An indoor air purification process based on nanometer micro-fog ionization

Abstract

The application discloses an indoor air purification process based on nanometer micro-mist ionization, and relates to the technical field of air purification.The water replenishing stock solution in a liquid storage humidifier is combined with recovered condensate in a mist area, the combined liquid phase system is subjected to electric property correction, degassing treatment and ion strength leveling treatment, and precursor water is obtained; the precursor water is sent to an atomization section to form a mother drop group, and is subjected to isohydric maturation in a closed wet field to obtain matured mother drop groups; the matured mother drop groups are sequentially introduced into a pre-polarization area and a main cracking area to form nanometer-sized negatively charged water-containing particles; the particles are then released into an indoor space after hydration stabilization in a wet field enrichment area, fractional separation, fractional backflow, rectification and dew point reduction treatment. The process can improve the stability and cracking consistency of the precursor water, reduce the entrainment of large droplets and the mixing of insufficiently charged particles, reduce the near-field wet load and output fluctuation, and improve the coagulation and sedimentation effect of indoor suspended pollutants.

Description

Technical Field

[0001] This invention relates to the field of air purification technology, specifically to an indoor air purification process based on nano-micro-mist ionization. Background Technology

[0002] With the development of consumer humidifiers, humidifiers are not only used to regulate indoor humidity, but some solutions also attempt to use charged water-containing microparticles to improve indoor air quality. If this technology is used for continuous operation in the near field near the bedside in the bedroom, it must not only be able to continuously produce mist, but also allow the output microparticles to actually enter the air layer of the human breathing zone and take effect on suspended pollutants in the air.

[0003] At present, existing technologies still have some practical problems in this scenario. After the equipment runs continuously, the replenishment liquid and the condensate recovered in the mist output zone will coexist. If there is no special treatment, it can easily cause subsequent mist output fluctuations. If the droplet size and charge state are not properly controlled, excessively large droplets and undercharged particles can be released together, which will not only weaken the effect on suspended pollutants, but also easily form wet accumulation and surface condensation in the near field of the bed.

[0004] Existing solutions are often insufficient in separating and recovering unqualified droplets and particles, resulting in a large amount of ineffective output and poor stability in continuous operation. At the same time, some solutions lack further adjustment of the output flow moisture load before misting, making the output flow prone to excessive moisture in the near field at the bedside, making it difficult to simultaneously take into account the purification effect of pollutants in the human breathing zone air layer and the near field use suitability. Summary of the Invention

[0005] To address the shortcomings of existing technologies, the technical solution of this invention is as follows: An indoor air purification process based on nano-mist ionization includes: The replenishing solution in the storage humidifier is combined with the condensate recovered from the mist outlet zone. The combined liquid phase system is then subjected to electrical correction, degassing, and ion strength balancing to obtain precursor water with an electrical conductivity of 50–200 μS / cm. The precursor water is fed into the atomization section for atomization to form a group of mother droplets. The mother droplets are then placed in a closed wet field for isohumid ripening to obtain a ripened mother droplet group with a median particle size D50 of 1 to 8 μm. The ripened mother droplets are then sequentially introduced into the prepolarization zone and the main pyrolysis zone to form a directional charge layer on the surface of the ripened mother droplets and pyrolyze them to form nanoscale negatively charged water-containing particles. Negatively charged water-containing microparticles are introduced into a humid and weak field region for hydration stabilization to obtain a hydrated and stable microparticle stream. The hydrated and stable microparticle stream is then separated to obtain a qualified microparticle stream and an unqualified microparticle stream. The unqualified microparticle stream includes large droplet components and undercharged electron water microparticle components. The large droplet components and undercharged electron water microparticle components are then returned to the atomization section and the main pyrolysis zone for further processing of the unqualified microparticle stream. The qualified particulate stream is rectified and dew point reduced to obtain a purified output stream. The purified output stream is then released into the indoor space, allowing it to come into contact with indoor suspended pollutants and promote their coagulation and settling, thus completing the indoor air purification.

[0006] Furthermore, the replenishing solution in the storage-type humidifier merges with the condensate recovered in the mist outlet zone, including: The condensate recovered from the mist outlet area is introduced into the settling buffer zone for static settling to obtain pre-purified recovered condensate; The pre-purified recovered condensate and the makeup water stock solution are then introduced into a mixing buffer for cyclic mixing. The volume ratio of the pre-purified recovered condensate to the makeup water stock solution is 1:4 to 1:8, resulting in the precursor water to be corrected.

[0007] Furthermore, the precursor water to be corrected is subjected to electrical correction treatment; The electrical correction process involves introducing the water, the precursor to be corrected, into the conductivity correction zone of the storage humidifier. Then, add conductivity correction liquid to the conductivity correction zone and circulate and mix the precursor water to be corrected with the conductivity correction liquid until the conductivity of the circulated and mixed liquid phase reaches 50-200 μS / cm, thus obtaining the precursor water to be degassed. The conductivity correction solution has a conductivity of 90–150 μS / cm. By volume, the precursor water is 100 parts and the conductivity correction solution is 3–10 parts.

[0008] Furthermore, the water in the precursor to be degassed is subjected to degassing treatment and ion strength leveling treatment. The degassing treatment involves spreading the water, the precursor to be degassed, along the liquid surface to form a thin liquid layer with a thickness of 0.4–0.9 mm. The thin liquid layer is then introduced into the depressurization and gas separation zone to release the free dissolved gas in the precursor water to be degassed, thus obtaining the degassed precursor water; Ion strength leveling is achieved by reciprocating the degassed precursor water along a closed-loop mixing path. The degassed precursor water, after reciprocating flow, is then introduced into a closed homogenization zone and allowed to stand for 20–45 seconds to make the ion concentration distribution in different micro-regions of the degassed precursor water tend to be uniform, thus forming precursor water.

[0009] Furthermore, the mother droplet group is placed in a closed, humid environment for isothermal maturation, including: Humidifying gas is continuously supplied to the enclosed humidification field, and the relative humidity inside the enclosed humidification field is maintained at 96% to 99%. This allows the mother droplet group to exchange water vapor with the humidified gas within a closed, humid environment. It causes droplets with a diameter of less than 1 μm to absorb moisture and grow, and causes droplets with a diameter of more than 8 μm to settle and detach from the parent droplet group; The droplets with a particle size of 1–8 μm were retained in the mother droplet group to obtain a mature mother droplet group with a median particle size D50 of 1–8 μm.

[0010] Furthermore, the matured mother droplet group is sequentially introduced into the pre-polarization region and the main pyrolysis region, causing a directional charge layer to form on the surface of the matured mother droplet group, which then pyrolyzes to form nanoscale negatively charged water-containing particles; wherein: The aging mother droplet group is introduced into the prepolarization region through the outlet channel, so that the aging mother droplet group passes through the prepolarization micro gap. Under the action of unipolar bias with an applied working voltage of 12-48V, the negative charge on the outer surface of the aging mother droplet group migrates and accumulates along the outer surface of the droplet towards the outlet side, forming a surface oriented charge layer. The matured mother droplets with surface oriented charge layers are then introduced into the main pyrolysis region through a connecting channel. The matured mother droplets with surface oriented charge layers pass through the main pyrolysis micro-gap and undergo ionization pyrolysis from the side where the surface oriented charge layer is located under the action of pulse loading with an applied working voltage of 80-220V, forming nanoscale negatively charged water-containing microparticles. The gap width of the main pyrolysis microgap is 0.05–0.30 mm.

[0011] Furthermore, the negatively charged nanoparticles containing water are introduced into the humid and weak field region, so that the relative humidity of the humid and weak field region is maintained at 92% to 98%, and the negatively charged nanoparticles containing water are in contact with the humidifying gas in the humid and weak field region, so that the negatively charged nanoparticles adsorb water molecules on their outer surface and complete the redistribution of surface charge, forming a hydrated and stable particle flow. The hydrated stable microparticle stream is then introduced into the graded separation zone, where it first changes direction through a deflection section. The inertial difference is used to cause the large droplets that are not completely broken up to break away from the mainstream and form large droplet components. Then, the mainstream after the deflection and separation section is made to enter the deflection and separation section. Under the action of the lateral bias electric field, the undercharged water-containing particles deviate from the mainstream and form a component of undercharged electron water particles. The particles that maintain the mainstream output after the deflection separation section form a qualified particle stream, while the large droplet component and the undercharged electron water particle component constitute an unqualified particle stream.

[0012] Furthermore, the large droplet components are introduced into the return liquid collection area, where they are gathered to form a reflux liquid phase. The reflux liquid phase is then introduced into the inlet liquid merging section before the atomization section through the liquid phase reflux channel, where it merges with the precursor water to form a re-atomized material stream. The undercharged water-containing microparticles are introduced into the microparticle reflux channel, and the electron-deficient water microparticles are introduced into the re-pyrolysis introduction section before the main pyrolysis zone through the microparticle reflux channel, where they merge with the mature mother droplets with surface oriented charge layers to form a re-pyrolysis stream. The re-atomized stream is then allowed to enter the atomization section for further atomization, while the re-pyrolysis stream is allowed to enter the main pyrolysis zone for further ionization and pyrolysis. The liquid phase reflux channel and the particle reflux channel are isolated from each other.

[0013] Furthermore, the qualified microparticle stream is guided into the rectifying channel for co-current flow, forming an axial microparticle stream; The axial particulate stream is then brought into parallel contact with the humidifying airflow, wherein the absolute moisture content of the humidifying airflow is lower than that of the axial particulate stream. This causes the axial particulate stream to release water vapor and lowers its dew point by 1.5–4.0°C, forming a purified output stream. The purified output stream is then released into the indoor space through the mist outlet.

[0014] The beneficial effects of this invention are as follows: 1. By performing electrical correction, degassing treatment, and ion strength balancing treatment on the liquid phase system formed by the replenishment water and the recovered condensate in the mist outlet zone, and controlling the liquid phase conductivity within the range of 50–200 μS / cm, the conductive state, dissolved gas state, and ion distribution state of the precursor water can be made more stable. This can reduce fluctuations in the subsequent atomization process, reduce the dispersion of mother droplet size and local instability, and provide a more stable liquid phase basis for subsequent maturation and pyrolysis.

[0015] 2. By placing the mother droplet group in a closed wet field for isohumid ripening, the volume median particle size D50 is stabilized at 1-8 μm. Then, it is processed sequentially through the prepolarization zone and the main pyrolysis zone. This allows a directional charge layer to be formed on the surface of the ripened mother droplet group. Ionization pyrolysis is then carried out along the side where the directional charge layer is located, making it easier to form nanoscale negatively charged water-containing microparticles. This can improve the directionality and sufficiency of pyrolysis, reduce the residue of large droplets and the mixing of undercharged microparticles, and facilitate the formation of a more stable and qualified microparticle stream in the future.

[0016] 3. By combining precursor water stabilization treatment with directional pyrolysis treatment, a continuous control relationship is formed between the front-end liquid phase state, the mother droplet boundary before pyrolysis, and the surface charge distribution during pyrolysis. On this basis, combined with hydration stabilization in the wet and weak field area, staged separation, branched reflux, rectification, and dew point reduction treatment, the final purified output stream can not only have a good coagulation and sedimentation effect of suspended pollutants, but also reduce large droplet entrainment, near-field wet load, and output fluctuations, making it more suitable for stable use under continuous indoor operation conditions. Attached Figure Description

[0017] Figure 1 This is a flowchart of the process steps of the present invention; Figure 2 This is a diagram illustrating the closed-loop recovery and output humidity control of the present invention. Figure 3 This is a schematic diagram of the microscopic mechanism of action of the present invention; Figure 4 This is a microscopic schematic diagram of the maturation mother droplet of the present invention. Detailed Implementation

[0018] 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 skilled in the art without creative effort are within the scope of protection of the present invention.

[0019] Example 1 Please see Figure 1 , Figure 2 , Figure 3 and Figure 4 This invention provides an indoor air purification process based on nano-micro-mist ionization, comprising: The replenishing solution in the storage humidifier is combined with the condensate recovered from the mist outlet zone. The combined liquid phase system is then subjected to electrical correction, degassing, and ion strength balancing to obtain precursor water with an electrical conductivity of 50–200 μS / cm. The precursor water is fed into the atomization section for atomization to form a group of mother droplets. The mother droplets are then placed in a closed wet field for isohumid ripening to obtain a ripened mother droplet group with a median particle size D50 of 1 to 8 μm. The ripened mother droplets are then sequentially introduced into the prepolarization zone and the main pyrolysis zone to form a directional charge layer on the surface of the ripened mother droplets and pyrolyze them to form nanoscale negatively charged water-containing particles. Negatively charged water-containing microparticles are introduced into a humid and weak field region for hydration stabilization to obtain a hydrated and stable microparticle stream. The hydrated and stable microparticle stream is then separated to obtain a qualified microparticle stream and an unqualified microparticle stream. The unqualified microparticle stream includes large droplet components and undercharged electron water microparticle components. The large droplet components and undercharged electron water microparticle components are then returned to the atomization section and the main pyrolysis zone for further processing of the unqualified microparticle stream. The qualified particulate stream is rectified and dew point reduced to obtain a purified output stream. The purified output stream is then released into the indoor space, allowing it to come into contact with indoor suspended pollutants and promote their coagulation and settling, thus completing the indoor air purification.

[0020] In this embodiment, a household liquid-storage humidifier with a rated liquid storage capacity of 2.5L was selected as the carrier, and continuous operation verification was conducted in a simulated bedroom environment. The volume of the test room was set to 18m². 3The bed is positioned against the wall, with the humidifier placed on the bedside table. The center of the humidifier's mist outlet is 0.42m above the pillow surface and 0.18m from the inner surface of the headboard, with the mist directed towards the air layer above the headboard where the human body breathes. The sampling location for the air layer in the human body's breathing zone is set as follows: 0.20m above the pillow surface, 0.10m from the longitudinal centerline of the bed, and 0.35m from the axis of the mist outlet.

[0021] Before the experiment, the indoor temperature was controlled at 24.0±0.5℃, the background relative humidity at 48%±3%, and the background wind speed below 0.08m / s. The target pollutant was a compound aerosol of indoor inhalable suspended pollutants, and the initial PM2.5 concentration in the breathing zone was controlled at 135–145 μg / m³. 3 The initial PM1.0 concentration was 88–96 μg / m³. 3 To simulate human respiratory exposure conditions in a near-field low-disturbance environment in a bedroom at night.

[0022] In this embodiment, 1350 mL of replenishing water stock solution is first added to the storage chamber of the storage humidifier, and then 250 mL of recovered condensate from the mist outlet condensation recovery channel is guided back to the storage chamber, so that the replenishing water stock solution and the recovered condensate from the mist outlet zone form a dual-source liquid phase system in the same storage system; after the dual-source liquid phase system is left to stand for 120 seconds, it is sent to the liquid phase adjustment unit through the bottom circulation liquid path.

[0023] During adjustment, an electrical correction solution was first added to adjust the conductivity of the liquid system from 68 μS / cm to 116 μS / cm. Then, the liquid system was spread along the liquid surface into a thin liquid layer with a thickness of about 0.55 mm, and degassed for 45 s under -0.052 MPa conditions to reduce the content of dissolved gas and microbubbles. After degassed, the liquid system was circulated back and forth along a closed loop for 160 s, and then allowed to stand in a closed homogenization chamber for 28 s to make the ion concentration distribution of different micro-regions in the dual-source liquid system tend to be uniform, thus obtaining precursor water.

[0024] The reason for adopting the above-mentioned dual-source liquid phase system and performing electrical correction, degassing treatment and ion strength balancing treatment is that when a civilian storage-type humidifier is running continuously in the near field at the bedside, the coexistence of the replenishment water source solution and the recovered condensate is an unavoidable actual working condition. If the dual-source liquid phase system is not uniformly adjusted, the precursor water is prone to conductivity drift, microbubble entrainment and local ion concentration fluctuations during continuous operation, which in turn leads to fluctuations in the mist particle size, near-field large droplet entrainment and insufficient stability of the breathing zone exposure.

[0025] After obtaining the precursor water, the precursor water is fed into the atomization section at a feed rate of 0.24 mL / min, where it forms a group of mother droplets under the action of the atomization components.

[0026] The formed mother droplet swarm is not directly output, but first enters a closed wet field for isohumidification. The relative humidity of the closed wet field is controlled at 97%, the airflow velocity is controlled at 0.16 m / s, and the residence time of the mother droplet swarm in the closed wet field is 1.5 s. After isohumidification, droplets with too small a particle size absorb moisture and grow, while droplets with too large a particle size are separated from the mainstream in the wet field due to inertia and gravity, and finally a mature mother droplet swarm with a median volumetric particle size D50 of 4.1 μm is obtained.

[0027] Verification has shown that the stability of the mother droplet boundary before pyrolysis is particularly critical for near-field applications at the bedside. If the particle size distribution of the mother droplet group is too wide, the main pyrolysis zone is prone to simultaneously outputting unstable large droplets and undercharged particles. The former will form visible wet condensation and boundary condensation in the near-field of the mist outlet, while the latter will cause fluctuations in the pollutant capture effect in the breathing zone, failing to form a stable purification effect.

[0028] The matured mother droplets continue to enter the prepolarization region and the main cleavage region. The prepolarization region uses a 24V unipolar bias to form a directional charge layer on the surface of the matured mother droplets. Subsequently, the matured mother droplets with the directional charge layer enter the main cleavage region and undergo directional cleavage under the action of a 160V pulse voltage to form nanoscale negatively charged water-containing particles.

[0029] A humidity-rich, low-field zone is set behind the main pyrolysis zone. The relative humidity in the humidity-rich, low-field zone is controlled at 95%, and the field strength is controlled at 0.18 kV / cm. This allows the newly generated negatively charged water-containing particles to complete surface hydration and charge redistribution under high humidity and low field strength conditions, resulting in a hydrated, stable particle stream.

[0030] The hydrated, stable microparticle stream then passes sequentially through a deflection and separation section. The deflection section removes incompletely fragmented large droplet components, while the separation section separates undercharged microparticle components. The large droplet components are refluxed back to the front of the atomization section via a liquid-phase reflux channel, while the undercharged microparticle components are refluxed back to the front of the main pyrolysis zone via a microparticle reflux channel. This prevents unstable large droplets and undercharged microparticles from directly entering the near-field misting area at the head of the bed. The separated, qualified microparticle stream enters the rectifying channel and comes into parallel contact with the low-humidity conditioning airflow, lowering the output dew point by 2.4°C. Finally, the purified output stream is released into the near-field misting area at the head of the bed.

[0031] The purpose of this process is, on the one hand, to maintain continuous contact with and condensation and sedimentation of suspended pollutants in the human breathing zone, and on the other hand, to significantly suppress near-field visible wet condensation and boundary condensation of fog, thus meeting the requirements for comfort and safety in continuous bedside operation scenarios.

[0032] This embodiment was run continuously for 8 hours, and the changes in suspended pollutants in the air layer of the human breathing zone, near-field visible condensation level, condensation on the inner boundary surface of the headboard, output fluctuation rate, and breathing zone exposure stability were detected at 30 minutes, 2 hours, and 8 hours of operation.

[0033] The test results show that, under the combined effects of dual-source liquid phase system pretreatment, pre-pyrolysis mother droplet boundary stabilization control, unqualified particulate stream diversion and reflux, and purification output stream dew point reduction treatment, the concentrations of PM2.5 and PM1.0 in the breathing zone air layer decreased significantly during continuous operation in the near field of the bed head. Furthermore, no continuous white fog agglomeration occurred in the near field of the fog outlet, and no obvious condensation or dew appeared on the bed headboard surface. The purification output stream maintained small fluctuations throughout the entire nighttime operation cycle, and was able to act relatively stably on suspended pollutants in the human breathing zone air layer.

[0034] Table 1: Performance Comparison Results of Different Process Schemes in Near-Field Continuous Operation Scenarios at the Bedside Parameter name Example 1.1 - Precursor water conductivity 116 μS per cm Comparative Example 1 - Precursor water conductivity 38 μS per cm Comparative Example 2 - Precursor water conductivity 67 μS per cm Comparative Example 3 - Precursor water conductivity 178 μS per cm Comparative Example 4 - Precursor water conductivity 236 μS per cm Precursor water conductivity (μS / cm) 116 38 67 178 236 Matured mother droplet group D50 (μm) 4.2 6.8 4.9 4.6 7.2 Outputs negatively charged water-containing particles D50 (nm) 185 452 243 228 418 Percentage of qualified microparticle streams (%) 88.6 48.7 79.4 76.8 51.6 PM2.5 removal rate (%) in the breathing zone (30 min) 79.3 41.8 70.6 68.9 46.3 PM1.0 removal rate (%) in the breathing zone (30 min) 72.1 33.7 63.4 61.2 37.1 Condensation rate on the headboard surface (g / h) 0.6 2.6 1 1.1 2.3 Output volatility (%) after 8 hours of continuous operation 4.8 18.9 8.2 8.9 17.4 Purification efficiency per unit energy consumption (% / kWh) 66.5 31.6 58.2 55.9 35.4 It should be noted that, in order to verify the purification effect of this embodiment on suspended pollutants in the air layer of the human breathing zone under the condition of continuous near-field operation of the bedside of the civil liquid storage humidifier, as well as the control effect on near-field visible wet condensation, boundary condensation, output fluctuation and breathing zone exposure stability, the relevant parameters in Example 1.1 and each comparative example were tested according to the following method.

[0035] The conductivity of the precursor water was obtained at the sampling port of the circulating liquid path before the precursor water enters the atomization section. After the sampled liquid was allowed to stand at 25℃ for 30s, it was measured three times continuously using a conductivity meter and the average value was taken. The unit is μS / cm. The conductivity of the precursor water is used to indicate the conductivity level of the dual-source liquid phase system formed by the makeup water and the condensate recovered from the mist outlet zone after electrical correction, degassing treatment and ion strength leveling treatment.

[0036] The maturation mother droplet group D50 was obtained between the closed humidification field outlet and the prepolarization zone inlet; online detection was performed using a micro laser particle size analyzer built into the humidifier to obtain the particle size volume distribution curve and read the median particle size D50 in μm. The maturation mother droplet group D50 is used to indicate the stability of the mother droplet boundary before pyrolysis.

[0037] The negatively charged water-containing particles D50 are sampled at the inner side of the mist outlet before the purified output stream is released. They are then detected online using an aerosol particle size analyzer or an electromigration particle size analyzer to obtain the particle size distribution curve and read the volume median particle size D50 in nm. The negatively charged water-containing particles D50 are used to indicate the particle size distribution level of negatively charged water-containing particles in the purified output stream.

[0038] The percentage of qualified particulate streams is calculated by the total particulate flux at the inlet of the staged separation zone and the target particulate flux at the outlet of the qualified particulate stream. The percentage of qualified particulate streams is calculated as "qualified particulate flux ÷ total particulate flux × 100%", and the unit is %. The percentage of qualified particulate streams is used to indicate the removal effect of the staged separation zone on large droplet components and undercharged particulate components.

[0039] The removal rates of PM2.5 and PM1.0 in the breathing zone over 30 minutes were obtained at the sampling location in the human breathing zone air layer. The sampling location was set at an area 0.20m above the pillow surface, 0.10m from the longitudinal centerline of the bed, and 0.35m from the axis of the mist outlet. The initial concentration before operation was measured first, and then the concentration after 30 minutes of continuous operation was measured. The values ​​were calculated as "(initial PM2.5 concentration - PM2.5 concentration after 30 minutes) ÷ initial PM2.5 concentration × 100%" and "(initial PM1.0 concentration - PM1.0 concentration after 30 minutes) ÷ initial PM1.0 concentration × 100%", respectively, with units of 1.

[0040] The condensation on the headboard surface is measured on the inner surface of the headboard facing the mist outlet. A pre-weighed water-absorbing collection plate is laid in a fixed area. After running continuously for 1 hour, it is weighed again. The condensation per unit time is calculated based on the mass difference before and after operation, with the unit being g / h. The condensation on the headboard surface is used to indicate the degree to which the purified output flow induces condensation on the surface.

[0041] The 8-hour continuous operation output volatility was used to evaluate the stability of the purified output flow under continuous nighttime operation conditions. The test object was the concentration of target particles in the purified output flow at the mist outlet. During the 8-hour continuous operation, the concentration of target particles was recorded every 30 minutes, for a total of 16 sets of data. After calculating the mean and standard deviation of the 16 sets of data, the 8-hour continuous operation output volatility was calculated according to "standard deviation ÷ mean × 100%", with the unit being 0.5%.

[0042] Table 1 shows that the water conductivity of the precursor has a significant impact on subsequent maturation, pyrolysis, separation, and continuous operation in the near field at the head of the bed.

[0043] In Example 1.1, the precursor water conductivity was controlled at 116 μS / cm, within the range of 50–200 μS / cm, the D50 of the mature mother droplet group was 4.2 μm, the D50 of the output negatively charged water-containing particles was 185 nm, the proportion of qualified particulate streams reached 88.6%, the PM2.5 removal rate in the breathing zone reached 79.3% in 30 min, the boundary condensation on the headboard was only 0.6 g / h, and the output fluctuation rate was only 4.8% after 8 hours of continuous operation.

[0044] The above results indicate that, under this conductivity condition, precursor water can effectively balance subsequent atomization stability, pyrolysis sufficiency, and near-field continuous operation adaptability.

[0045] In Comparative Example 1, the water conductivity of the precursor decreased to 38 μS / cm, which is below the lower limit of 50 μS / cm.

[0046] At this point, the D50 of the mature mother droplet group increased to 6.8 μm, the D50 of the output negatively charged water-containing particles increased to 452 nm, the proportion of qualified particulate flow decreased to 48.7%, the PM2.5 removal rate in the breathing zone was only 41.8% after 30 minutes, and the output fluctuation rate increased to 18.9% after 8 hours of continuous operation.

[0047] This result indicates that when the conductivity of the pre-phase water is too low, the liquid phase system has insufficient charge response capability in the subsequent pyrolysis process, which can easily lead to incomplete pyrolysis, larger target particle size, a decrease in the proportion of qualified particle streams, and ultimately weaken the purification effect on suspended pollutants in the air layer of the human respiratory zone.

[0048] Meanwhile, the condensation on the headboard surface increased to 2.6 g / h, indicating that the instability of the front-end pyrolysis and the back-end output state will further amplify the near-field wet load problem.

[0049] In Comparative Examples 2 and 3, the water conductivity of the precursor was 67 μS / cm and 178 μS / cm, respectively, both within the range of 50–200 μS / cm.

[0050] The two sets of data show that as long as the conductivity of the precursor water remains within this range, the subsequent process can still maintain a good operating condition overall.

[0051] In Comparative Example 2, the output negatively charged water-containing particles had a D50 of 243 nm, the qualified particle stream accounted for 79.4%, and the PM2.5 removal rate in the breathing zone over 30 minutes was 70.6%. In Comparative Example 3, the output negatively charged water-containing particles had a D50 of 228 nm, the qualified particle stream accounted for 76.8%, and the PM2.5 removal rate in the breathing zone over 30 minutes was 68.9%. Although the effects of the two groups were slightly lower than those of Example 1.1, they were still significantly better than Comparative Examples 1 and 4, which were outside the acceptable range.

[0052] This demonstrates that controlling the water conductivity of the precursor within the range of 50–200 μS / cm ensures that the liquid phase essentially enters the effective working window for subsequent processes. Furthermore, Example 1.1, corresponding to 116 μS / cm, further indicates that there is still an even better stable range within this range.

[0053] In Comparative Example 4, the precursor water conductivity increased to 236 μS / cm, which is higher than the upper limit of 200 μS / cm. At this time, the D50 of the mature mother droplet group increased to 7.2 μm, the D50 of the output negatively charged water-containing particles increased to 418 nm, the proportion of qualified particulate stream decreased to 51.6%, the PM2.5 removal rate in the breathing zone was only 46.3% after 30 minutes, the output fluctuation rate reached 17.4% after 8 hours of continuous operation, and the boundary condensation on the headboard increased to 2.3 g / h.

[0054] The above results indicate that when the conductivity of the pre-phase water is too high, the liquid phase conduction state is too strong, and subsequent processing is more likely to result in problems such as decomposition instability, large droplet residue, and increased output fluctuations.

[0055] Although the conductivity of the liquid phase is enhanced under high conductivity conditions, it does not translate into better purification effect; instead, it reduces near-field adaptability.

[0056] As can be seen from Table 1, the electrical conductivity of the precursor water is neither better the lower it is, nor better the higher it is; rather, it needs to be controlled within the range of 50–200 μS / cm.

[0057] Below this range, the liquid phase system has insufficient charge response and incomplete pyrolysis; above this range, the liquid phase system has excessive conductivity, resulting in decreased pyrolysis and output stability.

[0058] Only by controlling the precursor water conductivity within the range of 50–200 μS / cm can we better balance the boundaries of the maturation mother droplet group, the particle size of the output negatively charged water-containing particles, the proportion of qualified particulate flow, the removal effect of suspended pollutants in the breathing zone air layer, the control of condensation on the headboard surface, and the stability of continuous operation.

[0059] This demonstrates that limiting the water conductivity of the precursor to 50–200 μS / cm has a clear technological basis and can better support the realization of the relevant technical effects of this invention.

[0060] Example 2 Please refer to Figures 1-4 Specifically: the replenishing solution in the storage-type humidifier is combined with the condensate recovered in the mist outlet zone, including: The condensate recovered from the mist outlet area is introduced into the settling buffer zone for static settling to obtain pre-purified recovered condensate; The pre-purified recovered condensate and the makeup water stock solution are then introduced into a mixing buffer for cyclic mixing. The volume ratio of the pre-purified recovered condensate to the makeup water stock solution is 1:4 to 1:8, resulting in the precursor water to be corrected.

[0061] Electrical correction treatment was performed on the precursor water to be corrected; The electrical correction process involves introducing the water, the precursor to be corrected, into the conductivity correction zone of the storage humidifier. Then, add conductivity correction liquid to the conductivity correction zone and circulate and mix the precursor water to be corrected with the conductivity correction liquid until the conductivity of the circulated and mixed liquid phase reaches 50-200 μS / cm, thus obtaining the precursor water to be degassed. The conductivity correction solution has a conductivity of 90–150 μS / cm. By volume, the precursor water is 100 parts and the conductivity correction solution is 3–10 parts.

[0062] The water used as a pre-deaerated component was deaerated and its ionic strength was adjusted. The degassing treatment involves spreading the water, the precursor to be degassed, along the liquid surface to form a thin liquid layer with a thickness of 0.4–0.9 mm. The thin liquid layer is then introduced into the depressurization and gas separation zone to release the free dissolved gas in the precursor water to be degassed, thus obtaining the degassed precursor water; Ion strength leveling is achieved by reciprocating the degassed precursor water along a closed-loop mixing path. The degassed precursor water, after reciprocating flow, is then introduced into a closed homogenization zone and allowed to stand for 20–45 seconds to make the ion concentration distribution in different micro-regions of the degassed precursor water tend to be uniform, thus forming precursor water.

[0063] In this embodiment, the same civilian liquid storage humidifier with a rated liquid storage capacity of 2.5L as in Example 1 was still selected as the test carrier, and the civilian liquid storage humidifier was placed on the bedside table in a simulated bedroom environment.

[0064] This embodiment maintains the same bedside near-field continuous operation application scenario as Embodiment 1, but the research focus of this embodiment is on the precursor water construction stage, that is, the source stabilization treatment of the dual-source liquid phase system in the civil liquid storage humidifier, in which the replenishment water and the condensate recovered in the mist output zone coexist, to verify the role of the volume fraction ratio, electrical correction, thin liquid layer degassing and ionic strength leveling treatment of this embodiment on subsequent continuous and stable operation.

[0065] In this embodiment, 300 mL of condensate from the fog exit zone is first collected from the fog exit zone condensation recovery channel and then introduced into the sedimentation buffer zone.

[0066] The effective volume of the settling buffer is 450 mL. The bottom is a low-disturbance flat-bottom structure, and the side wall is provided with a supernatant outlet for preferentially exporting the upper liquid phase after static settling.

[0067] After the condensate from the fog exit zone is left to stand in the settling buffer for 180 seconds, a small amount of sediment layer forms at the bottom and a relatively clear liquid phase forms at the top.

[0068] The turbidity of the upper liquid phase was measured to be 6.8 NTU, indicating that after the condensate from the fog exit zone was allowed to settle in the settling buffer zone, the large particulate impurities and locally aggregated droplets carried by it had been initially reduced. The resulting upper liquid phase was used as pre-purified condensate for subsequent steps.

[0069] The purpose of setting up a settling buffer zone is to prevent the recovered condensate from the fog exit zone from being directly incorporated into the makeup water in its instantaneous original state. Instead, it reduces the short-term fluctuations and entrainment content of the recovered liquid by allowing it to settle, thereby reducing the uncertainty of the dual-source liquid phase system in subsequent construction.

[0070] After obtaining the pre-purified and recovered condensate, 200 mL of the pre-purified and recovered condensate and 1000 mL of the makeup water stock solution are introduced into the mixing buffer, so that the volume ratio of the pre-purified and recovered condensate to the makeup water stock solution is 1:5.

[0071] The effective volume of the mixing buffer is 1.5L, and a low-shear circulation loop is set inside. The mixture is circulated and mixed for 240s at a circulation flow rate of 0.35L / min to obtain the precursor water to be corrected.

[0072] The initial conductivity of the precursor water to be corrected was found to be 72 μS / cm, and the conductivity deviation between different sampling points was ±11 μS / cm.

[0073] The above results show that after the pre-purified recovered condensate and the makeup water are combined at a volume ratio of 1:5, the dual-source liquid phase system can retain the following characteristics of the recovered condensate in the fog zone to the actual operating state, and will not significantly amplify the liquid phase fluctuation due to the excessively high proportion of recovered condensate in the fog zone.

[0074] Compared with the volume ratio of 1:3 in Comparative Example 1.2 and 1:9 in Comparative Example 2.2 in Table 2, the 1:5 setting is more conducive to balancing the compositional stability and operational adaptability of the dual-source liquid phase system.

[0075] When the volume fraction ratio is too low, the proportion of condensate recovered in the mist outlet zone is too high, which will amplify the local enrichment components and instantaneous disturbances in the recovered liquid; when the volume fraction ratio is too high, the proportion of condensate recovered in the mist outlet zone is too low, which will result in insufficient response of the dual-source liquid phase system to the actual continuous operating state, leading to a decrease in the recovery capacity of the precursor water in dynamic operation.

[0076] Therefore, limiting the volume ratio of pre-purified recovered condensate to makeup water to 1:4 to 1:8, preferably 1:5, is beneficial to improving the controllability of the dual-source liquid phase system and the compatibility of subsequent precursor water.

[0077] After the precursor water is formed, it is introduced into the conductivity correction zone of the storage humidifier.

[0078] The conductivity correction zone has an effective volume of 180 mL and uses a circulating drainage method to keep the precursor water to be corrected constantly renewed.

[0079] The conductivity correction zone is located between the mixing buffer and the degassing unit and is used to adjust the conductivity of the precursor water to be corrected.

[0080] The conductivity correction zone includes a correction chamber, a water guide tube for the precursor to be corrected, a conductivity correction liquid inlet, a stirrer, and a conductivity detection device.

[0081] The precursor water to be calibrated is introduced into the conductivity calibration zone through the mixing buffer and the liquid guide tube. The liquid guide tube is preferably located at the bottom of the calibration chamber so that the precursor water to be calibrated enters the calibration chamber from bottom to top, thereby reducing liquid surface disturbance.

[0082] The conductivity correction solution is stored in a separate container and added to the conductivity correction area through the inlet. The conductivity correction solution is preferably added dropwise, allowing it to gradually enter the precursor water to be corrected, thus avoiding sudden changes in local conductivity. The inlet is preferably located at the top of the correction chamber or near the stirring element to ensure rapid diffusion of the conductivity correction solution after entry.

[0083] A low-speed agitator is installed in the conductivity correction zone. The agitator is a paddle-type agitator. When the agitator rotates, it causes the liquid in the correction chamber to circulate, so that the water to be corrected and the conductivity correction liquid are uniformly mixed in the conductivity correction zone. Circulation mixing means that the liquid forms a continuous flow and repeated turbulence under the action of agitation in the conductivity correction zone, and it is not limited to being achieved through an external circulation pipeline.

[0084] A conductivity detection device is placed within the conductivity correction zone to detect the conductivity of the liquid phase after cyclic mixing. When the liquid phase conductivity enters the range of 50–200 μS / cm and remains basically stable, the conductivity correction is deemed complete, and the precursor water to be degassed is obtained. Preferably, the conductivity correction solution has a conductivity of 90–150 μS / cm, and by volume, the precursor water to be corrected is 100 parts, and the conductivity correction solution is 3–10 parts.

[0085] In Example 2.1 of the invention, the conductivity correction liquid used has a conductivity of 120 μS / cm. By volume, 100 parts of water to be corrected and 6 parts of conductivity correction liquid are added to the conductivity correction area and kept circulating and mixed for 120s.

[0086] After electrical correction, the conductivity of the liquid phase system stabilized at 118 μS / cm, yielding the water precursor to be degassed.

[0087] The purpose of electrical correction is to introduce the precursor water to be corrected into the conductivity window applicable to subsequent processes, so that the dual-source liquid system has sufficient charge response capability in subsequent atomization, ripening and pyrolysis processes, and does not cause local liquid bridges, large droplet residues or output fluctuations due to excessive conductivity.

[0088] Comparative Example 3.2 in Table 2 uses a conductivity correction solution with a conductivity of 80 μS / cm, and the amount added is reduced to 2 parts of conductivity correction solution for every 100 parts of the precursor water to be corrected, resulting in a conductivity of only 91 μS / cm for the precursor water to be degassed. The subsequent atomization output particle size fluctuation rate and the output fluctuation rate after 8 hours of continuous operation are significantly increased. Comparative Example 4.2 used a conductivity correction solution with a conductivity of 160 μS / cm, and the amount added was increased to 12 parts of conductivity correction solution for every 100 parts of the precursor water to be corrected. This resulted in the conductivity of the precursor water to be degassed increasing to 156 μS / cm, increasing the inhomogeneity of the liquid phase space, and significantly reducing the proportion of qualified microparticles in the subsequent pyrolysis.

[0089] This demonstrates that limiting the conductivity of the conductivity correction solution to 90–150 μS / cm and limiting the amount of conductivity correction solution added to 100 parts of the precursor water to be corrected to 3–10 parts, preferably 120 μS / cm and 6 parts, is more conducive to obtaining a balanced and controllable electrical correction effect.

[0090] After completing the electrical correction process, the precursor water to be degassed is degassed. In this embodiment, the precursor water to be degassed is first introduced into the spreading liquid surface.

[0091] An inclined liquid guide plate with a length of 180 mm and a width of 60 mm is used along the liquid surface. The surface roughness Ra of the liquid guide plate is controlled to be 0.8 to 1.2 μm to ensure that the water of the precursor to be degassed spreads continuously along the liquid guide plate without obvious film breakage.

[0092] After the degassed water precursor has spread along the liquid surface to form a thin liquid layer with a thickness of 0.60 mm, it immediately enters the depressurization and gas separation zone. The working pressure of the depressurization and gas separation zone is controlled at -0.055 MPa, and the residence time is controlled at 40 s, so that the free dissolved gas in the water precursor to be degassed is released, thus obtaining the degassed water precursor.

[0093] The test results showed that the residual amount of dissolved gas after degassing was 3.1 mg / L, which was significantly lower than the level when suitable thin liquid layer conditions were not used.

[0094] In Comparative Example 5.2 in Table 2, the thin liquid layer thickness was reduced to 0.25 mm, resulting in an increase in the residual dissolved gas content to 4.7 mg / L and an increase in the atomization output particle size fluctuation rate to 10.8%. In Comparative Example 6.2, the thickness of the thin liquid layer was increased to 1.10 mm, and the residual amount of dissolved gas further increased to 6.1 mg / L, while the proportion of qualified microparticles in the subsequent pyrolysis decreased to 74.8%.

[0095] The above results show that a thinner or thicker liquid layer is not necessarily better.

[0096] If the liquid layer is too thin, the continuity of the liquid film will decrease, making it prone to local film breakage and edge retraction, resulting in unstable gas-liquid contact in the depressurization and gas separation zone; if the liquid layer is too thick, it will reduce the free interface area and prolong the gas diffusion path, thus reducing the degassing efficiency.

[0097] Limiting the thickness of the thin liquid layer to 0.4–0.9 mm, preferably 0.60 mm, can balance the continuity of the liquid film and the release efficiency of free dissolved gas, thereby improving the stability of the subsequent atomization boundary.

[0098] After the degassing process is completed, the ion strength of the degassing precursor water is adjusted.

[0099] In this embodiment, the degassed precursor water is first allowed to flow back and forth along a closed-loop mixing path for 180 seconds. The total length of the closed-loop mixing path is 0.85 m, and the circulation flow rate is maintained at 0.32 L / min to reduce the differences in liquid phase composition between different micro-regions in the degassed precursor water. Then, the degassed precursor water after the back and forth flow is introduced into a closed homogenization zone and left to stand for 30 seconds. The effective volume of the closed homogenization zone is 220 mL, and a low-disturbance closed cavity structure is adopted to allow the degassed precursor water to complete the re-homogenization of ion concentration in a relatively static and stable state, thus forming precursor water.

[0100] After multi-point sampling and testing, the average conductivity of the precursor water was 116 μS / cm, and the conductivity deviation at multiple points was reduced to ±3 μS / cm. After the dual-source liquid phase system was subjected to liquid replenishment and reflux disturbance, the time required for the conductivity to recover to a stable value was 52s.

[0101] Comparative Example 7.2 in Table 2 shortened the settling time in the closed homogenization zone to 10s, increased the multi-point conductivity deviation of the precursor water to ±8μS / cm, and extended the conductivity recovery time after dual-source liquid phase disturbance to 95s. Comparative Example 8.2 extends the settling time of the closed homogenization zone to 55s. Although the conductivity deviation at multiple points is improved compared to the 10s condition, the conductivity recovery time after disturbance is further extended to 118s.

[0102] The above results indicate that when the settling time in the closed homogenization zone is too short, the ion concentration redistribution is not fully completed; when the settling time is too long, although the local homogenization degree is improved, the recovery cycle of the dual-source liquid phase system during dynamic operation becomes slower, which is not conducive to the output stability under continuous near-field operation conditions at the bed head. Therefore, limiting the settling time in the closed homogenization zone to 20–45 s, preferably 30 s, is more conducive to achieving a balance between sufficient homogenization and dynamic response capability.

[0103] The precursor water formed above was fed into the subsequent atomization verification section and continuously operated under the same conditions as in Example 1, including subsequent ripening, pre-polarization, main pyrolysis, moisture-rich stabilization, staged separation, branch reflux, rectification, and dew point reduction treatment. Test results showed that the precursor water pretreated according to Example 2.1 had a particle size fluctuation rate of only 6.2% in the atomization output stage, a qualified microparticle flow rate of 86.4% in the subsequent pyrolysis, a boundary condensation rate of 0.5 g / h on the headboard, a PM2.5 removal rate of 75.1% in the breathing zone over 30 minutes, and an output fluctuation rate of 5.4% after 8 hours of continuous operation.

[0104] The above results demonstrate that the precursor water construction process in this embodiment, which involves "sedimentation pre-purification, proportional mixing, electrical correction, thin-layer degassing, and then circulation leveling," can significantly reduce the spatial fluctuations and dynamic recovery lag of the dual-source liquid phase system from the source. This provides a uniform, stable, low-bubble precursor water foundation suitable for controlled treatment, which is an important prerequisite for achieving stable purification of suspended pollutants in the breathing zone air layer and simultaneously suppressing boundary condensation in bedside near-field continuous operation application scenarios.

[0105] Table 2: Comparison of precursor water construction parameters and continuous near-field operation performance at the bed head Parameter name Invention Example 2.1 - Volume ratio 1:5 - Calibration solution 120 μS per cm / 6 parts - Thin liquid layer 0.6 mm - Stand for 30 s Comparative Example 1.2 - Volume ratio 1:3 - otherwise the same as Invention Example 2.1 Comparative Example 2.2 - Volume ratio 1:9 - otherwise the same as Invention Example 2.1 Comparative Example 3.2 - Calibration solution 80 μS per cm / 2 portions - otherwise the same as Invention Example 2.1 Comparative Example 4.2 - Calibration solution 160 μS per cm / 12 portions - otherwise the same as Invention Example 2.1 Comparative Example 5.2 - Thin liquid layer 0.25 mm - otherwise the same as Invention Example 2.1 Comparative Example 6.2 - Thin liquid layer 1.10 mm - otherwise the same as Invention Example 2.1 Comparative Example 7 - Let stand for 10 seconds - otherwise the same as Invention Example 2.1 Comparative Example 8.2 - Let stand for 55 seconds - otherwise the same as Invention Example 2.1 Volume ratio of pre-purified recovered condensate to makeup water stock solution 1:05 1:03 1:09 1:05 1:05 1:05 1:05 1:05 1:05 Conductivity of conductivity correction solution (μS / cm) 120 120 120 80 160 120 120 120 120 The amount of conductivity correction solution to be added (in parts) corresponding to 100 parts of the precursor water to be corrected. 6 6 6 2 12 6 6 6 6 Thin liquid layer thickness (mm) 0.6 0.6 0.6 0.6 0.6 0.25 1.1 0.6 0.6 Settling time (s) in the closed homogenization zone 30 30 30 30 30 30 30 10 55 Initial conductivity of precursor water to be corrected (μS / cm) 72 81 61 72 72 72 72 72 72 Electrical conductivity of the precursor water to be degassed (μS / cm) 118 121 117 91 156 118 118 118 118 Dissolved gas residue (mg / L) 3.1 3.3 3.2 3.2 3.4 4.7 6.1 3.2 3.2 Multi-point conductivity deviation of precursor water (±μS / cm) 3 9 8 7 10 4 4 8 6 Conductivity recovery time (s) after dual-source liquid phase disturbance 52 86 81 93 97 68 74 95 118 Atomized output particle size fluctuation rate (%) 6.2 13.8 12.9 15.9 16.7 10.8 12.4 10.6 9.8 Percentage of qualified microparticle streams after subsequent pyrolysis (%) 86.4 72.3 73.6 66.8 64.9 77.1 74.8 76.4 77.2 Condensation rate on the headboard surface (g / h) 0.5 1.4 1.2 1.5 1.7 0.9 1.1 0.9 0.8 PM2.5 removal rate in the breathing zone over 30 minutes (%) 75.1 63.5 64.8 60.4 58.9 68.5 66.7 68.1 67.5 Output volatility (%) after 8 hours of continuous operation 5.4 10.9 10.3 12.6 11.8 8.2 8.8 9.1 8.9 Table 2 shows that the combination of parameters used in Example 2.1—a volume ratio of 1:5, a conductivity correction solution of 120 μS / cm, 100 parts of precursor water to be corrected corresponding to 6 parts of conductivity correction solution, a thin liquid layer thickness of 0.60 mm, and a closed homogenization zone that has been left to stand for 30 s—can achieve a better precursor water state and more stable subsequent near-field operation results under dual-source liquid phase system conditions.

[0106] First, regarding the volume ratio of pre-purified recovered condensate to replenishment liquid, Invention Example 2.1 uses a ratio of 1:5. The conductivity recovery time after the disturbance of the dual-source liquid phase is only 52s, which is significantly better than 86s in Comparative Example 1.2 and 81s in Comparative Example 2. This indicates that a volume ratio that is too low or too high will weaken the dynamic recovery ability of the dual-source liquid phase system. Meanwhile, the atomization output particle size fluctuation rate of Invention Example 2.1 is only 6.2%, and the output fluctuation rate is only 5.4% after 8 hours of continuous operation, indicating that the 1:5 setting is more conducive to balancing the compositional stability and continuous operation adaptability of the dual-source liquid phase system.

[0107] Secondly, regarding the electrical correction conditions, Example 2.1 used a conductivity correction solution with a conductivity of 120 μS / cm, and added 6 parts of conductivity correction solution for every 100 parts of the precursor water to be corrected. The conductivity of the precursor water to be degassed stabilized at 118 μS / cm. In Comparative Example 3.2, due to the low conductivity of the conductivity correction solution and insufficient addition, the conductivity of the precursor water to be degassed was only 91 μS / cm, and the proportion of qualified microparticles in the subsequent pyrolysis decreased to 66.8%. In Comparative Example 4.2, due to the high conductivity of the conductivity correction solution and excessive addition, the conductivity of the precursor water to be degassed increased to 156 μS / cm, and the multi-point conductivity deviation of the precursor water increased to ±10 μS / cm. This shows that electrical correction should not only consider whether the average value falls within the range, but also whether the spatial distribution is balanced.

[0108] Therefore, limiting the conductivity of the conductivity correction solution to 90–150 μS / cm and limiting the amount added to 3–10 parts for every 100 parts of the precursor water to be corrected has clear process rationality.

[0109] Furthermore, regarding the thickness of the thin liquid layer, Example 2.1 uses a 0.60 mm thin liquid layer, with a dissolved gas residue of only 3.1 mg / L; the thin liquid layer of Comparative Example 5.2 is too thin, resulting in decreased liquid film continuity and an increase in dissolved gas residue to 4.7 mg / L; the thin liquid layer of Comparative Example 6.2 is too thick, resulting in insufficient free interface area and an increase in dissolved gas residue to 6.1 mg / L. This indicates that limiting the thickness of the thin liquid layer to 0.4–0.9 mm is more conducive to balancing liquid film continuity and degassing efficiency.

[0110] Finally, regarding the settling time in the closed homogenization zone, Example 2.1 used 30 s, and the multi-point conductivity deviation of the precursor water was ±3 μS / cm; Comparative Example 7.2 had too short a settling time, and the multi-point conductivity deviation increased to ±8 μS / cm; Comparative Example 8.2 had too long a settling time. Although the multi-point conductivity deviation was reduced, the conductivity recovery time after the dual-source liquid phase disturbance was extended to 118 s. This shows that a longer settling time is not necessarily better, but rather a balance needs to be struck between sufficient re-homogenization of ion concentration and dynamic response speed.

[0111] Based on the above results, it can be concluded that by synergistically limiting the ratio of the dual-source liquid phase system, the electrical correction window, the thin-layer degassing conditions, and the homogenization and settling time, the precursor water is significantly superior to each ratio in terms of spatial homogeneity, dynamic recovery ability, and adaptability to subsequent processes. This is ultimately reflected in a higher proportion of qualified microparticles in subsequent pyrolysis, a lower condensation on the bed head plate boundary, a higher PM2.5 removal rate in the breathing zone, and a lower output fluctuation rate after 8 hours of continuous operation.

[0112] Example 3 Please refer to Figures 1-4 Specifically: the mother droplet group is placed in a closed, humid environment for isothermal maturation, including: Humidifying gas is continuously supplied to the enclosed humidification field, and the relative humidity inside the enclosed humidification field is maintained at 96% to 99%. This allows the mother droplet group to exchange water vapor with the humidified gas within a closed, humid environment. It causes droplets with a diameter of less than 1 μm to absorb moisture and grow, and causes droplets with a diameter of more than 8 μm to settle and detach from the parent droplet group; The droplets with a particle size of 1–8 μm were retained in the mother droplet group to obtain a mature mother droplet group with a median particle size D50 of 1–8 μm.

[0113] The matured mother droplets were sequentially introduced into the pre-polarization region and the main cleavage region, causing a directional charge layer to form on the surface of the matured mother droplets, which then cleaved to form nanoscale negatively charged water-containing particles; wherein: The aging mother droplet group is introduced into the prepolarization region through the outlet channel, so that the aging mother droplet group passes through the prepolarization micro gap. Under the action of unipolar bias with an applied working voltage of 12-48V, the negative charge on the outer surface of the aging mother droplet group migrates and accumulates along the outer surface of the droplet towards the outlet side, forming a surface oriented charge layer. The matured mother droplets with surface oriented charge layers are then introduced into the main pyrolysis region through a connecting channel. The matured mother droplets with surface oriented charge layers pass through the main pyrolysis micro-gap and undergo ionization pyrolysis from the side where the surface oriented charge layer is located under the action of pulse loading with an applied working voltage of 80-220V, forming nanoscale negatively charged water-containing microparticles. The gap width of the main pyrolysis microgap is 0.05–0.30 mm.

[0114] It should be noted that during re-fracture, the initial state of each particle entering the electric field is not exactly the same. Particles may collide, adhere, rehydrate, or locally aggregate before and after re-fracture. Even if some particles are close to being qualified at the moment of re-fracture, they may still deviate from the target state again during subsequent transport due to local humidity, flow field disturbance, or inter-particle interaction. In order to ensure the stability of continuous operation, it is impossible to increase the voltage indefinitely, reduce the gap indefinitely, or extend the residence time indefinitely. Otherwise, it will introduce new fluctuations, excessive fracture, condensation risks, or engineering safety issues. Therefore, re-fracture is usually "to improve the pass rate as much as possible within a controllable window", rather than "forcibly processing all particles at once".

[0115] In this embodiment, a civilian liquid storage humidifier with a rated storage capacity of 2.5L was still selected as the test carrier, and the civilian liquid storage humidifier was placed on the bedside table in a simulated bedroom environment. The same indoor pollutant construction method as in Example 1 was adopted, and the precursor water was the precursor water formed in Example 2. This embodiment focuses on investigating the effects of closed wet field wet maturation treatment and two-stage pyrolysis treatment in the pre-polarization zone and main pyrolysis zone on the near-field continuous operation effect of the bedside table.

[0116] In this embodiment, the closed wet field adopts a closed cavity curing structure. The closed wet field cavity is 220mm long, 55mm wide, and 48mm high. The inlet end is provided with a mother droplet group introduction section and a humidification gas replenishment section, and the outlet end is provided with an outlet channel and connected to the pre-polarization zone.

[0117] The humidifying gas is supplied by an independent constant humidity gas supply unit, with the humidifying gas temperature controlled at 24.5℃ and the linear velocity controlled at 0.17m / s.

[0118] Humidifying gas is continuously supplied to the enclosed wet field, and the relative humidity in the enclosed wet field is kept stable at 97.0%.

[0119] After the mother droplet group enters the closed humid field, the average residence time in the closed humid field is controlled to be 1.6s, so that the mother droplet group and the humidifying gas can continuously exchange water vapor.

[0120] Online particle size analysis results show that under 97.0% relative humidity, droplets with a particle size of less than 1 μm undergo hygroscopic growth and enter the target particle size range. Droplets with a particle size of more than 8 μm detach from the mainstream under the influence of closed wet field turning channels, inertial deviation, and gravity. Droplets with a particle size of 1–8 μm remain in the mainstream and form mature mother droplet groups.

[0121] The median volumetric size (D50) of the mature mother droplet group was 4.3 μm, and the volume fraction of 1–8 μm droplets reached 88.1%.

[0122] The purpose of the above settings is to enable the mother droplet group to complete the particle size boundary convergence before entering the electric field treatment.

[0123] If the median volumetric diameter (D50) of the maturation mother droplet group is less than 1 μm, the droplet size is too small. During the pre-polarization stage, the surface charge migration is easily affected by the random drift of the droplets, and during the main pyrolysis stage, unstable negatively charged water-containing microparticles with larger particle sizes are more likely to form. If the median volumetric diameter (D50) of the maturation mother droplet group is greater than 8 μm, the droplet size is too large. During the main pyrolysis stage, the pyrolysis load increases, the number of coarse residual droplets increases, and the condensation on the near-field boundary surface at the bed head increases accordingly.

[0124] Therefore, controlling the volume median particle size D50 of the ripening mother droplet group within 1–8 μm, preferably within 4.3 μm, is beneficial for simultaneously meeting the surface charge redistribution requirements of the pre-polarization stage and the directional pyrolysis requirements of the main pyrolysis stage.

[0125] After the mature mother droplets leave the closed wet field, they enter the prepolarization zone through the outlet channel.

[0126] The pre-polarization region consists of two oppositely arranged insulating coated plates. The width of the pre-polarization micro-gap is controlled to be 0.20 mm, and the effective length of the plate is controlled to be 26 mm.

[0127] When the aging mother droplet group passes through the prepolarized microgap, it maintains a passage time of about 18ms under the action of 24V unipolar bias, which causes the negative charge on the outer surface of the aging mother droplet group to migrate and accumulate along the outer surface of the droplet towards the outlet side, forming a surface oriented charge layer.

[0128] The surface potential distribution at the outlet location shows that the surface potential on the outlet side accounts for 71.5% after pre-polarization, indicating that the surface charge of the matured mother droplet group has changed from a relatively dispersed state to an enriched state along the outlet side.

[0129] The purpose of setting up the pre-polarization region is to first establish a surface oriented charge layer, and then send the mature mother droplet group with the surface oriented charge layer into the main pyrolysis region, so that the main pyrolysis region can undergo more stable oriented ionization pyrolysis along the side where the surface oriented charge layer is located.

[0130] If the pre-polarization working voltage is lower than 12V, the driving force for the migration of negative charges on the surface of the maturation mother droplet group is insufficient, the surface directional charge layer is not fully established, and the subsequent main pyrolysis directionality is weakened; if the pre-polarization working voltage is higher than 48V, the front field effect is too strong, the surface state of the maturation mother droplet group is more sensitive to the fluctuation of the operating conditions, and the output stability decreases under continuous operation.

[0131] In this embodiment, the pre-polarization operating voltage is controlled at 24V, which is in the middle of the 12-48V range, balancing the sufficiency of the surface oriented charge layer formation and the stability of continuous operation.

[0132] The mature mother droplets with surface-oriented charge layers then enter the main pyrolysis region through a connecting channel; the main pyrolysis region adopts a pulse-loaded electrode structure, the width of the main pyrolysis microgap is controlled at 0.12 mm, the working voltage is controlled at 160 V, the pulse frequency is controlled at 20 kHz, and the duty cycle is controlled at 35%.

[0133] When the mature mother droplets with a surface-oriented charge layer pass through the main pyrolysis micro-gap, they undergo directional ionization pyrolysis from the side where the surface-oriented charge layer is located, forming nanoscale negatively charged water-containing microparticles.

[0134] The role of the prepolarization region is to enable the ripening mother droplet group to form a surface oriented charge layer before entering the main pyrolysis region, rather than to pyrolyze prematurely within the prepolarization region.

[0135] The median particle size (D50) of the matured mother droplet group was controlled to be 1–8 μm, the water conductivity of the precursor was controlled to be 50–200 μS / cm, and the matured mother droplet group was directed into the prepolarized microgap through the outlet channel.

[0136] Even with an applied working voltage of 12–48V, a local electric field can be formed on the outer surface of the droplet within the prepolarized microgap. This causes the migratable negative charges on the outer surface of the droplet to migrate and accumulate along the outer surface of the droplet towards the outlet side, thereby forming a surface-oriented charge layer.

[0137] Therefore, it can be seen that the low voltage in this embodiment can work not by the voltage value alone, but by the combined effect of the prepolarized microgap, the particle size of the mature mother droplet group, the conductivity state of the precursor water, and the droplet passage time.

[0138] The surface oriented charge layer refers to the asymmetric negative charge enrichment layer formed on the outer surface of the droplets along the exit side direction when the ripening mother droplet group passes through the prepolarization zone.

[0139] The surface-oriented charge layer is located in a shallow region on the outer surface of the droplet, and its thickness is preferably 5% to 15% of the droplet's equivalent radius.

[0140] After the surface oriented charge layer is formed, the average surface charge density of the droplet exit side hemisphere is higher than that of the inlet side hemisphere, and the ratio of the average surface charge density of the exit side to the inlet side is preferably 1.5 to 4.0.

[0141] In this embodiment, the surface potential ratio on the outlet side after pre-polarization reaches 71.5%, and the ratio of the equivalent average surface charge density on the outlet side to that on the inlet side is 2.3. Based on this, it can be determined that the surface oriented charge layer has been formed.

[0142] The surface-oriented charge layer in this embodiment differs from that of ordinary polarized droplets. Ordinary polarized droplets mainly exhibit changes in the overall dipole moment of the droplet, and the charge distribution on the outer surface of the droplet remains approximately symmetrical, which cannot provide a stable directional initiation surface for subsequent main pyrolysis.

[0143] The surface-oriented charge layer manifests as a recognizable negative charge enrichment region on the outer surface of the droplets along the exit side. This allows the matured mother droplets carrying the surface-oriented charge layer to preferentially undergo ionization and fragmentation from the exit side after entering the main fragmentation zone. This improves the directionality of the main fragmentation, reduces the dispersion of the particle size distribution after fragmentation, and increases the proportion of qualified microparticles in the subsequent fragmentation stream.

[0144] Particle size distribution analysis showed that the median volumetric diameter (D50) of the negatively charged water-containing microparticles after the main pyrolysis was 186 nm. Potential analysis showed that the zeta potential of the negatively charged water-containing microparticles after the main pyrolysis was -33 mV. Subsequent fractionation and separation analysis showed that the proportion of qualified microparticles in the subsequent pyrolysis stream reached 87.2%.

[0145] In this embodiment, the main pyrolysis operating voltage is controlled at 160V and the main pyrolysis micro-gap width is controlled at 0.12mm. The aim is to achieve a balance between lower overall energy consumption, higher directional pyrolysis efficiency, and better continuous operation stability.

[0146] If the main pyrolysis operating voltage is below 80V, the local pyrolysis driving force is insufficient, resulting in negatively charged water-containing particles with larger diameters and lower charge levels after main pyrolysis, and a significant decrease in the proportion of qualified particle streams in subsequent pyrolysis. If the main pyrolysis operating voltage is above 220V, although the degree of local pyrolysis is enhanced, excessive pyrolysis and overly strong field response are more likely to cause continuous operational fluctuations. If the width of the main pyrolysis microgap is greater than 0.30mm, the local field strength decreases, and the sufficiency and directionality of main pyrolysis are insufficient. If the width of the main pyrolysis microgap is less than 0.05mm, the local field effect is too strong, which is more likely to cause droplet retention, local liquid bridges, or increased output fluctuations.

[0147] Therefore, controlling the main pyrolysis working voltage at 80–220V and the main pyrolysis micro-gap width at 0.05–0.30mm, preferably 160V and 0.12mm, is beneficial for forming nanoscale negatively charged water-containing microparticles with more concentrated particle size, more stable charge, and higher subsequent utilization rate.

[0148] After completing the closed wet field aging, pre-polarization zone treatment and main pyrolysis zone treatment, the continuous operation verification was carried out according to the subsequent wet stabilization, graded separation, branch reflux, rectification and dew point reduction treatment conditions in Example 1.

[0149] Test results show that, under the operating conditions of this embodiment, after 30 minutes of continuous operation in the near field of the bed, the PM2.5 removal rate in the air layer of the human breathing zone reached 78.2%, the condensation on the boundary surface of the bed headboard was 0.4 g / h, and the output fluctuation rate was 5.1% after 8 hours of continuous operation.

[0150] Compared to the conditions where the median volumetric particle size (D50) of the maturation mother droplet group is less than 1 μm and greater than 8 μm, the pre-polarization working voltage is less than 12 V and greater than 48 V, the main pyrolysis working voltage is less than 80 V and greater than 220 V, and the main pyrolysis microgap width is less than 0.05 mm and greater than 0.30 mm, this embodiment maintains a better state in terms of the median volumetric particle size (D50) of the negatively charged water-containing microparticles after the main pyrolysis, the Zeta potential, the proportion of qualified microparticles in the subsequent pyrolysis, the boundary condensation on the headboard, and the output fluctuation rate after 8 hours of continuous operation.

[0151] This demonstrates that the two-stage process chain of "closed wet field isohumidification, prepolarization zone and main pyrolysis zone" defined in this embodiment can simultaneously solve the two problems of unstable input boundary before pyrolysis and insufficient directionality during pyrolysis. It is an important technical basis for achieving stable purification of suspended pollutants in the air layer of the breathing zone under the condition of continuous operation in the near field at the bed head in this embodiment. The specific contents are shown in Table 3.

[0152] Table 3: Effects of isowet ripening and two-stage pyrolysis parameter windows on near-field continuous operation performance at the bed head. Parameter name Invention Example 3.1 - The maturation mother droplet group D50 is 4.3 μm - Pre-polarization 24V - Main pyrolysis 160V - Main pyrolysis micro-gap 0.12 mm Comparative Example 1.3 - The D50 of the matured mother droplet group was below the lower limit of -0.8 μm - otherwise the same as Invention Example 3.1 Comparative Example 2.3 - The D50 of the matured mother droplet group is higher than the upper limit - 9.1 μm - otherwise the same as Invention Example 3.1 Comparative Example 3.3 - Pre-polarization voltage and main pyrolysis voltage are below the lower limit, and the main pyrolysis microgap is above the upper limit - Pre-polarization 8V - Main pyrolysis 70V - Microgap 0.36mm Comparative Example 4.3 - Pre-polarization voltage and main pyrolysis voltage are higher than the upper limit, and the main pyrolysis microgap is lower than the lower limit - Pre-polarization 54V - Main pyrolysis 240V - Microgap 0.03mm Matured mother droplet group D50 (μm) 4.3 0.8 9.1 4.2 4.4 Volume fraction of 1–8 μm droplets (%) 88.1 58.6 54.9 87.8 87.4 Pre-polarization operating voltage (V) 24 24 24 8 54 Main decomposition operating voltage (V) 160 160 160 70 240 Main pyrolysis microgap width (mm) 0.12 0.12 0.12 0.36 0.03 Percentage of surface potential on the outlet side after pre-polarization (%) 71.5 69.8 70.1 55.2 83.6 The negatively charged water-containing particles after the main cleavage have a D50 (nm) value. 186 326 298 392 142 Zeta potential (mV) after main cleavage -33 -23 -25 -17 -43 Percentage of qualified microparticle streams after subsequent pyrolysis (%) 87.2 66.1 62.8 53.6 57.4 Condensation rate on the headboard surface (g / h) 0.4 0.9 1.4 1.6 1.2 PM2.5 removal rate in the breathing zone over 30 minutes (%) 78.2 60.8 57.6 49.2 55.8 Output volatility (%) after 8 hours of continuous operation 5.1 8.9 9.7 13.1 12.6 Table 3 shows that the combination of parameters used in Example 3.1, namely, a median particle size D50 of 4.3 μm for the matured mother droplet group, a pre-polarization working voltage of 24 V, a main pyrolysis working voltage of 160 V, and a main pyrolysis microgap width of 0.12 mm, can simultaneously achieve mother droplet boundary stabilization before pyrolysis and surface charge direction stabilization during pyrolysis in a near-field continuous operation scenario at the bedside, thereby significantly improving the subsequent output quality.

[0153] First, in terms of controlling the boundary of the maturation mother droplet group, Invention Example 3.1 controls the median particle size D50 of the maturation mother droplet group within the range of 1 to 8 μm, and preferably 4.3 μm. The volume fraction of 1 to 8 μm droplets reaches 88.1%, indicating that the mother droplet group entering the prepolarization zone and the main pyrolysis zone after wet maturation in a closed wet field is in a relatively ideal particle size range.

[0154] In Comparative Example 1.3, the median volumetric diameter (D50) of the maturation mother droplet group decreased to 0.8 μm, below the lower limit of 1 μm. After the main pyrolysis, the D50 of the negatively charged water-containing particles increased to 326 nm, and the proportion of qualified particles in the subsequent pyrolysis flow decreased to 66.1%. This indicates that when the maturation mother droplet group is too fine, the small droplets are more prone to random drift and unstable surface charge migration in the electric field, which ultimately weakens the directionality of the main pyrolysis.

[0155] In Comparative Example 2.3, the median volumetric diameter (D50) of the maturated mother droplet group increased to 9.1 μm, which is higher than the upper limit of 8 μm. The boundary condensation on the headboard increased to 1.4 g / h, and the PM2.5 removal rate in the breathing zone decreased to 57.6% in 30 min. This indicates that when the maturated mother droplet group is too coarse, it is more difficult for large droplets to be fully broken down, and both coarse residual droplets and near-field wet load increase significantly.

[0156] Therefore, limiting the median particle size D50 of the matured mother droplet group to 1–8 μm has clear process significance.

[0157] Secondly, regarding the pre-polarization operating voltage, Example 3.1 uses 24V, and the surface potential ratio on the outlet side reaches 71.5% after pre-polarization, indicating that the directional charge layer on the surface of the mature mother droplet group is sufficiently established.

[0158] In Comparative Example 3.3, the pre-polarization working voltage was reduced to 8V, which is lower than the 12V lower limit. After pre-polarization, the surface potential ratio on the outlet side was only 55.2%, indicating that the migration and accumulation of surface charge to the outlet side was significantly insufficient. After the main pyrolysis, the D50 of the negatively charged water-containing particles increased to 392nm, and the proportion of qualified particles in the subsequent pyrolysis flow decreased to 53.6%.

[0159] In Comparative Example 4.3, the pre-polarization operating voltage was increased to 54V, which is higher than the upper limit of 48V. Although the surface potential ratio on the output side increased to 83.6%, the output fluctuation rate increased to 12.6% after 8 hours of continuous operation, indicating that an excessively strong field effect in the pre-polarization front section would amplify system fluctuations.

[0160] Therefore, limiting the pre-polarization operating voltage to 12–48V, preferably 24V, can balance the sufficiency of surface oriented charge layer formation with continuous operation stability.

[0161] Furthermore, regarding the main pyrolysis operating voltage and the main pyrolysis microgap width, Example 3.1 uses 160V and 0.12mm. After the main pyrolysis, the D50 of the negatively charged water-containing particles is 186nm, the Zeta potential is -33mV, and the proportion of qualified particles in the subsequent pyrolysis reaches 87.2%, indicating that the main pyrolysis is sufficient and the output is stable.

[0162] In Comparative Example 3.3, the main pyrolysis operating voltage was reduced to 70V and the main pyrolysis microgap width was increased to 0.36mm. After main pyrolysis, the D50 of negatively charged water-containing particles increased to 392nm, the Zeta potential was only -17mV, and the PM2.5 removal rate in the respiratory zone decreased to 49.2% after 30min. This indicates that when the main pyrolysis operating voltage is below 80V and the main pyrolysis microgap width is above 0.30mm, the local field strength is insufficient, the pyrolysis is incomplete, and the directionality is poor.

[0163] In Comparative Example 4.3, the main pyrolysis operating voltage was increased to 240V and the main pyrolysis microgap width was reduced to 0.03mm. Although the D50 of negatively charged water-containing particles decreased to 142nm after main pyrolysis, the boundary condensation on the headboard plate still reached 1.2g / h. After 8 hours of continuous operation, the output fluctuation rate reached 12.6%. This indicates that when the main pyrolysis operating voltage is higher than 220V and the main pyrolysis microgap width is lower than 0.05mm, the local field effect is too strong, which can easily lead to excessive pyrolysis, output fluctuation, and decreased near-field adaptability.

[0164] This demonstrates that limiting the main pyrolysis operating voltage to 80–220V and the main pyrolysis micro-gap width to 0.05–0.30mm, with 160V and 0.12mm being preferred, can achieve a more reasonable balance between pyrolysis sufficiency, particle size concentration, charge stability, and continuous operation adaptability.

[0165] Based on Table 3, it can be concluded that the innovation embodied in Invention Example 3.1 is not a simple high-humidity treatment plus electric field treatment, but rather by locking the median particle size D50 of the mature mother droplet group within the range of 1 to 8 μm, and locking the pre-polarization working voltage, the main pyrolysis working voltage, and the main pyrolysis microgap width within the ranges of 12 to 48 V, 80 to 220 V, and 0.05 to 0.30 mm, respectively, so that the mother droplet boundary is stable before pyrolysis and the directional charge control is achieved simultaneously during pyrolysis.

[0166] It is this continuous process chain that enables this embodiment to outperform the comparative examples in several aspects, including the D50 of negatively charged water-containing particles after the main pyrolysis, the Zeta potential, the proportion of qualified particles in subsequent pyrolysis, the condensation on the boundary surface of the bed headboard, the PM2.5 removal rate in the breathing zone at 30 min, and the output fluctuation rate after 8 hours of continuous operation.

[0167] Example 4 Please refer to Figures 1-4 Specifically: nano-sized negatively charged water-containing particles are introduced into a humid and weak field region, so that the relative humidity of the humid and weak field region is maintained at 92% to 98%, and the nano-sized negatively charged water-containing particles are made to come into contact with the humidifying gas in the humid and weak field region, so that the outer surface of the nano-sized negatively charged water-containing particles adsorbs water molecules and completes the redistribution of surface charge, forming a hydrated and stable particle flow. The hydrated stable microparticle stream is then introduced into the graded separation zone, where it first changes direction through a deflection section. The inertial difference is used to cause the large droplets that are not completely broken up to break away from the mainstream and form large droplet components. Then, the mainstream after the deflection and separation section is made to enter the deflection and separation section. Under the action of the lateral bias electric field, the undercharged water-containing particles deviate from the mainstream and form a component of undercharged electron water particles. The particles that maintain the mainstream output after the deflection separation section form a qualified particle stream, while the large droplet component and the undercharged electron water particle component constitute an unqualified particle stream.

[0168] Large droplet components are introduced into the return liquid collection area, where they are aggregated to form a reflux liquid phase. The reflux liquid phase is then introduced into the inlet liquid merging section before the atomization section through the liquid phase reflux channel, where it merges with the precursor water to form a re-atomized material stream. The undercharged water-containing microparticles are introduced into the microparticle reflux channel, and the electron-deficient water microparticles are introduced into the re-pyrolysis introduction section before the main pyrolysis zone through the microparticle reflux channel, where they merge with the mature mother droplets with surface oriented charge layers to form a re-pyrolysis stream. The re-atomized stream is then allowed to enter the atomization section for further atomization, while the re-pyrolysis stream is allowed to enter the main pyrolysis zone for further ionization and pyrolysis. The liquid phase reflux channel and the particle reflux channel are isolated from each other.

[0169] In this embodiment, a civilian liquid storage humidifier with a rated storage capacity of 2.5L is still selected as the test carrier, and the civilian liquid storage humidifier is placed on the bedside table in a simulated bedroom environment. The same pollutant construction method as in Example 1 is adopted. The wet ripening, prepolarization and main pyrolysis of the precursor water are carried out under the preferred conditions of Examples 1 to 3, so that the nano-sized negatively charged water-containing particles formed after the main pyrolysis enter the wet-rich weak field region and the graded separation region of this embodiment.

[0170] The humidified, weak-field zone is located between the outlet of the main pyrolysis zone and the inlet of the staged separation zone. It adopts a closed, steady-state flow channel structure with a length of 95 mm, a width of 18 mm, and a height of 12 mm. The humidifying gas is supplied by an independent humidification branch, with the temperature controlled at 24.5℃ and the linear velocity controlled at 0.14 m / s.

[0171] Enclosed electrode plates are installed in the humid and weak field area with a plate spacing of 2.0 mm. The working field strength in the area is controlled at 0.10 kV / cm. Insulation isolation sections are installed on both sides of the electrode plates.

[0172] After the main pyrolysis, the negatively charged nanoparticles containing water come into contact with the humidified gas in a humid and weak field region for 0.85 s. This causes water molecules to be adsorbed on the outer surface of the negatively charged nanoparticles and the surface charge to be redistributed, forming a hydrated and stable microparticle stream.

[0173] In this embodiment, the relative humidity of the humid and weak field area is controlled at 95%. Under this condition, the potential retention rate reaches 89.4% after hydration stabilization for 30 seconds.

[0174] The relative humidity in the wet and weak field area is limited to 92% to 98% in order to simultaneously satisfy the requirements of sufficient surface hydration and controllable near-field moisture load.

[0175] If the relative humidity in the wet and weak field area is below 92%, for example, the relative humidity in Comparative Example A is 90%, then the hydration of the outer surface of the particles is insufficient. After hydration stabilization, the potential retention rate is only 68.7% after 30 seconds. The identification and recovery rate of the insufficiently charged water-containing particle components decreases to 62.8%, the proportion of qualified particle streams decreases to 71.5%, the boundary condensation on the headboard increases to 0.93 g / h, and the output fluctuation rate increases to 9.8% after 8 hours of continuous operation.

[0176] If the relative humidity in the humid and weak field area is higher than 98%, for example, the relative humidity in Comparative Example B is 99%, although the potential retention rate can still be maintained at 84.1%, the separation rate of large droplet components decreases to 75.4%, the condensation on the boundary surface of the bed head increases to 1.58 g / h, and the output fluctuation rate increases to 11.1% after 8 hours of continuous operation.

[0177] Therefore, the relative humidity in the humid and weak field area should be controlled at 92% to 98%, preferably 95%, which is more conducive to balancing the hydration stability of microparticles, the accuracy of subsequent classification, and the near-field adaptability of the bed.

[0178] After leaving the humid and weak field region, the hydrated stable microparticle stream enters the graded separation region.

[0179] The graded separation zone consists of a deflection section and a deflection separation section connected in sequence. The deflection section has a mainstream turning angle of 42° and an effective length of 34 mm. The hydrated stable microparticle stream first turns through the deflection section, and the inertial difference causes the incompletely fragmented large droplets to deviate from the mainstream and enter the large droplet collection branch, forming large droplet components. In this embodiment, the separation rate of large droplet components reaches 82.7%.

[0180] After passing through the deflection and separation section, the mainstream continues into the deflection and separation section. The effective length of the deflection and separation section is 28 mm, and it is equipped with lateral bias electrodes. The lateral bias electric field strength is controlled at 0.08 kV / cm. To ensure a clear basis for determining the "shunting critical distance," this embodiment defines the shunting critical distance as: the lateral distance from the mainstream centerline to the boundary of the mainstream maintaining channel at the exit section of the deflection and separation section, and sets it to 1.20 mm.

[0181] Water-containing particles with a offset distance of less than 1.20 mm along the lateral bias electric field direction enter the lateral collection branch, forming a component of undercharged water-containing particles; particles with an offset distance of greater than or equal to 1.20 mm along the lateral bias electric field direction and maintaining the mainstream output constitute a qualified particle stream.

[0182] In this embodiment, the recovery rate of undercharged water-containing particulate components reached 78.6%, and the proportion of qualified particulate streams reached 88.3%.

[0183] In this embodiment, large droplet components are introduced into the return liquid collection area, where they converge to form a reflux liquid phase. This reflux liquid phase is then introduced through the liquid phase reflux channel into the inlet merging section before the atomization section, where it merges with the precursor water to form a re-atomized stream; the re-atomization utilization rate of the reflux liquid phase reaches 91.2%. Simultaneously, undercharged water-containing microparticle components are introduced into the microparticle reflux channel and then introduced through the microparticle reflux channel into the re-pyrolysis introduction section before the main pyrolysis zone, where they merge with a group of mature mother droplets carrying a surface-oriented charge layer to form a re-pyrolysis stream; the re-pyrolysis utilization rate of the undercharged water-containing microparticle components reaches 84.5%. The liquid phase reflux channel and the microparticle reflux channel are isolated from each other, with the liquid phase reflux channel having an inner diameter of 3.0 mm and the microparticle reflux channel having an inner diameter of 1.2 mm, to avoid mutual interference between liquid phase condensation and microparticle agglomeration in the same reflux branch.

[0184] In Comparative Example C, the lateral bias electric field of the deflection separation section was turned off and the backflow of undercharged water-containing microparticles was canceled. As a result, the proportion of qualified microparticles was only 69.2%, and the output volatility increased to 12.4% after 8 hours of continuous operation.

[0185] In Comparative Example D, the liquid phase reflux channel and the particle reflux channel are shared. The utilization rate of reflux liquid phase re-atomization is reduced to 84.6%, the utilization rate of undercharged water-containing particles re-decomposition is reduced to 61.7%, the boundary condensation on the headboard plate is increased to 0.88 g / h, and the output fluctuation rate is increased to 10.6% after 8 hours of continuous operation.

[0186] The above results indicate that both the deflection separation section screening and the dual reflux isolation setup are necessary process features.

[0187] After completing the hydration stabilization in the humid and weak field area, inertial separation in the deflection section, charge identification in the deflection separation section, and closed-loop processing of the dual return flow, continuous operation verification was carried out according to the rectification and dew point reduction processing conditions in Example 1.

[0188] Test results show that, under the preferred operating conditions in this embodiment, the condensation rate on the headboard is 0.45 g / h, the PM2.5 removal rate in the breathing zone reaches 79.1% in 30 min, and the output fluctuation rate is 4.9% after 8 hours of continuous operation.

[0189] This demonstrates that the process chain of this embodiment, which includes "hydration stabilization in the humid and weak field area, inertial separation in the deflection and flow section, charge identification in the deflection and separation section, and separation and isolation of liquid phase reflux and particle reflux," can further stabilize, screen, and reuse nanoscale negatively charged water-containing particles after main pyrolysis. This is an important technical part of this embodiment for achieving stable purification of suspended pollutants in the air layer of the human breathing zone under continuous near-field operation conditions at the bedside.

[0190] Example 5 Please refer to Figures 1-4Specifically: the qualified microparticle stream is guided into the rectifier channel for co-current flow to form an axial microparticle stream; The axial particulate stream is then brought into parallel contact with the humidifying airflow, wherein the absolute moisture content of the humidifying airflow is lower than that of the axial particulate stream. This causes the axial particulate stream to release water vapor and lowers its dew point by 1.5–4.0°C, forming a purified output stream. The purified output stream is then released into the indoor space through the mist outlet.

[0191] In this embodiment, the bedside near-field continuous operation application scenario of Embodiments 1 to 4 is still used. The civilian liquid storage humidifier is installed on the bedside table. The precursor water isohumidification, prepolarization, main pyrolysis, hydration stabilization, staged separation and dual reflux are all carried out under the preferred conditions of Embodiments 1 to 4, so that the qualified microparticle stream enters the rectification and dew point reduction treatment section of this embodiment.

[0192] In this embodiment, the qualified microparticle stream is guided into the rectifier channel for co-current flow guidance. The rectifier channel adopts a straight, narrow, and long channel structure with a channel length of 120mm, a channel width of 10mm, and a channel height of 8mm. Parallel rectifier vanes are installed inside, with a vane spacing of 1.5mm, to reduce the transverse turbulence component and make the qualified microparticle stream form a stable mainstream along the mist exit direction.

[0193] After passing through the rectifier channel, the qualified microparticle stream forms an axial microparticle stream. According to flow field detection, the axial velocity at the outlet of the rectifier channel accounts for 91.8%, indicating that the rectifier channel has transformed the microparticle stream from a multi-directional disturbance state to a directional flow state dominated by axial transport.

[0194] The purpose of setting up the rectification channel is to reduce the lateral diffusion and local eddies of the microparticle flow before the mist outlet, thereby providing a more stable contact interface for the subsequent humidification airflow to make parallel contact.

[0195] After the axial microparticle stream is formed, it is then brought into parallel contact with the humidified airflow.

[0196] In this embodiment, the humidifying airflow is provided by an independent low-humidity branch, the temperature of the humidifying airflow is controlled at 23.8℃, and the absolute moisture content of the humidifying airflow is controlled at 9.1 g / m³; the absolute moisture content of the axial particulate stream before entering the humidifying contact section is 11.8 g / m³. 3 The humidity-regulating contact section is 85mm long and adopts a parallel flow sandwich channel structure. The axial microparticle flow and the humidity-regulating airflow maintain the same direction of flow, and the contact time is controlled at 0.72s.

[0197] Since the absolute moisture content of the humidified airflow is lower than that of the axial particulate flow, the axial particulate flow releases some water vapor during the parallel flow contact process, causing the dew point of the axial particulate flow to drop from 16.6℃ to 13.9℃, a decrease of 2.7℃, thus forming a purified output flow.

[0198] After the purified output is released into the indoor space through the mist outlet, it maintains its ability to capture and promote the sedimentation of suspended pollutants in the human breathing zone, while reducing the risk of cold and wet deposits on the near-field surface of the bed.

[0199] In this embodiment, under the above conditions, the condensation on the headboard surface is 0.38 g / h, the PM2.5 removal rate in the breathing zone is 78.4% in 30 min, and the output fluctuation rate is 4.7% after 8 hours of continuous operation.

[0200] The dew point reduction of axial particulate flow is limited to 1.5–4.0 °C to establish a balance between near-field condensation suppression capability and effective wet load retention capability of particulates.

[0201] If the dew point decrease is less than 1.5℃, it indicates that the axial particulate stream is not releasing enough water vapor, and the purified output stream still carries a high humidity load.

[0202] In Comparative Example E, by reducing the humidifying airflow rate and increasing the absolute moisture content of the humidifying airflow, the dew point of the axial particulate flow was reduced by only 0.9℃. Under these conditions, the boundary condensation on the headboard increased to 0.86 g / h, and the output fluctuation rate increased to 7.9% after 8 hours of continuous operation. This indicates that when the dew point reduction is insufficient, the risk of wet deposition in the near-field of fog exit remains high, and the effect of suppressing boundary condensation on the near-field of the headboard is not ideal.

[0203] If the dew point reduction is higher than 4.0℃, it indicates that the axial particulate stream releases too much water vapor. Although the near-field wet load is further reduced, the effective wet load on the particulate surface decreases too quickly, which may weaken the stabilizing effect of the purified output stream in the breathing zone air layer.

[0204] In Comparative Example F, by increasing the flow rate of the humidifying airflow and further reducing the absolute moisture content of the humidifying airflow, the dew point of the axial particulate flow was reduced by 4.8°C.

[0205] Under these conditions, although the condensation on the headboard surface decreased to 0.31 g / h, the PM2.5 removal rate in the breathing zone decreased to 69.2% within 30 minutes, and the output fluctuation rate increased to 6.8% after 8 hours of continuous operation. This result indicates that when the dew point is lowered too much, although the purified output stream is drier, the effective moisture content in the axial particulate stream is weakened, affecting the stability of the particles' action in the human breathing zone air layer.

[0206] Therefore, the dew point reduction value is controlled between 1.5 and 4.0℃, preferably between 2.7℃, which can simultaneously ensure the inhibition of near-field boundary condensation at the bedside, the purification effect of suspended pollutants in the breathing zone air layer, and the stability of continuous operation throughout the night.

[0207] In this embodiment, the rectifier channel first converts the qualified microparticle stream into an axial microparticle stream, and then uses a humidified airflow with a lower absolute moisture content to make parallel contact, so that the axial microparticle stream completes appropriate moisture release and dew point adjustment before fogging, thereby further converting the qualified microparticle stream formed in the front section into a purified output stream that is more suitable for continuous operation in the near field at the bedside.

[0208] Although embodiments of the invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention.

Claims

1. An indoor air purification process based on nano-micro-mist ionization, characterized in that, include: The replenishing solution in the storage humidifier is combined with the condensate recovered from the mist outlet zone. The combined liquid phase system is then subjected to electrical correction, degassing, and ion strength balancing to obtain precursor water with an electrical conductivity of 50–200 μS / cm. The precursor water is fed into the atomization section for atomization to form a group of mother droplets. The mother droplets are then placed in a closed wet field for isohumid ripening to obtain a ripened mother droplet group with a median particle size D50 of 1 to 8 μm. The ripened mother droplets are then sequentially introduced into the prepolarization zone and the main pyrolysis zone to form a directional charge layer on the surface of the ripened mother droplets and pyrolyze them to form nanoscale negatively charged water-containing particles. Negatively charged water-containing microparticles are introduced into a humid and weak field region for hydration stabilization to obtain a hydrated and stable microparticle stream. The hydrated and stable microparticle stream is then separated to obtain a qualified microparticle stream and an unqualified microparticle stream. The defective microparticle stream includes large droplet components and undercharged electron water microparticle components; The large droplet components and the undercharged electron water microparticle components are then diverted back to the atomization section and the main pyrolysis zone to continue processing the unqualified microparticle streams. The qualified microparticle stream is rectified and dew point reduced to obtain a purified output stream, which is then released into the indoor space.

2. The indoor air purification process based on nano-micro-mist ionization according to claim 1, characterized in that, The replenishing solution in the storage-type humidifier is combined with the condensate recovered in the mist outlet zone, including: The condensate recovered from the mist outlet area is introduced into the settling buffer zone for static settling to obtain pre-purified recovered condensate; The pre-purified recovered condensate and the makeup water stock solution are then introduced into a mixing buffer for cyclic mixing. The volume ratio of the pre-purified recovered condensate to the makeup water stock solution is 1:4 to 1:8, resulting in the precursor water to be corrected.

3. The indoor air purification process based on nano-micro-mist ionization according to claim 2, characterized in that, Electrical correction treatment was performed on the precursor water to be corrected; The electrical correction process involves introducing the precursor water to be corrected into the conductivity correction zone of the storage humidifier. Then, add conductivity correction liquid to the conductivity correction zone and circulate and mix the precursor water to be corrected with the conductivity correction liquid until the conductivity of the circulated and mixed liquid phase reaches 50-200 μS / cm, thus obtaining the precursor water to be degassed. The conductivity of the conductivity correction solution is 90-150 μS / cm, and by volume, the precursor water to be corrected is 100 parts, and the conductivity correction solution is 3-10 parts.

4. The indoor air purification process based on nano-micro-mist ionization according to claim 3, characterized in that, The water precursor to be degassed is subjected to degassing treatment and ion strength leveling treatment; The degassing process involves spreading the water, the precursor to be degassed, along the liquid surface to form a thin liquid layer with a thickness of 0.4–0.9 mm. The thin liquid layer is then introduced into the depressurization and gas separation zone to release the free dissolved gas in the precursor water to be degassed, thus obtaining the degassed precursor water; The ion strength leveling process involves reciprocating the degassed precursor water along a closed-loop mixing path. The degassed precursor water, after reciprocating flow, is then introduced into a closed homogenization zone and allowed to stand for 20–45 seconds to make the ion concentration distribution in different micro-regions of the degassed precursor water tend to be uniform, thus forming precursor water.

5. The indoor air purification process based on nano-micro-mist ionization according to claim 4, characterized in that, The step of placing the mother droplet group in a closed humid field for isotropic maturation includes: Humidifying gas is continuously supplied to the enclosed humidification field, and the relative humidity inside the enclosed humidification field is maintained at 96% to 99%. This allows the mother droplet group to exchange water vapor with the humidified gas within a closed, humid environment. It causes droplets with a diameter of less than 1 μm to absorb moisture and grow, and causes droplets with a diameter of more than 8 μm to settle and detach from the parent droplet group; The droplets with a particle size of 1–8 μm were retained in the mother droplet group to obtain a mature mother droplet group with a median particle size D50 of 1–8 μm.

6. The indoor air purification process based on nano-micro-mist ionization according to claim 5, characterized in that, The matured mother droplets were sequentially introduced into the pre-polarization region and the main cleavage region, causing a directional charge layer to form on the surface of the matured mother droplets, which then cleaved to form nanoscale negatively charged water-containing particles; wherein: The aging mother droplet group is introduced into the prepolarization region through the outlet channel, so that the aging mother droplet group passes through the prepolarization micro gap. Under the action of unipolar bias with an applied working voltage of 12-48V, the negative charge on the outer surface of the aging mother droplet group migrates and accumulates along the outer surface of the droplet towards the outlet side, forming a surface oriented charge layer. The matured mother droplets with surface oriented charge layers are then introduced into the main pyrolysis region through a connecting channel. The matured mother droplets with surface oriented charge layers pass through the main pyrolysis micro-gap and undergo ionization pyrolysis from the side where the surface oriented charge layer is located under the action of pulse loading with an applied working voltage of 80-220V, forming nanoscale negatively charged water-containing microparticles. The gap width of the main pyrolysis microgap is 0.05 to 0.30 mm.

7. The indoor air purification process based on nano-micro-mist ionization according to claim 6, characterized in that, The negatively charged nanoparticles are introduced into a humid and weak field region, and the relative humidity of the humid and weak field region is maintained at 92% to 98%. The negatively charged nanoparticles are then in contact with the humidifying gas in the humid and weak field region, so that water molecules are adsorbed on the outer surface of the negatively charged nanoparticles and the surface charge is redistributed, forming a hydrated and stable particle flow. The hydrated stable microparticle stream is then introduced into the graded separation zone, where it first changes direction through a deflection section. The inertial difference is used to cause the large droplets that are not completely broken up to break away from the mainstream and form large droplet components. Then, the mainstream after the deflection and separation section is made to enter the deflection and separation section. Under the action of the lateral bias electric field, the undercharged water-containing particles deviate from the mainstream and form a component of undercharged electron water particles. The particles that maintain the mainstream output after the deflection separation section form a qualified particle stream, wherein the large droplet component and the undercharged electron water particle component constitute an unqualified particle stream.

8. The indoor air purification process based on nano-micro-mist ionization according to claim 7, characterized in that, Large droplet components are introduced into the return liquid collection area, where they are aggregated to form a reflux liquid phase. The reflux liquid phase is then introduced into the inlet liquid merging section before the atomization section through the liquid phase reflux channel, where it merges with the precursor water to form a re-atomized material stream. The undercharged water-containing microparticles are introduced into the microparticle reflux channel, and the electron-deficient water microparticles are introduced into the re-pyrolysis introduction section before the main pyrolysis zone through the microparticle reflux channel, where they merge with the mature mother droplets with surface oriented charge layers to form a re-pyrolysis stream. The re-atomized stream is then introduced into the atomization section for further atomization, and the re-pyrolysis stream is introduced into the main pyrolysis zone for further ionization and pyrolysis. The liquid phase reflux channel and the particle reflux channel are isolated from each other.

9. The indoor air purification process based on nano-micro-mist ionization according to claim 8, characterized in that, The qualified micro-particle stream is guided into the rectifier channel for co-current flow, forming an axial micro-particle stream; The axial particulate stream is then brought into parallel contact with the humidifying airflow, wherein the absolute moisture content of the humidifying airflow is lower than that of the axial particulate stream, causing the axial particulate stream to release water vapor and lowering its dew point by 1.5 to 4.0°C, forming a purified output stream, which is then released into the indoor space through a mist outlet.

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