heat exchangers and coalescing sprayers arranged in parallel, an absorption heat pump 22, a circulating pump 17, a three-way regulating valve 105, a three-way switching valve group, and an intelligent control module 23.

[0093] The three-way switching valve group includes a flue gas proportioning valve 101, a liquid distribution valve 102, a series-parallel switching valve 103, and a liquid junction valve 104, all equipped with electric switch actuators to automatically switch between single-tower operation, dual-tower parallel operation, and dual-tower series operation modes. The absorption heat pump 22 includes an evaporator 18, an absorber 19, a condenser 21, and a generator 20. The generator 20 has a heating coil connected to an external driving heat source unit. The driving heat source unit can provide low-pressure extraction steam from a steam turbine or saturated steam from a boiler to heat the dilute solution to generate refrigerant vapor and regenerate it into a concentrated solution.

[0094] The solution outlet pipe 5 at the bottom of the swirl heat exchanger agglomerating sprayer is connected to the inlet of the circulating pump 17, and the outlet of the circulating pump 17 is connected to the inlet of the three-way regulating valve 105. The first outlet of the three-way regulating valve 105 is connected to the heat source side inlet of the evaporator 18, and the second outlet is directly connected to the inlet of the atomizing nozzle assembly 16 via a bypass pipe. The heat source side outlet of the evaporator 18 is connected to the atomizing nozzle assembly 16 after merging with the bypass pipe. The user-side return water pipe is connected to the hot water side inlet of the absorber 19, the hot water side outlet of the absorber 19 is connected to the hot water side inlet of the condenser 21, and the hot water side outlet of the condenser 21 is connected to the user-side water supply network, thus constructing a heat cascade enhancement path.

[0095] The intelligent control module 23 integrates an operating parameter sensing unit, configured to acquire real-time status signals on the flue gas side and the working fluid side through data interaction with the external control system and the water quality analyzer 10. This operating parameter sensing unit monitors the current and frequency of the circulating pump 17 and, in conjunction with a preset flow resistance curve, analyzes and obtains the system's dynamic back pressure and circulating working fluid flow rate, achieving soft measurement of operating conditions. This eliminates the need for numerous additional flow and pressure sensors, reducing system hardware costs and failure rates. The intelligent control module 23 can calculate the system's heat exchange efficiency ratio based on real-time operating parameters and dynamically adjust the opening of the three-way regulating valve 105 to optimize the distribution ratio of the circulating working fluid between the heat source side of the evaporator 18 and the bypass pipeline, precisely matching the heat pump's operating characteristics with the user's heat load requirements, thus achieving optimal system energy efficiency.

[0096] In addition, the heat exchange between the circulating working fluid and the user-side return water can also be achieved using submerged heat exchange coils within the tower. Specifically, spiral or serpentine heat exchange coils are arranged within the integrated primary settling tank 6, with user-side return water or circulating water flowing through the coils, and the outer side of the coils submerged by the high-temperature circulating working fluid. The circulating working fluid exchanges sensible heat with the return water in the coils within the settling tank, outputting the waste heat from the flue gas obtained in the sprayer as hot water. Since the heat exchange coils are located in the settling tank area at the bottom of the tower, they have minimal impact on the main swirling flow field within the upper tower body 2 and the lower tower body 3, allowing for direct heating within the tower without significantly disrupting the swirling structure.

[0097] The present invention discloses an operation method for a heat pump system including a cyclone heat exchanger and polymer sprayer for flue gas waste heat recovery, the method comprising the following steps:

[0098] S1: The flue gas purified by upstream denitrification, deacidification and dust removal is tangentially introduced into the upper tower 2 of the cyclone heat exchanger agglomeration sprayer through flue gas inlet pipe 1 to construct a circumferential high-speed and stable cyclone field.

[0099] S2: After the circulating working fluid is formed into fine droplets through the atomizing nozzle assembly 16, it enters the upper tower body 2 tangentially with the flue gas. Under the action of swirling shear force, the droplets generate high-speed rotation and accelerate interface renewal, significantly reducing the interface thermal resistance and achieving efficient absorption of sensible and latent heat of flue gas. This can reduce the flue gas temperature from 150℃~180℃ to about 40℃~55℃, and significantly reduce the moisture content of the outlet flue gas.

[0100] S3: Under the synergistic effect of the swirling centrifugal field and the multi-stage enhanced coalescence cone disk 11, the microdroplets migrate towards the tower wall and are wetted and captured, forming a dynamically renewed continuous liquid film. As the flux increases, the liquid film converges and becomes unstable and breaks down, coalescing into large-scale droplets. Overcoming the airflow drag, the droplets fall back to the integrated primary sedimentation collection tank 6 at the bottom. The multi-stage laminar flow unit composed of internal sedimentation baffles 9 achieves in-situ sedimentation and purification self-balance of solid and liquid impurities.

[0101] S4: After initial separation, the flue gas continues to rise to the overflow pipe 15, where the internal demisting element induces the airflow to make a violent turn and local acceleration. The residual microdroplets are deeply captured through inertial collision and interception mechanisms. The captured liquid phase is driven by gravity to fall back to the integrated primary sedimentation collection tank 6. After multi-stage aggregation and top demisting, the flue gas discharged from the top of the tower is basically free of mist droplets. The clean flue gas after cooling and dehumidification is discharged into the downstream chimney through the flue gas outlet pipe 14.

[0102] S5: The circulating working fluid collected in the integrated primary sedimentation collection tank 6 is monitored in real time by the water quality tester 10 for its pH value and conductivity, and the feedback is sent to the intelligent control module 23. When the pH value or conductivity exceeds the preset threshold, it means that the acidic components or salts in the circulating working fluid have accumulated to the limit. The intelligent control module 23 opens the intelligent drain valve 7 to perform volume reduction and directional draining, and discharges the high solid content mud at the bottom to maintain the quality of the circulating working fluid and prevent scaling and corrosion of the heat pump evaporator 18.

[0103] S6: Multi-condition adaptive flow path switching and coordinated control steps: The intelligent control module 23, based on the real-time flue gas flow rate, system back pressure, and user-side heat load demand obtained by the operating parameter sensing unit, coordinates and drives the three-way switching valve group to dynamically switch the operating mode.

[0104] Specifically, it includes the following three modes:

[0105] Format 1: Single-tower operation mode. When the flue gas flow rate or heat load demand is less than 50% of the rated operating condition, or when a maintenance command for a specific tower is received, the intelligent control module 23 drives the flue gas proportioning valve 101 to switch to a one-way conduction state to cut off the inlet of the controlled tower, and the linkage series-parallel switching valve 103 switches to the direct discharge channel to ensure that the flue gas of the operating tower directly enters the main pipe; at the same time, it drives the liquid distribution valve 102 to close the liquid branch leading to the controlled tower, and supplies the full amount of circulating working fluid to the operating tower; it drives the liquid junction valve 104 to close the solution outlet of the controlled tower to prevent backflow of accumulated liquid; this mode ensures mass transfer efficiency by maintaining a high liquid-to-gas ratio in the operating tower, and can realize online maintenance and non-stop operation of the waste heat recovery system;

[0106] Form 2: Parallel operation mode of dual towers. When high heat load demand, peak flue gas flow, or system back pressure exceeds the preset threshold is detected, the intelligent control module 23 drives the flue gas proportioning valve 101 to open the diversion mode, and the series-parallel switching valve 103 switches to the direct discharge channel, constructing a symmetrical parallel dual flow channel and doubling the flue gas flow area; at the same time, it drives the liquid distribution valve 102 to distribute the spray liquid in equal amounts, and drives the liquid confluence valve 104 to fully open; this mode optimizes the power consumption of the induced draft fan by reducing the gas phase pressure drop and ensures that the two towers achieve load peaking under a balanced liquid-gas ratio, which is suitable for the high load operation of the boiler;

[0107] Form 3: Dual-tower series operation mode. When low flue gas volume or deep condensation demand is detected, the intelligent control module 23 drives the flue gas proportioning valve 101 to guide the flow to tower A, and the series-parallel switching valve 103 blocks the direct discharge channel, guiding the flue gas from the outlet of tower A to the inlet of tower B, so that the flue gas flows through towers A and B in sequence to form a two-stage series flow field; at the same time, the liquid distribution valve 102 is driven to adjust the distribution of spray liquid, so that the flue gas exchanges heat with the circulating working fluid in tower A to complete sensible heat recovery, and contacts the low-temperature working fluid returning from the heat pump end in tower B to complete latent heat deep extraction, and drives the liquid confluence valve 104 to fully open; this mode uses the operating temperature difference between the two towers to build a gradient heat exchange path, which greatly improves the recovery ratio of the total heat of the flue gas, and realizes deep cooling of the flue gas and maximizes the utilization of waste heat.

[0108] S7: The purified circulating working fluid is pressurized by the circulating pump 17 and sent to the three-way regulating valve 105. The intelligent control module 23 dynamically allocates the flow rate according to the heat pump operating characteristics and user heat load. Part of the circulating working fluid enters the heat source side of the evaporator 18 as a low-grade heat source to drive the low-pressure refrigerant in the evaporator 18 to absorb heat and evaporate, releasing heat and cooling down. The other part is directly output through the bypass pipeline. The low-temperature working fluid after heat release is mixed and temperature-adjusted with the heat working fluid of the bypass branch at the junction point and then sent to the atomizing nozzle assembly 16 for recycling.

[0109] S8: The low-pressure refrigerant vapor generated by the evaporator 18 of the absorption heat pump 22 enters the absorber 19, is absorbed by the concentrated absorbent solution, and the released absorption heat preheats the return water on the user side.

[0110] S9: The dilute absorbent solution after absorption enters the generator 20. After being heated by the saturated steam of the external driving heat source, high-pressure refrigerant vapor is separated. The vapor enters the condenser 21 and releases condensation heat to reheat the preheated user-side return water.

[0111] S10: The return water from the user side flows sequentially through the hot water side of the absorber 19 and the hot water side of the condenser 21. The water temperature is continuously increased through the stepwise absorption of heat at different energy levels. Finally, after reaching the preset heating temperature, it is sent to the user side water supply network. It can be used for various scenarios such as heating in the factory area, preheating of process water, or low-temperature drying.

[0112] Example 2:

[0113] The difference between this embodiment and Embodiment 1 is that:

[0114] The outer wall of the upper tower body 2 is provided with a plurality of axially arranged upper outer protrusions evenly distributed along its circumference, and the outer wall of the lower tower body 3 is provided with a plurality of lower outer protrusions evenly distributed along its circumference and arranged along the generatrix direction of the conical surface. The upper outer protrusions and the lower outer protrusions are connected in a one-to-one correspondence.

[0115] When dust-laden flue gas and circulating working fluid form a swirling flow field within the tower, the airflow and droplets rotate and rise along the circumference of the tower. As they flow through the axial micro-grooves on the inner wall, the local wall curvature and tangential velocity distribution change, causing the near-wall fluid to generate axially developing micro-vortices and ribbon-like secondary flows, disrupting the stability of the near-wall layer. These axial micro-vortices enhance the volatility and renewal frequency of the near-wall liquid film, strengthening heat and mass transfer near the tower wall. Furthermore, the low-velocity bands formed within the micro-grooves facilitate the capture of circulating working fluid and dust-laden particles thrown towards the wall by centrifugal force, extending their residence time within the grooves and allowing for multiple collisions and aggregations with subsequent droplets, increasing the size of the falling droplets.

[0116] Compared with a smooth cylindrical structure, this embodiment effectively enhances the near-wall micro-vortex through a simple axially outward groove structure, which is beneficial to improving the aggregation efficiency of the circulating working fluid and fine particles and the heat and mass transfer coefficient near the tower wall.

[0117] Example 3:

[0118] The difference between this embodiment and Embodiment 1 is that:

[0119] The upper tower body 2 is a prism-shaped structure, preferably a heptagonal prism, and the lower tower body 3 is a pyramid-shaped structure, preferably a heptagonal pyramid.

[0120] When dust-laden flue gas and circulating working fluid form a main swirling flow within the tower, local pressure gradient changes and shear inhomogeneities near the edges induce localized separation and backflow of the near-wall fluid, creating multiple micro-vortex regions around the tower wall. On one hand, the micro-vortex structure enhances the exchange of mass and momentum between the near-wall liquid film and the main flow, increasing the heat and mass transfer coefficients near the tower wall. On the other hand, radial velocity disturbances near the corner regions facilitate the more frequent throwing of particles and fine circulating working fluid droplets towards the tower wall, causing them to collide with the liquid film and rapidly coalesce.

[0121] Compared with the cylindrical structure, this embodiment further enhances the circulating working fluid and particle aggregation effect and heat and mass transfer capacity in the near-wall region without significantly increasing the pressure drop.

[0122] Example 4:

[0123] The difference between this embodiment and Embodiment 1 is that:

[0124] The walls of both the upper tower body 2 and the lower tower body 3 have a continuous spiral corrugated structure with equal elliptic angles. The direction of the spiral corrugation is completely consistent with the direction of the main swirling flow formed by the tangential intake of flue gas, and extends continuously spirally from bottom to top along the axial direction of the tower body. The crests and troughs of the corrugations are evenly distributed alternately along the axial direction of the tower body, forming a continuous spiral guide channel on the inner wall of the tower body. The flow cross section of the spiral guide channel is distributed in a periodic pattern of contraction-expansion-recontraction along the spiral extension direction of the channel, where the trough is the channel contraction section and the transition area between adjacent crests is the channel expansion section.

[0125] When the main swirling flow and the spiral microgrooves on the inner wall superimpose, a three-dimensional microvortex structure with composite rotational characteristics is formed in the near-wall region. On the one hand, the spiral channels guide the near-wall fluid to move in a coupled axial and circumferential direction, generating secondary swirling flows that develop along the channels. On the other hand, the alternating contraction and expansion of the flow channel cross-section caused by the spiral ripples cause periodic acceleration and deceleration of the local flow, inducing liquid film fluctuations and droplet redistribution. This structure not only enhances the mixing and energy exchange between the near-wall liquid film and the main flow, improving heat and mass transfer efficiency, but also facilitates the entrainment of droplets and fine particles thrown towards the wall into the spiral channels, where they undergo longer residence time and more collisions and coalescence, ultimately forming larger droplets that fall back into the integrated primary sedimentation collection tank. Compared with prismatic structures and axially convex groove structures, this embodiment constructs a stronger three-dimensional microvortex field, resulting in more continuous and uniform disturbance to the gas-liquid two-phase system. While ensuring a moderate pressure drop, it further enhances droplet coalescence and heat transfer effects.

[0126] It will be apparent to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the invention can be implemented in other forms without departing from its spirit or essential characteristics. Therefore, the embodiments should be considered in all respects as exemplary and non-limiting, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of the equivalents of the claims are intended to be included within the present invention. No reference numerals in the claims should be construed as limiting the scope of the claims.

[0127] Furthermore, it should be understood that although this specification describes embodiments, not every embodiment contains only one independent technical solution. This narrative style is merely for clarity. Those skilled in the art should consider the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery, characterized in that: The system includes a flue gas inlet pipe (1), an upper tower body (2), a lower tower body (3), an underflow pipe (4), a solution outlet pipe (5), an integrated primary sedimentation collection tank (6), an intelligent drain valve (7), a drain outlet (8), a settling baffle (9), a water quality analyzer (10), a reinforced coalescence cone (11), a flue gas outlet pipe (14), an overflow pipe (15), and an atomizing nozzle assembly (16). The upper tower body (2) and the lower tower body (3) are vertically connected and fixed. The upper tower body (2) has a cylindrical structure, and the lower tower body (3) has a single cone structure. The upper end of the side wall of the upper tower body (2) is connected to at least one tangentially arranged flue gas inlet pipe (1). An atomizing nozzle assembly (16) is installed inside the flue gas inlet pipe (1). The spray direction of all nozzles in the atomizing nozzle assembly (16) points to the inside of the upper tower body (2). An overflow pipe is connected to the upper end of the upper tower body (2). 15), the side wall of the overflow pipe (15) is connected to the flue gas outlet pipe (14), and the interior of the upper tower body (2) is equipped with a multi-stage spaced reinforced agglomeration cone (11) along the height direction. The lower end of the lower tower body (3) is connected to the integrated primary sedimentation collection tank (6) through the underflow pipe (4). The integrated primary sedimentation collection tank (6) is equipped with multiple sets of sedimentation baffles (9). The bottom of the integrated primary sedimentation collection tank (6) is a conical structure that shrinks towards the center and the end is equipped with a drain pipe (8). The drain pipe (8) is connected to the intelligent drain valve (7). The solution outlet pipe (5) is located in the upper part of the side wall of the integrated primary sedimentation collection tank (6). The side wall of the integrated primary sedimentation collection tank (6) is also sealed and fixed with a water quality detector (10). The sensing probe of the water quality detector (10) extends into the supernatant area above the sedimentation baffle (9).

2. The swirl heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 1, characterized in that: The upper tower body (2) is a cylindrical structure, and the lower tower body (3) is a conical structure.

3. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 2, characterized in that: The outer wall of the upper tower body (2) is provided with multiple upper outer protrusions, and the outer wall of the lower tower body (3) is provided with multiple lower outer protrusions. The upper outer protrusions and the lower outer protrusions are connected in a one-to-one correspondence.

4. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 1, characterized in that: The upper tower body (2) is a prism-shaped structure, and the lower tower body (3) is a pyramid-shaped structure.

5. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 2, characterized in that: The walls of the upper tower body (2) and the lower tower body (3) are both of a continuous spiral corrugated structure. The spiral corrugated structure is consistent with the main swirling direction formed by the tangential intake of flue gas and extends continuously from bottom to top along the axial direction of the tower body. The crests and troughs of the corrugations are evenly distributed alternately along the axial direction of the tower body, forming a continuous spiral guide channel on the inner wall of the tower body. The flow cross section of the spiral guide channel is distributed in a periodic contraction-expansion-recontraction pattern along the spiral extension direction of the channel.

6. A swirl heat exchanger and coalescing sprayer for flue gas waste heat recovery according to claim 2, 3, 4, or 5, characterized in that: The settling baffle (9) is one or more of the following: a zigzag plate, a multi-stage sawtooth plate, or a honeycomb zigzag plate.

7. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 6, characterized in that: The overflow pipe (15) is equipped with a demisting element.

8. A cyclone heat exchanger and agglomeration sprayer for flue gas waste heat recovery according to claim 7, characterized in that: The enhanced coalescence cone disk (11) is either an annular cone disk or a baffle cone disk, and has two forms, as detailed below: Format 1: Multiple reinforced coalescing cones (11) are arranged at intervals along the height of the tower body, and their radial dimensions decrease from top to bottom; a vertically penetrating flow channel is formed between two adjacent reinforced coalescing cones (11), and the flow channel is gradually narrowed from top to bottom; Form Two: Multiple reinforced coalescing cones (11) have the same radial dimension. Each reinforced coalescing cone (11) has a main channel at its edge. The main channels of every two adjacent reinforced coalescing cones (11) are alternately staggered.

9. A heat pump system comprising a cyclone heat exchanger and polymer sprayer for flue gas waste heat recovery as described in any one of claims 1-8, characterized in that: The system includes a circulating pump (17), an absorption heat pump (22), an intelligent control module (23), a three-way regulating valve (105), a three-way switching valve group, and at least two sets of parallel swirl heat exchanger sprayers; the three-way switching valve group includes a flue gas proportioning valve (101), a liquid distribution valve (102), a series-parallel switching valve (103), and a liquid junction valve (104), all equipped with switching actuators to achieve automatic switching between single-tower operation, dual-tower parallel operation, and dual-tower series operation modes; the absorption heat pump ( 22) Includes an evaporator (18), an absorber (19), a generator (20), and a condenser (21). The generator (20) is equipped with a heating coil connected to an external driving heat source unit. The solution outlet pipe (5) of the swirl heat exchange agglomeration sprayer is connected to the inlet of the circulating pump (17), and the outlet of the circulating pump (17) is connected to the inlet of the three-way regulating valve (105). The first outlet of the three-way regulating valve (105) is connected to the heat source side inlet of the evaporator (18), and the second outlet is directly connected to the inlet of the atomizing nozzle assembly (16) via a bypass pipe. The intelligent control module (23) integrates an operating parameter sensing unit, configured to obtain real-time status signals of the flue gas side and the working fluid side through data interaction with the external control system and the water quality detector (10). The operating parameter sensing unit obtains dynamic back pressure and flow rate by monitoring the current and frequency of the circulating pump (17) and combining the preset flow resistance curve analysis, thereby realizing soft measurement of the operating condition. The intelligent control module (23) is used to calculate the heat exchange efficiency ratio and dynamically... The opening degree of the three-way regulating valve (105) is adjusted to optimize the distribution ratio of the circulating working fluid between the heat source side of the evaporator (18) and the bypass pipeline; the heat source side outlet of the evaporator (18) is connected to the atomizing nozzle assembly (16) after merging with the bypass pipeline, the user side return water pipe is connected to the hot water side inlet of the absorber (19), the hot water side outlet of the absorber (19) is connected to the hot water side inlet of the condenser (21), and the hot water side outlet of the condenser (21) is connected to the user side water supply network to construct a heat cascade boosting path.

10. A method for operating a heat pump system including a swirl heat exchanger and polymer sprayer for flue gas waste heat recovery according to claim 9, characterized in that: The method includes the following steps: S1: The flue gas purified upstream is introduced tangentially into the upper tower (2) of the swirl heat exchanger agglomeration sprayer through the flue gas inlet pipe (1) to construct a circumferential high-speed swirling field; S2: The circulating working fluid is transported to the atomizing nozzle assembly (16), and after being atomized into fine droplets by the nozzle, it enters the upper tower body (2) tangentially along with the flue gas; S3: Under the synergistic effect of the swirling centrifugal field and the multi-stage enhanced coalescence cone disk (11), the microdroplets migrate towards the tower wall and are wetted and captured, forming a dynamically renewed continuous liquid film; as the flux increases, the liquid film converges and becomes unstable and breaks down, coalescing into large-scale droplets, overcoming the airflow drag and falling back to the integrated primary sedimentation collection tank (6) at the bottom, and using the multi-stage laminar flow unit composed of internal sedimentation baffles (9) to achieve in-situ sedimentation and purification self-balance of solid and liquid impurities; S4: The flue gas after initial separation continues to rise to the overflow pipe (15) to capture the remaining microdroplets; the liquid phase formed by the capture is driven by gravity to fall back to the integrated primary sedimentation collection tank (6), and the flue gas after deep cooling, dehumidification and purification is discharged from the flue gas outlet pipe (14). S5: The circulating working fluid collected in the integrated primary sedimentation collection tank (6) is monitored in real time by the water quality tester (10) for its pH value and conductivity, and fed back to the intelligent control module (23); when the pH value or conductivity exceeds the preset threshold, the intelligent control module (23) opens the intelligent drain valve (7) to perform reduced-volume directional sewage discharge; S6: The intelligent control module (23) uses the real-time flue gas flow, system back pressure and user-side heat load demand obtained by the operation parameter sensing unit to drive the three-way switching valve group to perform dynamic switching of the operation mode. S7: The purified circulating working fluid is pressurized by the circulating pump (17) and sent to the three-way regulating valve (105). The intelligent control module (23) dynamically allocates the flow rate according to the operating characteristics of the heat pump. A portion of the circulating working fluid enters the heat source side of the evaporator (18) and drives the low-pressure refrigerant in the evaporator (18) to absorb heat and evaporate, releasing heat and cooling down. Another portion is directly output through the bypass pipeline. The low-temperature working fluid after heat release is mixed and temperature-adjusted with the heat working fluid of the bypass branch at the junction point and then sent to the atomizing nozzle assembly (16) for recycling. S8: The low-pressure refrigerant vapor generated by the evaporator (18) of the absorption heat pump (22) enters the absorber (19), is absorbed by the concentrated solution, and the released heat preheats the return water on the user side. S9: The absorbed dilute solution enters the generator (20), and after being heated by an external driving heat source, it separates into high-pressure refrigerant vapor. The vapor enters the condenser (21) and releases condensation heat to reheat the preheated user-side return water. S10: The user-side return water flows sequentially through the hot water side of the absorber (19) and the hot water side of the condenser (21). Through the stepwise absorption of heat at different energy levels, the water temperature is continuously increased, and finally, after reaching the preset heating temperature, it is sent to the user-side water supply network.

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