Hazardous waste collection and treatment system and method

Abstract

The application discloses a hazardous waste collecting and processing system and method, belongs to the technical field of hazardous waste processing, and solves the problems of extreme working condition response lag caused by single-point pH monitoring failure, pH rebound caused by instantaneous emission compliance, and neutralization reaction interference caused by impurities. The method calculates the current waste pH value through real-time average calculation of multiple pH sensors in the conveying pipeline, generates a neutralizing agent instruction according to pH lower than 6.0 or higher than 8.0; pre-separates suspended solids by using a stepped sedimentation tank; switches to an emergency treatment tank when at least two sensors simultaneously monitor pH lower than 2.0 or higher than 12.0; and switches to a final outlet when the pH at the outlet of the neutralization reaction tank continuously reaches 6.0-8.0 for a dynamic time t seconds and the sediment concentration is less than or equal to 5%. The method is mainly used for safe and stable treatment of liquid hazardous waste.

Description

Technical Field

[0001] This invention relates to the field of hazardous waste treatment technology, specifically to a hazardous waste collection and treatment system and method. Background Technology

[0002] In the field of liquid hazardous waste treatment, there are significant technical bottlenecks in the centralized treatment of multi-source waste liquids (such as electroplating pickling solutions, dyeing and printing wastewater, and pharmaceutical organic waste liquids). Existing systems generally use a single pH sensor for acidity and alkalinity monitoring. When sensor drift or extreme waste liquids are introduced, the reliability of the monitoring data is severely reduced. For example, it is common for strong acid or strong alkali waste liquids to be injected without timely detection, which may lead to uncontrolled neutralization reactions or equipment corrosion. Although adding monitoring points can partially improve reliability, data conflicts from multiple sensors can easily lead to frequent false alarms, which in turn reduces operational stability.

[0003] The emission determination mechanism has significant flaws. Wastewater containing buffering agents often exhibits a slow pH rise after neutralization, but current technology relies solely on a single pH test to determine discharge, leading to some waste exceeding permissible pH levels during subsequent storage. Simultaneously, suspended impurities in hazardous waste (such as metal fragments and organic colloids) directly enter the neutralization tank, gradually depositing to form a slab layer. This sediment not only reduces the effective tank volume but also interferes with the reaction process, forcing periodic system shutdowns for cleaning and severely impacting continuous operation efficiency. The root cause lies in the failure to consider the interaction between the dynamic equilibrium of the reaction and sediment accumulation in the emission determination process.

[0004] Impurity separation in the pretreatment stage faces engineering challenges. Closed-loop pipelines struggle to integrate efficient separation equipment, while external separation units require excessive space and are ill-suited for compact treatment plant layouts. Unseparated suspended solids entering subsequent units reduce neutralization efficiency and accelerate sedimentation, creating a vicious cycle. Furthermore, fixed-parameter designs cannot adapt to dynamic conditions: insufficient neutralizer at high flow rates and the need for higher reaction intensities in heavy metal-containing wastewater, but static coefficients cannot be adjusted accordingly; fixed reaction times ignore changes in flow rate and tank volume, leading to over-reaction at low flow rates and incomplete reaction at high flow rates.

[0005] The aforementioned problems have long constrained the safety and stability of the processing system. Attempts to improve reliability by adding monitoring points have been hampered by malfunctions caused by data conflicts; external separation devices are difficult to implement due to space constraints; and the complexity of dynamic operating conditions makes it difficult to accurately adapt fixed parameter systems. These shortcomings collectively result in a lack of effective solutions for problems such as delayed response to extreme operating conditions, insufficient emission stability, and interference from impurities. Summary of the Invention

[0006] This invention provides a hazardous waste collection and treatment system and method, aiming to solve the safety risks caused by the failure of single-point pH monitoring in the treatment of liquid hazardous waste. When the mixing of multiple waste liquids causes a sudden change in pH, a single sensor cannot reliably identify extreme operating conditions (such as pH < 2.0 or > 12.0), which may lead to equipment corrosion or uncontrolled reaction. At the same time, instantaneous pH compliance during discharge cannot avoid the risk of pH rebound in waste liquids containing buffers, and impurities directly enter the reaction tank, causing precipitation and accumulation. Existing systems lack integrated pre-separation and multi-level emergency mechanisms, making it difficult to balance the requirements of monitoring reliability, reaction stability, and impurity control.

[0007] This paper addresses the issue of neutralizer addition deviation in the fixed-coefficient method within a nonlinear pH range. When the waste pH is below 4.0 or above 10.0, the required neutralizing agent dosage per unit pH change increases dramatically, but the linear calculation formula cannot adaptively compensate for this, leading to insufficient or excessive addition under strong acid / base conditions. Existing technologies lack a pH-dependent compensation strategy, resulting in agent waste or incomplete neutralization.

[0008] This addresses the lack of coordinated handling of sensor failures and extreme operating conditions. The existing system only triggers alarms for sensor drift (such as continuous data deviation) without linking emergency actions; it still responds according to the standard procedure when extreme pH values ​​occur, delaying timely intervention. Furthermore, the lack of a system degradation mechanism in the event of multiple sensor failures may perpetuate erroneous operating conditions.

[0009] This addresses the issue of fixed parameters failing to adapt to dynamic operating conditions. At high flow rates (>100 L / min), the original neutralization coefficient leads to insufficient addition; waste containing heavy metals requires higher neutralization strength, but the static coefficient does not differentiate between these requirements. The fixed reaction time ignores changes in flow rate and tank volume, resulting in over-reaction at low flow rates and under-reaction at high flow rates.

[0010] Addressing the secondary risks associated with pathway switching. Current technologies do not detect pH changes within the reaction vessel when switching emergency pathways; switching under drastic fluctuations may exacerbate reaction imbalances. Emission pathway switching only verifies pH values, neglecting the risk of blockage due to excessive sediment (>5%). Furthermore, the lack of automated corrective measures after timeouts makes manual intervention inefficient.

[0011] The solutions address endpoint misjudgments and delayed emergency responses. High-frequency dynamic pH signals (such as ΔpH / Δt) are not used for emission determination; emissions are only determined after a single instance of compliance. Extreme operating condition responses rely on single sensor thresholds, resulting in a high false alarm rate. Emission conditions are not incorporated into sediment concentration verification, leading to insufficient control of physical risks.

[0012] This addresses the issue of chain reactions triggered by component mutations. When waste liquid is mixed with unknown components (such as organic solvents), conventional neutralization processes may fail. Current technologies lack mutation recognition mechanisms; even when the mutation rate of near-infrared characteristic peaks exceeds 30% or the spectrum mismatches, the original process continues, leading to the collapse of the reaction system.

[0013] This addresses the issue of insufficient deep purification after mutation. Buffering only stabilizes pH and does not remove substances such as colloids / enzyme inhibitors introduced by the mutation. Conventional precipitation has low separation efficiency for particles <5μm, and residual impurities interfere with subsequent neutralization. Existing methods lack an integrated approach combining targeted removal with magnetic carriers and multi-stage sedimentation.

[0014] This addresses the issue of unstable separation efficiency in emulsified hazardous waste. Chemical demulsifiers exhibit poor adaptability and lag in response to changes in oil droplet size (τ) or conductivity (σ). Static temperature control and electric field parameter settings cannot optimize demulsification kinetics in real time, leading to incomplete oil-water separation.

[0015] This addresses the problem of low efficiency in the step-by-step treatment of multiple pollutants. Free oil droplets and heavy metal ions require separate treatment, which is complex and generates secondary sludge. Existing adsorption materials have limited functionality and cannot simultaneously remove hydrophobic and metalophilic pollutants, making carrier regeneration and resource recovery difficult.

[0016] To achieve these and other advantages according to the present invention, a hazardous waste collection and treatment system is provided, comprising:

[0017] Collection device for receiving liquid hazardous waste;

[0018] The pipeline connects to the collection device and is used to transport liquid hazardous waste;

[0019] Multiple pH sensors are installed in the delivery pipeline to monitor the pH value of liquid hazardous waste in real time;

[0020] The controller connects to multiple pH sensors to calculate the average pH value measured by the multiple pH sensors as the current pH value of the waste, and generates instructions on the amount of neutralizer to be added based on whether the current pH value of the waste is below 6.0 or above 8.0.

[0021] A neutralizer adding device, connected to a controller, is used to add alkaline or acidic neutralizer to the delivery pipeline according to the neutralizer adding amount instruction;

[0022] The neutralization reaction vessel, connected downstream of the delivery pipeline, is used to receive liquid hazardous waste from the delivery pipeline and alkaline or acidic neutralizing agent added by the neutralizing agent adding device, and to mix and neutralize it.

[0023] Emergency response tank;

[0024] The three-way valve has its inlet connected to the outlet of the neutralization reaction tank, its first outlet connected to the inlet of the emergency treatment tank, and its second outlet connected to the final outlet of the system.

[0025] A near-infrared spectrometer, embedded in the delivery pipeline, is used to scan the characteristic absorption peaks of liquid hazardous waste in real time, providing component data for the controller to generate neutralizing agent instructions;

[0026] A stepped sedimentation tank is installed between the conveying pipeline and the neutralization reaction tank to pre-separate suspended solid impurities, ensuring that the waste entering the neutralization reaction tank meets the reaction conditions.

[0027] The controller is connected to a three-way valve. When at least two of the multiple pH sensors simultaneously detect a pH value below 2.0 or above 12.0, the controller switches the three-way valve to the first outlet. When the final pH sensor at the outlet of the neutralization reaction tank detects that the waste pH value is in the range of 6.0 to 8.0 and remains within a dynamic time t seconds, the controller switches the three-way valve to the second outlet.

[0028] Preferably, in the hazardous waste collection and treatment system of the present invention, the controller generates a neutralizing agent addition instruction based on the current pH value of the waste, specifically as follows:

[0029] When the current pH value of the waste is below 6.0, the amount of alkaline neutralizer to be added is determined according to the formula: Amount of alkaline neutralizer added = K1 × (6.0 - current pH value of waste) × θ1;

[0030] When the current pH value of the waste is higher than 8.0, the amount of acid neutralizer to be added is determined according to the formula: Acid neutralizer addition amount = K2 × (current waste pH value - 8.0) × θ2;

[0031] Wherein, K1 is the preset addition coefficient of alkaline neutralizer with a value range of 1.0 to 5.0 L / (min·pH), K2 is the preset addition coefficient of acidic neutralizer with a value range of 1.0 to 5.0 L / (min·pH), and θ1 and θ2 are both pH compensation factors, determined by looking up a table.

[0032] Preferably, in the hazardous waste collection and treatment system of the present invention, the controller is further equipped with an emergency control module, which performs the following operations:

[0033] The deviation between the pH sensor's monitored value and the average value is compared in real time. If the value of any sensor deviates from the average value by more than ±2.0 for three consecutive times, the sensor is marked as faulty and an alarm is triggered.

[0034] When the current waste pH value is below 2.0 or above 12.0, regardless of whether a neutralizer addition instruction is generated, immediately control the three-way valve to switch to the first outlet and start the circulating cooling system of the emergency treatment tank;

[0035] When the number of faulty sensors exceeds 50% of the total, the automatic neutralization process is shut down and switched to manual intervention mode.

[0036] Preferably, in the hazardous waste collection and treatment system of the present invention, the controller is further configured with a dynamic adjustment module, which includes:

[0037] Neutralizing agent optimization unit: Based on real-time data Q from the flow sensor in the delivery pipeline and the waste composition database, dynamically adjusts K1 and K2 to meet the following conditions:

[0038] When Q > 100 L / min, the values ​​of K1 and K2 are reduced to 0.8 times the original coefficients;

[0039] When the waste composition contains heavy metal ions, the basic values ​​of K1 and K2 increase by 30%;

[0040] Delay Adaptive Unit: The dynamic time t is calculated by the formula t=V / (Q×C), where V is the effective volume of the neutralization reaction vessel, C is the reaction sufficiency constant, which takes a value of 0.5-1.5, and t is automatically limited to the range of 60-120 seconds.

[0041] Preferably, in the hazardous waste collection and treatment system of the present invention, the switching action of the three-way valve needs to be confirmed by a safety verification module, including:

[0042] (1) Before switching to the first outlet, the controller retrieves the pH change rate data of the neutralization reaction tank in the last 10 seconds. If the absolute value of the change rate exceeds 0.5 pH / second, the switching is delayed until the change rate drops below 0.2 pH / second.

[0043] (2) Before switching to the second exit, two conditions must be met in sequence:

[0044] Condition 1: The final pH sensor reading remains within the range of 6.0-8.0 for t seconds;

[0045] Condition 2: The ultrasonic detector reading of the sediment at the bottom of the neutralization reaction vessel is ≤5% of the threshold.

[0046] Timeout mechanism: If condition 2 is not met within 60 seconds after condition 1 is met, then execute:

[0047] Start the stirrer at the bottom of the neutralization reaction vessel at 30-50 rpm for 20 seconds;

[0048] Anionic polyacrylamide flocculant was injected into the neutralization reaction vessel at a rate of 0.05-0.1 ppm of the waste volume inside the vessel.

[0049] After standing for 10 seconds, retest the concentration of the precipitate.

[0050] If the concentration is still >5%, switch to the first outlet and trigger the precipitate over-limit alarm;

[0051] (3) An operation log is automatically generated after each switch, recording the switch time, trigger parameters and sensor status.

[0052] The present invention also provides a method for collecting and treating hazardous waste, comprising the following steps:

[0053] (a) The pH value of the liquid hazardous waste is collected in real time by multiple pH sensors installed in the delivery pipeline, and the controller calculates the average value as the current pH value of the waste.

[0054] (b) If the current waste pH value is below 6.0 or above 8.0, dynamically select the K1 or K2 coefficient according to the flow rate Q in the conveying pipeline, calculate the amount of neutralizer to be added according to the formula, and add the neutralizer to the conveying pipeline;

[0055] (c) Install a high-frequency pH sensor at the outlet of the neutralization reaction tank, with a sampling frequency ≥10Hz, to monitor the instantaneous pH value and change rate ΔpH / Δt of the waste after the reaction;

[0056] (d) When at least two pH sensors in the delivery pipeline simultaneously detect pH < 2.0 or > 12.0, immediately switch the three-way valve to the emergency treatment tank; if the absolute value of ΔpH / Δt is > 0.5pH / second and the instantaneous pH value deviates from the range of 6.0-8.0, start the emergency diversion simultaneously;

[0057] (e) When the pH value at the outlet of the neutralization reaction tank remains in the range of 6.0-8.0 for a dynamic time t seconds, and the ultrasonic detector confirms that the concentration of precipitate at the bottom of the neutralization reaction tank is <5%, switch the three-way valve to the final outlet.

[0058] Preferably, in the hazardous waste collection and treatment method of the present invention, the following step is added before step (b):

[0059] (b1) The liquid hazardous waste is scanned in real time by a near-infrared spectrometer embedded in the delivery pipeline to obtain the characteristic absorption peak intensity value S at the target wavelength λ. t λ is preset to a specific wavelength in the range of 500-1800nm ​​according to the type of hazardous waste;

[0060] (b2) The controller calculates the critical peak mutation rate ΔS = |S t -S t-1 | / S t-1 ×100%, S t-1 This represents the intensity value of the characteristic absorption peak from the previous sampling period, with a sampling period of 1 second.

[0061] If ΔS > 30% or the current absorption peak does not match the hazardous waste characteristic spectrum in the pre-stored database, it is determined to be a compositional mutation.

[0062] (b3) Execute when components change abruptly:

[0063] Reduce the neutralizer addition rate to 50% of the current flow rate Q;

[0064] Add phosphate buffer solution with pH 7.0 to the delivery line, the amount added is V. buffer =0.2×Q×ΔS / 100;

[0065] After a delay of 10-20 seconds, repeat step (b) and temporarily set the coefficients of K1 and K2 to 3.0 L / (min·pH).

[0066] Preferably, in the hazardous waste collection and treatment method of the present invention, after step (b3), the following step is added:

[0067] (b4) Immobilized phosphatase was implanted in the delivery line 0.5-1.0m downstream of the buffer injection point. The immobilized phosphatase was loaded on the surface of Fe3O4 magnetic nanoparticle carrier with a particle size of 50-100nm. The carrier filling density was 1-5g / L, and the working temperature was maintained at 25-40℃.

[0068] (b5) When Δ S When the concentration is ≤10% for 30 seconds, the abrupt change in composition is determined to be resolved, and the magnetic separation device is activated with a magnetic field strength ≥0.5T to adsorb and remove the nanoparticle carrier.

[0069] (b6) The waste after magnetic separation enters a stepped sedimentation tank for three-stage settling:

[0070] Primary sedimentation: Let stand for 5 minutes to remove suspended solids with a particle size >50μm;

[0071] Secondary sedimentation: Add 0.1 ppm cationic polyacrylamide flocculant, let stand for 3 minutes, and remove particles with a diameter of 5-50 μm;

[0072] Three-stage sedimentation: High-frequency ultrasonic dispersion of colloid at 20kHz and 100±10W is applied, and the particles <5μm are removed after standing for 2 minutes.

[0073] Preferably, in the hazardous waste collection and treatment method of the present invention, a demulsification enhancement step is added before the three-stage settling in step (b6):

[0074] Electrochemical demulsification pretreatment is performed on the waste after magnetic separation:

[0075] A pulsed electric field device is installed at the inlet of the stepped sedimentation tank, with an electrode spacing of 10-20 cm, and an applied amplitude of [value missing]. V p =2.0× Frequency f=50 / t A square wave pulse, wherein: s The real-time conductivity of the waste was obtained using an online conductivity meter. t The average particle size of the oil droplets is monitored in real time using a laser particle size analyzer.

[0076] Simultaneously regulate the waste temperature T, if C o ≥0.01%, T=40+5×ln(C o )℃, if C o <0.01%, T=40℃, where C o The concentration of the oil phase was calculated by inversion from the characteristic peak at 1700 nm using a near-infrared spectrometer, and T was automatically limited to the range of 25-40℃.

[0077] When the rate of change of dielectric constant Δ e / Δ t When the rate is ≤0.1% / s for 10 seconds, the demulsification is considered complete.

[0078] Preferably, in the hazardous waste collection and treatment method of the present invention, a dual-functional magnetic carrier adsorption is integrated in the stepped sedimentation tank after demulsification:

[0079] The magnetic nanoparticle carrier was surface-modified with bifunctional components, wherein the hydrophobic end was octyltriethoxysilane (C8H). 17 -Si-(OC2H5)3) modification layer, 5-10nm thick; metalophilic end is a dithiocarbamate chelating group (-N(CSS-)) grafted onto the outside of the hydrophobic layer;

[0080] When the rate of change of dielectric constant indicates that demulsification is complete, a bifunctional carrier is injected into the primary settling zone of the sedimentation tank at a volume of 0.1-0.5 vol% of the waste volume.

[0081] A rotating magnetic field with a strength of 0.3-0.8T and a rotation speed of 10-30rpm is applied synchronously to drive the carrier to perform the operation. The hydrophobic end adsorbs free oil droplets with a contact angle >150°; the metalophilic end complexes cadmium ions, lead ions, and mercury ions to form insoluble sulfides.

[0082] After sedimentation, the carrier is recovered by a magnetic separation device, and heavy metals are desorbed with 0.1M dilute hydrochloric acid. The desorbed liquid enters the electrodeposition recovery unit.

[0083] The present invention has at least the following beneficial effects:

[0084] 1. Monitoring reliability is improved by calculating the average values ​​of multiple pH sensors in the delivery pipeline, reducing the risk of single-point failure; a dual-threshold (2.0 / 12.0) emergency mechanism ensures switching to the emergency tank within 30 seconds under extreme conditions. A stepped sedimentation tank pre-separates suspended solids, reducing sediment formation in the reaction tank. Final discharge is verified by both pH duration (t seconds) and sediment concentration (≤5%) to prevent rebound after instantaneous compliance. The system integrates monitoring, separation, emergency response, and discharge into a closed loop, enhancing treatment safety and stability.

[0085] Second, the dosage is dynamically adjusted using pH-dependent compensation factors (θ1, θ2). For example, when pH < 3.0, θ1 = 30.0, precisely matching the nonlinear requirements of strong acid environments. A lookup table method is used to solidify the logic of five compensation intervals, avoiding complex calculation delays. Preset coefficients K1 and K2 have adjustable ranges (1.0-5.0 L / (min·pH)) to adapt to different neutralizing agent reaction efficiencies, reducing reagent deviation rates.

[0086] III. A fault diagnosis mechanism that detects three consecutive deviations from the mean ±2.0, enabling early identification and alarm of sensor drift. Extreme pH (<2.0 or >12.0) triggers forced switching of the three-way valve and activation of the cooling system, with a response delay of less than 5 seconds. When more than 50% of the sensors are faulty, the system automatically switches to manual mode to prevent inaccurate operation.

[0087] IV. When the flow rate is >100L / min, K1 and K2 are reduced to 0.8 times to match the requirements of high flow rate conditions; the triggering coefficient of heavy metal ions is increased by 30% to enhance the neutralization strength. The reaction time t is dynamically calculated based on the tank volume V and the flow rate Q (t=V / (Q×C)), and the C value (0.5-1.5) is adjustable to adapt to different waste reaction kinetics. The t limit is 60-120 seconds to ensure the sufficiency of the reaction.

[0088] 5. Before switching to the emergency path, verify that the pH change rate is ≤0.2pH / second to prevent the reaction imbalance from worsening. The emission path must sequentially meet the following requirements: pH continuously meets the standard for t seconds and precipitate ≤5%. The timeout mechanism automatically starts stirring (30-50rpm) and flocculant injection (0.05-0.1ppm). If the secondary detection fails, switch to the emergency path. The operation log records the switching parameters to support fault tracing.

[0089] VI. A high-frequency pH sensor (≥10Hz) captures instantaneous fluctuations, avoiding false judgments from single detections. Dual sensors simultaneously trigger an immediate emergency switch when pH <2.0 or >12.0, and collaborative judgment with ΔpH / Δt > 0.5pH / second improves response reliability. Discharge requires two conditions: pH continuously meeting the standard for t seconds and precipitate <5%, reducing physicochemical risks.

[0090] VII. A component mutation is determined when the near-infrared characteristic peak mutation rate ΔS > 30% or spectral mismatch occurs. Buffer solution (pH=7.0) is prepared according to V... buffer =0.2×Q×ΔS / 100 is injected into the stable system, and the neutralizing agent rate is reduced to 50% to avoid side reactions. After a delay of 10-20 seconds, neutralization is restarted with a temporary coefficient of 3.0 L / (min·pH) to ensure a safe transition under abrupt changes.

[0091] 8. Immobilized phosphatase carrier (Fe3O4, 50-100nm) degrades organophosphorus pollutants, and enzyme recovery is achieved through magnetic separation (≥0.5T). Three-stage sedimentation and classification removes impurities: the first stage removes particles >50μm, the second stage uses flocculant (0.1ppm) to remove particles 5-50μm, and the third stage uses ultrasound (20kHz, 100W) to disperse colloids <5μm, reducing turbidity to below 1NTU.

[0092] IX. Adaptive Pulse Electric Field Parameters: Amplitude V p =2.0× Matching conductivity, frequency f=50 / τ matching oil droplet size. Temperature T according to oil phase concentration C. o Dynamic regulation: C o When ≥0.01%, T = 40 + 5 × ln(C) o At ℃, the demulsification kinetics were optimized. The demulsification endpoint was objectively determined by a dielectric constant change rate ≤0.1% / s for 10 seconds.

[0093] 10. Dual-functional carrier operates simultaneously: An octylsilane hydrophobic layer (5-10 nm) adsorbs oil droplets (contact angle >150°), while dithiocarbamate complexes cadmium, lead, and mercury ions to form sulfides. A rotating magnetic field (0.3-0.8 T, 10-30 rpm) enhances carrier-contaminant contact. 0.1 M HCl desorbs heavy metals, and the desorbate is electrowinning recovered for resource utilization. The carrier injection volume is 0.1-0.5 vol% to ensure economic efficiency.

[0094] Other advantages, objectives and features of the present invention will become apparent in part from the following description, and in part from those skilled in the art through study and practice of the invention. Detailed Implementation

[0095] The present invention will now be described in further detail so that those skilled in the art can implement it based on the description.

[0096] It should be understood that terms such as “having,” “comprising,” and “including” as used herein do not exclude the presence or addition of one or more other elements or combinations thereof.

[0097] According to one embodiment of the present invention, a hazardous waste collection and treatment system is provided, comprising: a collection device for receiving liquid hazardous waste;

[0098] The pipeline connects to the collection device and is used to transport liquid hazardous waste;

[0099] Multiple pH sensors are installed in the delivery pipeline to monitor the pH value of liquid hazardous waste in real time;

[0100] The controller connects to multiple pH sensors to calculate the average pH value measured by the multiple pH sensors as the current pH value of the waste, and generates instructions on the amount of neutralizer to be added based on whether the current pH value of the waste is below 6.0 or above 8.0.

[0101] A neutralizer adding device, connected to a controller, is used to add alkaline or acidic neutralizer to the delivery pipeline according to the neutralizer adding amount instruction;

[0102] The neutralization reaction vessel, connected downstream of the delivery pipeline, is used to receive liquid hazardous waste from the delivery pipeline and alkaline or acidic neutralizing agent added by the neutralizing agent adding device, and to mix and neutralize it.

[0103] Emergency response tank;

[0104] The three-way valve has its inlet connected to the outlet of the neutralization reaction tank, its first outlet connected to the inlet of the emergency treatment tank, and its second outlet connected to the final outlet of the system.

[0105] A near-infrared spectrometer, embedded in the delivery pipeline, is used to scan the characteristic absorption peaks of liquid hazardous waste in real time, providing component data for the controller to generate neutralizing agent instructions;

[0106] A stepped sedimentation tank is installed between the conveying pipeline and the neutralization reaction tank to pre-separate suspended solid impurities, ensuring that the waste entering the neutralization reaction tank meets the reaction conditions.

[0107] The controller is connected to a three-way valve. When at least two of the multiple pH sensors simultaneously detect a pH value below 2.0 or above 12.0, the controller switches the three-way valve to the first outlet. When the final pH sensor at the outlet of the neutralization reaction tank detects that the waste pH value is in the range of 6.0 to 8.0 and remains within a dynamic time t seconds, the controller switches the three-way valve to the second outlet.

[0108] Existing liquid hazardous waste treatment systems typically use a single pH sensor to monitor acidity and alkalinity, triggering the addition of neutralizing agents based on a fixed threshold. Such systems have low tolerance for sensor failure; when faced with sudden pH changes (such as a sudden injection of strong acid or alkali), misjudgments may occur due to the failure of this single monitoring point. Furthermore, current technologies lack rapid emergency diversion mechanisms for extreme pH levels (below 2.0 or above 12.0), and the determination of the neutralization reaction endpoint relies solely on a single pH measurement, failing to consider reaction stability and precipitate interference.

[0109] In this embodiment, the collection device can be a receiving tank with a sealed cover; the conveying pipeline can be a corrosion-resistant polyethylene pipe with an inner diameter range of 50-100mm; the pH sensor can be a glass electrode type, with at least three equidistantly arranged along the pipeline axis; the controller can be an industrial PLC with a built-in mean calculation algorithm; the neutralizing agent addition device can be equipped with a metering pump, with its outlet connected to the middle section of the conveying pipeline; the neutralization reaction tank can be designed as a vertical container with a stirring paddle, with an effective volume of 1-5m³; the emergency treatment tank can be equipped with a circulating cooling coil; the three-way valve can be an electric ball valve; the near-infrared spectrometer can be installed on the straight section of the conveying pipeline, with a scanning wavelength range covering 500-1800nm; the stepped sedimentation tank can be designed as a three-stage series sedimentation tank. The connection relationship of each component is as follows: the outlet of the collection device is connected to the inlet of the conveying pipeline, the outlet of the conveying pipeline is connected to the inlet of the neutralization reaction tank via the stepped sedimentation tank, and the outlet of the neutralization reaction tank is connected to the inlet of the three-way valve.

[0110] In this embodiment, a collection device receives liquid hazardous waste and transports it to subsequent units via a conveying pipeline. Multiple pH sensors are installed inside the conveying pipeline to monitor the pH value of the flowing waste in real time. A controller connects to all pH sensors and calculates the average pH value as the current waste pH. If this average value is below 6.0 or above 8.0, the controller generates a neutralizer addition command. The neutralizer addition device injects alkaline or acidic neutralizer into the conveying pipeline according to the command. The waste and neutralizer then enter a neutralization reaction tank for mixing and reaction. A near-infrared spectrometer is embedded in the conveying pipeline to scan the characteristic absorption peaks of the waste in real time, providing compositional data for the controller to generate the neutralizer command. A stepped sedimentation tank is installed between the conveying pipeline and the neutralization reaction tank to pre-separate suspended impurities, ensuring that the waste entering the neutralization reaction tank meets the reaction conditions. The outlet of the neutralization reaction tank is connected to the inlet of a three-way valve; the first outlet of the three-way valve leads to an emergency treatment tank, and the second outlet leads to the system's final discharge port. When at least two of the multiple pH sensors simultaneously detect a pH value below 2.0 or above 12.0, the controller immediately switches the three-way valve to the first outlet, allowing waste to enter the emergency treatment tank. When the final pH sensor at the neutralization tank outlet detects a pH value that remains within the dynamic range of 6.0 to 8.0 for a dynamic time t seconds, the controller switches the three-way valve to the second outlet for discharge.

[0111] The system in this embodiment reduces the risk of single-point monitoring failure through multi-sensor mean calculation; improves the response speed to extreme waste liquids by using a dual-threshold (2.0 / 12.0) emergency mechanism; reduces the interference of impurities on the neutralization reaction through step-sedimentation tank pretreatment; ensures that the pH value of the discharged waste is stable and meets the standard by combining the endpoint determination condition of continuous dynamic time t seconds; and provides basic data for component monitoring through real-time scanning of near-infrared spectrometer.

[0112] According to another embodiment of the present invention, a hazardous waste collection and treatment system is provided, wherein the controller generates a neutralizing agent addition instruction based on the current pH value of the waste, specifically as follows:

[0113] When the current pH value of the waste is below 6.0, the amount of alkaline neutralizer to be added is determined according to the formula: Amount of alkaline neutralizer added = K1 × (6.0 - current pH value of waste) × θ1;

[0114] When the current pH value of the waste is higher than 8.0, the amount of acid neutralizer to be added is determined according to the formula: Acid neutralizer addition amount = K2 × (current waste pH value - 8.0) × θ2;

[0115] Wherein, K1 is the preset addition coefficient of alkaline neutralizer with a value range of 1.0 to 5.0 L / (min·pH), K2 is the preset addition coefficient of acidic neutralizer with a value range of 1.0 to 5.0 L / (min·pH), and θ1 and θ2 are both pH compensation factors, determined by looking up a table.

[0116] Current systems typically calculate the amount of neutralizer to add by multiplying a fixed coefficient by the pH deviation value, without considering the differences in reaction efficiency across different pH ranges. For example, when the pH is below 4.0, the amount of neutralizer required per unit pH change increases significantly, but current methods do not compensate for this non-linear characteristic, which may lead to insufficient neutralization or waste of reagents.

[0117] In this embodiment, the controller can be configured with a data storage module to pre-store a pH compensation factor lookup table. The base values ​​of K1 and K2 can be set via a human-machine interface, allowing operators to adjust them within a range of 1.0 to 5.0 liters per minute per pH unit. The compensation factor assignment logic is embedded in the control algorithm: for example, when pH is detected at 3.5, θ1=10.0 is automatically called, and when pH is detected at 11.5, θ2=30.0 is called. The neutralizer addition device can receive a command signal with the compensation factor and perform the addition action by adjusting the metering pump stroke. Example implementation: When pH=4.2 is detected, θ1 is 3.0. If K1 is set to 2.0 liters per minute per pH unit, the addition amount is 2.0 × (6.0 - 4.2) × 3.0 = 10.8 liters per minute.

[0118] In this embodiment, the controller executes a specific algorithm when generating a neutralizer addition command. When the current waste pH value obtained from real-time calculation is below 6.0, the amount of alkaline neutralizer to be added is calculated using a formula: the amount of alkaline neutralizer added equals a preset coefficient K1 multiplied by the difference between 6.0 and the current pH value, and then multiplied by a compensation factor θ1. The value range of K1 is set to 1.0 to 5.0 liters per minute per pH unit. When the current waste pH value is above 8.0, the amount of acidic neutralizer to be added is calculated using a formula: the amount of acidic neutralizer added equals a preset coefficient K2 multiplied by the difference between the current pH value and 8.0, and then multiplied by a compensation factor θ2. The value range of K2 is also 1.0 to 5.0 liters per minute per pH unit. The compensation factors θ1 and θ2 are determined by looking up a table: for θ1, it is 1.0 when the pH is in the range of 5.0 to 6.0, 3.0 when it is in the range of 4.0 to 5.0, 10.0 when it is in the range of 3.0 to 4.0, and 30.0 when it is below 3.0; for θ2, it is 1.0 when the pH is in the range of 8.0 to 9.0, 3.0 when it is in the range of 9.0 to 10.0, 10.0 when it is in the range of 10.0 to 11.0, and 30.0 when it is above 11.0.

[0119] The system in this embodiment introduces a pH range-dependent compensation factor to more accurately match the nonlinear neutralization characteristics under strong acid and strong alkali environments; a lookup table method is used to achieve differentiated control in different pH ranges, reducing the deviation in neutralizer dosage under extreme pH conditions; and the adjustable range of preset coefficients K1 and K2 provides process adaptability.

[0120] According to another embodiment of the present invention, a hazardous waste collection and treatment system is provided, wherein the controller is further configured with an emergency control module, which performs the following operations:

[0121] The deviation between the pH sensor's monitored value and the average value is compared in real time. If the value of any sensor deviates from the average value by more than ±2.0 for three consecutive times, the sensor is marked as faulty and an alarm is triggered.

[0122] When the current waste pH value is below 2.0 or above 12.0, regardless of whether a neutralizer addition instruction is generated, immediately control the three-way valve to switch to the first outlet and start the circulating cooling system of the emergency treatment tank;

[0123] When the number of faulty sensors exceeds 50% of the total, the automatic neutralization process is shut down and switched to manual intervention mode.

[0124] Existing systems lack effective diagnostic mechanisms for abnormal pH sensor data, making them prone to malfunctions when a single sensor drifts or fails. Furthermore, current emergency responses rely solely on preset thresholds and lack a coordinated strategy for handling sensor malfunctions and extreme pH conditions; delayed manual intervention may exacerbate the risk of accidents.

[0125] In this implementation, the emergency control module can be integrated into the controller software, containing three independent execution threads: a deviation comparison thread performs data comparison every 5 seconds, using a sliding window to record the three most recent monitoring values; an extreme pH response thread sets dual threshold trigger conditions of 2.0 and 12.0, sending the highest priority switching command to the three-way valve upon triggering; and a fault statistics thread updates the list of faulty sensors in real time, activating the mode switching program when the ratio of the number of faults to the total number of sensors exceeds 0.5. An alarm device can be connected to an audible and visual alarm, and the manual intervention mode can be switched to manual control panel control. Implementation example: The system is configured with 6 pH sensors. When 4 sensors are marked as faulty, the metering pump power is automatically turned off and the red warning light on the control panel is illuminated.

[0126] In this embodiment, the emergency control module configured in the controller executes a continuous monitoring process. First, it compares the deviation between the pH sensor readings and the calculated average value in real time. If any sensor's readings deviate from the average value by more than ±2.0 for three consecutive times, the module marks the sensor as faulty and triggers an alarm signal. Second, when the real-time calculated current waste pH value is below 2.0 or above 12.0, regardless of whether a neutralizer addition command is generated, it immediately controls the three-way valve to switch to the emergency treatment tank outlet and simultaneously starts the circulating cooling system of the emergency treatment tank. Finally, it counts the number of all faulty sensors. When the number of faulty sensors exceeds 50% of the total number of sensors, it automatically shuts down the neutralizer addition process and switches to manual intervention mode.

[0127] The system in this embodiment achieves early identification of sensor faults through continuous deviation analysis; establishes a forced switching mechanism for extreme pH conditions; sets a fault quantity threshold to ensure the safe exit of the system when monitoring is inaccurate; and provides timely warnings of abnormal states through an alarm function.

[0128] According to another embodiment of the present invention, a hazardous waste collection and treatment system is provided, wherein the controller is further configured with a dynamic adjustment module, the module comprising:

[0129] Neutralizing agent optimization unit: Based on real-time data Q from the flow sensor in the delivery pipeline and the waste composition database, dynamically adjusts K1 and K2 to meet the following conditions:

[0130] When Q > 100 L / min, the values ​​of K1 and K2 are reduced to 0.8 times the original coefficients;

[0131] When the waste composition contains heavy metal ions, the basic values ​​of K1 and K2 increase by 30%;

[0132] Delay Adaptive Unit: The dynamic time t is calculated by the formula t=V / (Q×C), where V is the effective volume of the neutralization reaction vessel, C is the reaction sufficiency constant, which takes a value of 0.5-1.5, and t is automatically limited to the range of 60-120 seconds.

[0133] Existing systems use fixed neutralizer addition coefficients and reaction time parameters, which cannot adapt to fluctuations in flow rate or changes in waste composition. For example, under high flow rate conditions, the required neutralizer dosage for the same pH deviation increases, but the fixed coefficients will result in insufficient addition; waste containing heavy metals requires a longer reaction time, but the static setpoints cannot meet such needs.

[0134] In this embodiment, the dynamic adjustment module can be integrated into the core processing unit of the controller. An electromagnetic flow meter can be selected as the flow sensor and installed in the middle section of the delivery pipeline. The waste composition database can store historical detection data or receive near-infrared spectral analysis results in real time. The default value of the reaction sufficiency constant C can be set to 1.0, allowing the operator to manually adjust it within the range of 0.5 to 1.5. Implementation example: When the detected flow rate is 120 liters per minute, the system automatically reduces the K1 coefficient from its original value of 3.0 to 2.4; if copper ions are detected simultaneously, the basic K1 value increases by 30% to 3.12. For a reaction vessel with an effective volume of 2 cubic meters, at a flow rate of 100 liters per minute and C set to 1.0, the calculated t = 2000 / (100 × 1) = 20 seconds is automatically adjusted to 60 seconds because it is below the lower limit of 60 seconds.

[0135] In this embodiment, the dynamic adjustment module configured in the controller includes a neutralizer optimization unit and a time-adaptive unit. The neutralizer optimization unit acquires real-time flow sensor data Q from the delivery pipeline. When the flow rate exceeds 100 liters per minute, it adjusts the neutralizer addition coefficients K1 and K2 to 0.8 times their original set values. Simultaneously, it accesses the waste composition database; if heavy metal ions are detected in the waste, the base values ​​of K1 and K2 are increased by 30%. The time-adaptive unit calculates the dynamic time t according to the formula t = V divided by Q multiplied by C, where V is the effective volume of the neutralization reaction vessel, and C is the reaction sufficiency constant, ranging from 0.5 to 1.5. The calculated t value is automatically limited to a range of 60 to 120 seconds.

[0136] The system in this embodiment dynamically adjusts the neutralizer addition ratio based on flow rate changes to avoid insufficient neutralization under high flow rate conditions; it automatically increases the neutralization intensity for waste containing heavy metals; and it dynamically adjusts the reaction time through volume-flow correlation calculations to ensure the reaction completion rate under different operating conditions.

[0137] According to another embodiment of the present invention, a hazardous waste collection and treatment system is provided, wherein the switching action of a three-way valve needs to be confirmed by a safety verification module, including:

[0138] (1) Before switching to the first outlet, the controller retrieves the pH change rate data of the neutralization reaction tank in the last 10 seconds. If the absolute value of the change rate exceeds 0.5 pH / second, the switching is delayed until the change rate drops below 0.2 pH / second.

[0139] (2) Before switching to the second exit, two conditions must be met in sequence:

[0140] Condition 1: The final pH sensor reading remains within the range of 6.0-8.0 for t seconds;

[0141] Condition 2: The ultrasonic detector reading of the sediment at the bottom of the neutralization reaction vessel is ≤5% of the threshold.

[0142] Timeout mechanism: If condition 2 is not met within 60 seconds after condition 1 is met, then execute:

[0143] Start the stirrer at the bottom of the neutralization reaction vessel at 30-50 rpm for 20 seconds;

[0144] Anionic polyacrylamide flocculant was injected into the neutralization reaction vessel at a rate of 0.05-0.1 ppm of the waste volume inside the vessel.

[0145] After standing for 10 seconds, retest the concentration of the precipitate.

[0146] If the concentration is still >5%, switch to the first outlet and trigger the precipitate over-limit alarm;

[0147] (3) An operation log is automatically generated after each switch, recording the switch time, trigger parameters and sensor status.

[0148] Existing systems typically rely on a single pH condition when switching emission paths, without considering reaction stability and the risk of sediment accumulation. For example, switching directly when the pH in the neutralization tank fluctuates drastically may result in the discharge of unreacted waste; discharge when sediment at the bottom of the tank exceeds a safety threshold can lead to pipe blockage or secondary pollution.

[0149] In this embodiment, the safety verification module can be integrated into the controller, containing three subroutines: a rate of change analysis subroutine calculates the ΔpH / Δt value per second; a condition monitoring subroutine continuously compares pH data with precipitate concentration; and a timeout handling subroutine controls the start / stop of the agitator and the injection of flocculant. The precipitate detector can be an ultrasonic thickness sensor, installed at the center of the tank bottom. Implementation example: When the detected pH change rate reaches 0.6 pH per second, a delay is applied to the switching process, which is executed after the rate drops to 0.15 pH per second. If the pH remains within the acceptable range at t=80 seconds but the precipitate concentration is 8%, the system starts agitation and injects 0.08 ppm of flocculant; if the concentration is still 6% upon secondary detection, the system switches to the emergency outlet. The log can be recorded as "2025-07-10 14:30: Switching to the second outlet failed, precipitate concentration 6%, sensors S1-S3 normal".

[0150] In this embodiment, the switching action of the three-way valve needs to be confirmed by the safety verification module. Before switching to the first outlet, the controller retrieves the pH change rate data of the neutralization reaction tank for the most recent 10 seconds. If the absolute value of the change rate exceeds 0.5 pH per second, the switching is delayed until the change rate drops below 0.2 pH per second. Before switching to the second outlet, two conditions must be met sequentially: Condition 1 requires the final pH sensor monitoring value to remain within the range of 6.0 to 8.0 for a continuous dynamic time t seconds; Condition 2 requires the ultrasonic detector reading of the sediment at the bottom of the tank to not exceed the threshold of 5%. If Condition 2 is not met within 60 seconds after Condition 1 is met, the timeout mechanism is activated: first, the bottom agitator is turned on and runs at a speed of 30 to 50 revolutions per minute for 20 seconds; then, 0.05 to 0.1 ppm of anionic polyacrylamide flocculant is injected; after standing for 10 seconds, the sediment concentration is re-detected. If the concentration is still greater than 5%, the system switches to the first outlet and triggers an alarm. After each switch, the operation log is automatically recorded, including the switching time, trigger parameters, and sensor status.

[0151] The system in this embodiment prevents the discharge of unstable reactants through a pH change rate threshold; dual conditions ensure that the discharged waste meets pH and precipitate standards; an overtime mechanism automatically attempts to remove precipitates; and an operation log provides process traceability.

[0152] According to another embodiment of the present invention, a method for collecting and treating hazardous waste is provided, comprising the following steps:

[0153] (a) The pH value of the liquid hazardous waste is collected in real time by multiple pH sensors installed in the delivery pipeline, and the controller calculates the average value as the current pH value of the waste.

[0154] (b) If the current waste pH value is below 6.0 or above 8.0, dynamically select the K1 or K2 coefficient according to the flow rate Q in the conveying pipeline, calculate the amount of neutralizer to be added according to the formula, and add the neutralizer to the conveying pipeline;

[0155] (c) Install a high-frequency pH sensor at the outlet of the neutralization reaction tank, with a sampling frequency ≥10Hz, to monitor the instantaneous pH value and change rate ΔpH / Δt of the waste after the reaction;

[0156] (d) When at least two pH sensors in the delivery pipeline simultaneously detect pH < 2.0 or > 12.0, immediately switch the three-way valve to the emergency treatment tank; if the absolute value of ΔpH / Δt is > 0.5pH / second and the instantaneous pH value deviates from the range of 6.0-8.0, start the emergency diversion simultaneously;

[0157] (e) When the pH value at the outlet of the neutralization reaction tank remains in the range of 6.0-8.0 for a dynamic time t seconds, and the ultrasonic detector confirms that the concentration of precipitate at the bottom of the neutralization reaction tank is <5%, switch the three-way valve to the final outlet.

[0158] Existing methods for treating liquid hazardous waste typically rely on a single pH value to determine the neutralization endpoint, without considering the dynamic stability of the reaction; emergency response is based solely on a fixed pH threshold, lacking multi-sensor collaborative verification; and the failure to detect precipitate concentration before discharge may lead to pipeline blockage or secondary pollution.

[0159] In this embodiment, the high-frequency pH sensor can be a solid-state electrode type, installed in the vertical pipe section at the outlet of the neutralization reaction tank, with a fixed sampling frequency of 10 Hz. The dynamic time t is calculated using the formula t=V / (Q×C) (V is the tank volume, Q is the flow rate, and C is an adjustable constant of 0.5-1.5). For example, with a 2 cubic meter tank, a flow rate of 100 liters / minute, and C of 1.0, t=120 seconds (automatically limited to 60 seconds because the calculated result of 20 seconds is lower than the lower limit of 60 seconds). Precipitation detection can be performed using an ultrasonic concentration meter, with the probe immersed 10 cm below the liquid surface at the bottom of the tank. The 5% threshold corresponds to 12 mA in the instrument's output signal range of 4-20 mA. Implementation example: When both pH sensors simultaneously detect pH=1.8, the three-way valve switches to the emergency tank within 0.5 seconds; under normal operating conditions, if the pH remains stable at 7.0±0.2 for t=90 seconds and the precipitate concentration is 3%, then it switches to the final outlet.

[0160] In this embodiment, multiple pH sensors within the delivery pipeline collect the pH value of the liquid hazardous waste in real time, and the controller calculates the average value as the current pH value of the waste. If this value is lower than 6.0 or higher than 8.0, the neutralizing agent addition amount is calculated according to the formula based on the flow rate Q of the delivery pipeline, using a dynamic selection coefficient K1 or K2, and is added to the pipeline. A high-frequency pH sensor is installed at the outlet of the neutralization reaction tank to monitor the instantaneous pH value and rate of change ΔpH / Δt of the waste after the reaction at a sampling frequency of not less than 10 Hz. When at least two pH sensors in the delivery pipeline simultaneously detect a pH value lower than 2.0 or higher than 12.0, the three-way valve is immediately switched to the emergency treatment tank; if the absolute value of ΔpH / Δt is greater than 0.5 pH per second and the instantaneous pH value deviates from the range of 6.0-8.0, emergency diversion is initiated simultaneously. When the pH value at the outlet of the neutralization reaction tank remains within the range of 6.0 to 8.0 for a dynamic time t seconds, and the ultrasonic detector confirms that the concentration of sediment at the bottom of the tank is lower than 5%, the three-way valve is switched to the final outlet.

[0161] The method of this embodiment captures instantaneous pH fluctuations through high-frequency sampling to avoid misjudgment in a single detection; the dual-sensor synchronous triggering mechanism improves the reliability of response under extreme operating conditions; dynamic time t ensures sufficient reaction; and a 5% precipitate concentration threshold prevents the risk of physical blockage.

[0162] According to another embodiment of the present invention, a method for collecting and treating hazardous waste is provided, wherein the following step is added before step (b):

[0163] (b1) The liquid hazardous waste is scanned in real time by a near-infrared spectrometer embedded in the delivery pipeline to obtain the characteristic absorption peak intensity value S at the target wavelength λ. t λ is preset to a specific wavelength in the range of 500-1800nm ​​according to the type of hazardous waste;

[0164] (b2) The controller calculates the critical peak mutation rate ΔS = |S t -S t-1 | / S t-1 ×100%, S t-1 This represents the intensity value of the characteristic absorption peak from the previous sampling period, with a sampling period of 1 second.

[0165] If ΔS > 30% or the current absorption peak does not match the hazardous waste characteristic spectrum in the pre-stored database, it is determined to be a compositional mutation.

[0166] (b3) Execute when components change abruptly:

[0167] Reduce the neutralizer addition rate to 50% of the current flow rate Q;

[0168] Add phosphate buffer solution with pH 7.0 to the delivery line, the amount added is V. buffer =0.2×Q×ΔS / 100L / min;

[0169] After a delay of 10-20 seconds, repeat step (b) and temporarily set the coefficients of K1 and K2 to 3.0 L / (min·pH).

[0170] Current methods rely solely on pH adjustment for neutralization. When waste composition changes abruptly (such as the introduction of high concentrations of organic solvents or oxidants), conventional neutralizing agents may become ineffective or even trigger side reactions. Existing technologies lack real-time identification and buffering mechanisms for sudden changes in composition.

[0171] In this embodiment, the near-infrared spectrometer can be installed in the transparent window section of the delivery pipeline, the light source can be a halogen tungsten lamp, and the detector can be an InGaAs array. The characteristic spectrum database can store the standard absorption spectra of at least 100 hazardous wastes, and the matching algorithm can use the minimum mean square error method. The phosphate buffer solution can be a disodium hydrogen phosphate-potassium dihydrogen phosphate system, and the storage tank can be equipped with a metering pump. Implementation example: When detecting ΔS=40% (e.g., S... t =1500, S t-1 When Q = 80 L / min, add buffer V (e.g., Q = 1071). buffer =0.2×80×40 / 100=6.4 liters; after a 15-second delay, neutralization is performed at K1=3.0. The mutation threshold of 30% corresponds to the fixed parameter of the mutation detection module in the spectrometer output signal.

[0172] In this embodiment, the following operation is added before step (b): the liquid hazardous waste is scanned in real time by a near-infrared spectrometer embedded in the delivery pipeline to obtain the characteristic absorption peak intensity value S at the preset target wavelength λ. t (λ is preset to a specific wavelength within the range of 500-1800 nm based on the type of hazardous waste; for example, 1720 nm can be selected for oily waste). The controller calculates the peak change rate ΔS between adjacent sampling periods (per period of 1 second), using the formula ΔS = S t Subtract S t-1 The absolute value divided by S t-1 Multiply by 100%. If ΔS is greater than 30% or the current absorption peak does not match the hazardous waste characteristic spectrum in the pre-stored database, it is determined to be a component mutation. In case of mutation, execute the following: reduce the neutralizer addition rate to 50% of the current flow rate Q; add phosphate buffer solution with pH=7.0 to the delivery line, the addition amount being V. buffer Calculate using the formula 0.2 multiplied by Q multiplied by ΔS divided by 100; after a delay of 10-20 seconds, repeat the neutralizer addition step, at which point the coefficients K1 and K2 are temporarily set to 3.0 liters per minute per pH unit.

[0173] The method of this embodiment identifies component mutations by near-infrared spectral change rate; buffer injection stabilizes the reaction system; the neutralizing agent addition rate is temporarily reduced to avoid side reactions; and a preset coefficient of 3.0 liters per minute per pH unit provides a safe operating margin.

[0174] According to another embodiment of the present invention, a method for collecting and treating hazardous waste is provided, wherein after step (b3), the following step is added:

[0175] (b4) Immobilized phosphatase was implanted in the delivery line 0.5-1.0m downstream of the buffer injection point. The immobilized phosphatase was loaded on the surface of Fe3O4 magnetic nanoparticle carrier with a particle size of 50-100nm. The carrier filling density was 1-5g / L, and the working temperature was maintained at 25-40℃.

[0176] (b5) When Δ S When the concentration is ≤10% for 30 seconds, the abrupt change in composition is determined to be resolved, and the magnetic separation device is activated with a magnetic field strength ≥0.5T to adsorb and remove the nanoparticle carrier.

[0177] (b6) The waste after magnetic separation enters a stepped sedimentation tank for three-stage settling:

[0178] Primary sedimentation: Let stand for 5 minutes to remove suspended solids with a particle size >50μm;

[0179] Secondary sedimentation: Add 0.1 ppm cationic polyacrylamide flocculant, let stand for 3 minutes, and remove particles with a diameter of 5-50 μm;

[0180] Three-stage sedimentation: High-frequency ultrasonic dispersion of colloid at 20kHz and 100±10W is applied, and the particles <5μm are removed after standing for 2 minutes.

[0181] Current methods for treating wastes resulting from compositional mutations primarily rely on buffer solutions to stabilize the pH, but they fail to address the deep removal of substances such as colloids, microorganisms, or enzyme inhibitors introduced by the mutation. Conventional precipitation processes are insufficiently efficient at separating micron-sized particles, easily leading to obstacles in subsequent neutralization reactions.

[0182] In this embodiment, the magnetic nanoparticle carrier can be Fe3O4 particles prepared by co-precipitation, and the surface can be modified with aminosilane to achieve covalent fixation of phosphatase. The magnetic separation device can be equipped with electromagnetic coils, and the electrode spacing can be set to 10 cm. The stepped sedimentation tank can be designed as three rectangular tanks connected in series, and the effective water depth can be set to 1.2 m. Implementation example: The carrier filling density is selected as 3 g / L, and the temperature is maintained at 35°C; magnetic separation is started when ΔS=8% for 30 seconds (1.0 Tesla field strength for 60 seconds); after the first stage of sedimentation, the turbidity of the supernatant drops to 20 NTU; after the second stage of flocculant addition, the turbidity drops to 5 NTU; and after the third stage of ultrasonic treatment, the turbidity is below 1 NTU. The ultrasonic power threshold of 100±10 watts is controlled by a closed-loop feedback mechanism through generator output power.

[0183] In this embodiment, an additional operation is added after step (b3): ​​an immobilized phosphatase is implanted in the delivery pipeline 0.5 to 1.0 meters downstream of the buffer injection point. This enzyme is loaded onto the surface of a magnetic nanoparticle carrier with a particle size of 50 to 100 nanometers, and the carrier packing density is controlled at 1 to 5 grams per liter. The operating temperature is maintained at 25 to 40 degrees Celsius through the pipeline jacket. When the mutation rate ΔS remains below 10% for 30 seconds, the mutation is considered resolved, and the magnetic separation device (magnetic field strength not less than 0.5 Tesla) is activated to adsorb and remove the nanoparticle carrier. After magnetic separation, the waste enters a stepped sedimentation tank for three-stage sedimentation: the first stage sedimentation is allowed to stand for 5 minutes to remove suspended solids with a particle size greater than 50 micrometers; the second stage sedimentation adds 0.1 ppm cationic polyacrylamide flocculant and is allowed to stand for 3 minutes to remove particles with a particle size of 5 to 50 micrometers; the third stage sedimentation applies high-frequency ultrasonic dispersion colloid at a frequency of 20 kHz and a power of 100 ± 10 watts and is allowed to stand for 2 minutes to remove particles smaller than 5 micrometers.

[0184] The method of this embodiment degrades organophosphorus pollutants by immobilizing phosphatases; achieves efficient recovery of enzyme active components by using magnetic carriers; removes impurities of different particle sizes by three-stage sedimentation and classification; and improves the destabilization efficiency of colloids by ultrasonic dispersion.

[0185] According to another embodiment of the present invention, a method for collecting and treating hazardous waste is provided, wherein a demulsification enhancement step is added before the three-stage settling in step (b6):

[0186] Electrochemical demulsification pretreatment is performed on the waste after magnetic separation:

[0187] A pulsed electric field device is installed at the inlet of the stepped sedimentation tank, with an electrode spacing of 10-20 cm, and an applied amplitude of [value missing]. V p =2.0× Frequency f=50 / t A square wave pulse, wherein: s The real-time conductivity of the waste (μS / cm, obtained via an online conductivity meter) is given. t The average droplet size (μm, monitored in real time by a laser particle size analyzer) is the oil droplet size.

[0188] Simultaneously regulate the waste temperature T, if C o ≥0.01%, T=40+5×ln(C o )℃, if C o <0.01%, T=40℃, where C o The concentration of the oil phase was calculated by inversion from the characteristic peak at 1700 nm using a near-infrared spectrometer, and T was automatically limited to the range of 25-40℃.

[0189] When the rate of change of dielectric constant Δ e / Δ t When the rate is ≤0.1% / s for 10 seconds, the demulsification is considered complete.

[0190] Existing methods for treating oil-containing emulsified hazardous waste mainly rely on chemical demulsifiers, which suffer from high reagent consumption and unstable separation efficiency. Conventional temperature control and fixed electric field parameters are difficult to adapt to real-time changes in conductivity and oil droplet size.

[0191] In this embodiment, the pulsed electric field device can be equipped with titanium-plated ruthenium electrodes, and the power supply can be a programmable high-voltage generator. The conductivity meter can be installed in the inlet pipe section of the sedimentation tank, and the laser particle size analyzer can be a diffraction-type online probe. Temperature control can be achieved using a plate heat exchanger, and the absorbance of the near-infrared spectrometer at 1700 nm is related to C... o The correspondence can be pre-defined (e.g., absorbance 0.35 corresponds to C). o =0.05%). Implementation example: When detecting σ = 2.5 millisiemens per centimeter, V p =2.0× ≈3.16 kV; if τ = 10 μm, then f = 5 Hz; when C o When the dielectric constant is 0.08%, T = 40 + 5 × ln(0.08) ≈ 44℃, and it is automatically adjusted to 40℃ because it exceeds the upper limit. A parallel plate capacitance sensor can be used for dielectric constant detection; the 0.1% threshold per second corresponds to the fixed parameters of the capacitance change rate detection module.

[0192] In this embodiment, an electrochemical demulsification enhancement step is added before the three-stage sedimentation in step (b6): a pulsed electric field device is installed at the inlet of the stepped sedimentation tank for the waste after magnetic separation. The electrode spacing is set to 10 to 20 cm, and a square wave pulse is applied with an amplitude of [missing value]. V p The frequency f is calculated by multiplying the waste flow rate by the square root of the real-time conductivity σ (σ is obtained through an online conductivity meter) using formula 2.0. The frequency f is calculated by dividing the average oil droplet size τ by formula 50 (τ is monitored in real-time using a laser particle size analyzer). The waste temperature T is simultaneously controlled: if the oil phase concentration C... o If the value is greater than or equal to 0.01%, then T equals 40 plus 5 multiplied by C. o The natural logarithm of C (in degrees Celsius); if C o If it is less than 0.01%, then T is set to 40 degrees Celsius. C o Inversion calculations using near-infrared spectroscopy at the 1700 nm characteristic peak automatically limited T to the range of 25 to 40 degrees Celsius. When the rate of change of the dielectric constant Δ... e / Δ t When the rate of demulsification continues to be no more than 0.1% per second for 10 seconds, it is determined that the demulsification is complete.

[0193] The method of this embodiment improves demulsification efficiency by using pulse parameters that are adaptive to conductivity and oil droplet size; optimizes oil-water separation kinetics with temperature control formula; and objectively determines the demulsification endpoint with a dielectric constant change rate threshold of 0.1% per second.

[0194] According to another embodiment of the present invention, a method for collecting and treating hazardous waste is provided, wherein a dual-functional magnetic carrier adsorption is integrated in a stepped sedimentation tank after demulsification:

[0195] The magnetic nanoparticle carrier was surface-modified with bifunctional components, including a hydrophobic end: octyltriethoxysilane (C8H4O2). 17 -Si-(OC2H5)3) modification layer, thickness 5-10nm; metal-philic end: dithiocarbamate chelating group (-N(CSS-)) grafted onto the outside of the hydrophobic layer;

[0196] When the rate of change of dielectric constant indicates that demulsification is complete, a bifunctional carrier is injected into the primary settling zone of the sedimentation tank at a volume of 0.1-0.5 vol% of the waste volume.

[0197] A rotating magnetic field with a strength of 0.3-0.8T and a rotation speed of 10-30 rpm is applied synchronously to drive the carrier to perform the following actions:

[0198] Oil phase capture: Free oil droplets are adsorbed at the hydrophobic end, with a contact angle >150°;

[0199] Heavy metal chelation: Metal-philic ions chelate cadmium, lead and mercury ions to form insoluble sulfides;

[0200] After sedimentation, the carrier is recovered by a magnetic separation device, and heavy metals are desorbed with 0.1M dilute hydrochloric acid. The desorbed liquid enters the electrodeposition recovery unit.

[0201] Existing methods require stepwise treatment of free oil droplets and heavy metal ions in demulsified waste, such as first adsorbing the oil phase and then chemically precipitating the heavy metals. This process is complex and prone to generating secondary sludge. Conventional adsorption materials have limited functionality and cannot simultaneously remove both types of pollutants.

[0202] In this embodiment, the carrier can be Fe3O4 particles with a particle size of 100 nm, the octyltriethoxysilane modification can be performed by chemical vapor deposition, and the dithiocarbamate grafting can be performed by mercapto-olefin click chemistry. The rotating magnetic field device can be equipped with a Helmholtz coil, and the speed control can be achieved by a stepper motor drive. Example implementation: 0.3% volume percentage of carrier is injected (e.g., 30 liters of carrier suspension is injected into 10 cubic meters of waste), a 0.5 Tesla rotating magnetic field (20 revolutions per minute) is applied, and the contact angle detection value is 152 degrees. During the desorption stage, the carrier is rinsed with 0.1M hydrochloric acid at a volume of 2 times, and the lead ion concentration in the desorbate is detected at 120 mg / L. The electrodeposition recovery unit can be equipped with a stainless steel cathode tank. Parameters such as the lower limit of carrier thickness of 5 nm and the contact angle threshold of 150 degrees are retained as per the original claims.

[0203] In this embodiment, a bifunctional magnetic carrier is integrated for adsorption in a stepped sedimentation tank after demulsification. First, the magnetic nanoparticle carrier undergoes surface modification: a 5-10 nm thick modification layer is formed at the hydrophobic end using octyltriethoxysilane; a dithiocarbamate chelating group is grafted onto the outside of the hydrophobic layer at the metalophilic end. When the dielectric constant change rate indicates demulsification is complete, the bifunctional carrier is injected into the primary sedimentation zone of the sedimentation tank at a volume percentage of 0.1-0.5% of the waste. A rotating magnetic field with a strength of 0.3-0.8 Tesla and a rotation speed of 10-30 rpm is simultaneously applied, driving the carrier to perform its dual function: the hydrophobic end adsorbs free oil droplets (contact angle greater than 150 degrees), and the metalophilic end complexes cadmium, lead, and mercury ions to form insoluble sulfides. After sedimentation, the carrier is recovered using a magnetic separation device, and heavy metals are desorbed using 0.1 mol / L dilute hydrochloric acid. The desorbed solution is then transported to an electrodeposition recovery unit.

[0204] The method of this embodiment uses a dual-functional carrier to simultaneously remove oil phase and heavy metals; a rotating magnetic field enhances the carrier's contact efficiency with pollutants; and dilute hydrochloric acid desorption enables carrier regeneration and heavy metal recovery.

[0205] Example:

[0206] Taking the centralized treatment of liquid hazardous waste in a certain electroplating industrial park as an example

[0207] This electroplating industrial park processes 200 tons of mixed wastewater daily, including strong acid cleaning solution (pH 1.5~3.0) and cyanide copper plating wastewater (containing Cu). 2+ The system contained wastewater containing 200 mg / L of pollutants and emulsified degreasing wastewater (oil phase concentration 0.15%). In the past, the neutralization tank corroded due to a sudden drop in pH, and the oil contamination of heavy metal ions caused excessive precipitates (>12%).

[0208] The delivery pipeline uses DN80 polyethylene pipes with a flow range of 50~150 L / min.

[0209] pH monitoring uses six glass electrode sensors (model PHG-209A) spaced 1.5m apart.

[0210] The controller uses a Siemens S7-1500 PLC with a pre-stored θ compensation table (θ1=30.0 when pH<3.0).

[0211] The stepped sedimentation tank adopts a three-stage series connection with a total volume of 10m³ (4m³ for the first stage, 3m³ for the second stage, and 3m³ for the third stage).

[0212] The bifunctional carrier uses Fe3O4 nanoparticles (80 nm in diameter), an octylsilane layer thickness of 8 nm, and a chelating group loading of 0.8 mmol / g.

[0213] Processing steps

[0214] Step 1: Identification of Extreme pH Events and Compositional Mutations

[0215] 14:00:00: The collection device receives pickling waste liquid (containing Fe) with pH=1.8. 3+ 1500 mg / L), flow rate Q = 120 L / min.

[0216] Real-time values ​​from 6 pH sensors: [1.82, 1.79, 1.85, 1.80, 15.60 (fault drift), 1.83]

[0217] The controller calculates the average value as: (1.82+1.79+1.85+1.80+1.83) / 5 = 1.82 (excluding the fault value of 15.60).

[0218] Emergency Operations

[0219] The current pH is 1.82 (<2.0). Immediately switch the three-way valve to the emergency treatment tank (response time <3 seconds).

[0220] Mark sensor #5 as faulty (3 consecutive deviations from the mean > ±2.0), triggering an audible and visual alarm.

[0221] Start the emergency tank's circulating cooling system (cool down to 25°C).

[0222] 14:02:30: Near-infrared spectrometer (λ=1720nm) detects absorbance S t =1850, S t-1 =1200 (ΔS=54.2%>30%), indicating a mutation in composition (mixed with emulsified defatting wastewater).

[0223] Buffering:

[0224] The neutralizing agent addition rate was reduced to 60 L / min (Q×50%).

[0225] Inject pH 7.0 phosphate buffer: V buffer =0.2×120×54.2 / 100≈13 L.

[0226] After a 15-second delay, add lime slurry at a temporary K1 of 3.0 L / (min·pH) (addition amount = 3.0 × (6.0 - 1.82) × 30.0 ≈ 377 L / min).

[0227] Step 2: Deep purification of mutant components

[0228] 14:03:00: Immobilized phosphatase vector was implanted 0.8m downstream of the buffer injection point (filling density 3g / L, temperature maintained at 35℃).

[0229] 14:05:00: ΔS drops to 8% and remains there for 30 seconds. Magnetic separation device is activated (field strength 0.7T). Recovery rate >98%.

[0230] Stepped sedimentation:

[0231] Primary sedimentation: Let stand for 5 minutes to remove metal particles >50μm (turbidity decreases from 100 NTU to 25 NTU).

[0232] Secondary sedimentation: Add 0.1 ppm cationic polyacrylamide, let stand for 3 minutes, and remove 5-50 μm oil droplets (turbidity reduced to 6 NTU).

[0233] Demulsification enhancement (before stage III sedimentation):

[0234] Conductivity σ = 3.2 mS / cm → V p =2.0× ≈3.58 kV.

[0235] Oil droplet size τ=12μm → f=50 / 12≈4.2 Hz.

[0236] oil phase concentration C o =0.15% → T=40+5×ln(0.15)≈37℃.

[0237] The dielectric constant change rate Δε / Δt ≤ 0.1% / s lasts for 10 seconds (demulsification is complete).

[0238] Three-stage sedimentation: Apply 20kHz / 100W ultrasound, let stand for 2 minutes, and the colloidal particles will decrease to <1 NTU.

[0239] Step 3: Simultaneous decontamination using dual-function carriers

[0240] 14:20:00: Inject 0.3 vol% bifunctional carrier (60 L) into the primary settling zone and simultaneously apply a rotating magnetic field (0.5 T, 20 rpm).

[0241] Hydrophobic adsorption: Contact angle detection value 152°, free oil droplet removal rate >95%.

[0242] Heavy metal chelation: Cu adsorption on the support 2+ 180 mg / L, Pb 2+ At 35 mg / L, sulfide precipitates are formed.

[0243] 14:35:00: Magnetic separation and recovery of carrier, 0.1M HCl desorption of heavy metals (desorption rate 92%), desorption solution sent to electrowinning unit to recover copper metal.

[0244] Step 4: Neutralization reaction and safe emission

[0245] 14:40:00: Waste enters the neutralization reaction tank (V=5m³), monitored by a high-frequency pH sensor (10Hz) at the outlet:

[0246] The pH remained stable at 7.0±0.3, and the dynamic time t=V / (Q×C)=5000 / (100×1.2)≈42 seconds → the amplitude was automatically limited to 60 seconds.

[0247] The concentration of the precipitate detected by ultrasonic testing was 4.2% < 5%.

[0248] Security verification:

[0249] Condition 1: pH between 6.0 and 8.0 for 60 seconds → Satisfied.

[0250] Condition 2: Precipitate ≤ 5% → Satisfied.

[0251] Discharge action: Switch the three-way valve to the final outlet and generate a log:

[0252] "2025-07-10 14:41:30 Switched to final outlet | pH=7.1 for 60 seconds | Precipitate 4.2% | Sensor status: 1-4, 6 normal; 5 faulty"

[0253] This embodiment demonstrates that when dealing with complex conditions such as a sudden drop in pH of electroplating wastewater, oil contamination, and excessive heavy metals, the system achieves safe and stable discharge through closed-loop control logic and multi-stage purification units, reducing overall treatment costs by 31%.

[0254] The number of devices and processing scale described herein are for the purpose of simplifying the description of the invention. Applications, modifications, and variations of the invention will be readily apparent to those skilled in the art.

[0255] Although embodiments of the present invention have been disclosed above, they are not limited to the applications listed in the specification and embodiments. They can be applied to various fields suitable for the present invention. For those skilled in the art, other modifications can be easily made. Therefore, without departing from the general concept defined by the claims and their equivalents, the present invention is not limited to the specific details and embodiments shown and described herein.

Claims

1. A method for collecting and treating hazardous waste, characterized in that, Includes the following steps: (a) The pH value of the liquid hazardous waste is collected in real time by multiple pH sensors installed in the delivery pipeline, and the controller calculates the average value as the current pH value of the waste. (b) If the current waste pH value is below 6.0 or above 8.0, dynamically select the K1 or K2 coefficient according to the flow rate Q in the conveying pipeline, calculate the amount of neutralizer to be added according to the formula, and add the neutralizer to the conveying pipeline; When the current pH value of the waste is below 6.0, the amount of alkaline neutralizer to be added is determined according to the formula: Amount of alkaline neutralizer added = K1 × (6.0 - current pH value of waste) × θ1; When the current pH value of the waste is higher than 8.0, the amount of acid neutralizer to be added is determined according to the formula: Acid neutralizer addition amount = K2 × (current waste pH value - 8.0) × θ2; Wherein, K1 is the preset addition coefficient of alkaline neutralizer with a value range of 1.0 to 5.0 L / (min·pH), K2 is the preset addition coefficient of acidic neutralizer with a value range of 1.0 to 5.0 L / (min·pH), and θ1 and θ2 are both pH compensation factors, determined by the lookup table method; the lookup table method realizes differentiated control in different pH ranges, accurately matching the nonlinear neutralization characteristics under strong acid and strong base environments; When Q > 100 L / min, the values ​​of K1 and K2 are reduced to 0.8 times their original values; when the waste composition contains heavy metal ions, the basic values ​​of K1 and K2 are increased by 30%. (c) Install a high-frequency pH sensor at the outlet of the neutralization reaction tank, with a sampling frequency ≥10Hz, to monitor the instantaneous pH value and change rate ΔpH / Δt of the waste after the reaction; (d) When at least two pH sensors in the delivery pipeline simultaneously detect pH < 2.0 or > 12.0, immediately switch the three-way valve to the emergency treatment tank; if the absolute value of ΔpH / Δt is > 0.5pH / second and the instantaneous pH value deviates from the range of 6.0-8.0, start the emergency diversion simultaneously; (e) When the pH value at the outlet of the neutralization reaction tank remains in the range of 6.0-8.0 for a dynamic time t seconds, and the ultrasonic detector confirms that the concentration of precipitate at the bottom of the neutralization reaction tank is <5%, switch the three-way valve to the final outlet.

2. The hazardous waste collection and treatment method as described in claim 1, characterized in that, Before step (b), add the following steps: (b1) The liquid hazardous waste is scanned in real time by a near-infrared spectrometer embedded in the delivery pipeline to obtain the characteristic absorption peak intensity value S at the target wavelength λ. t λ is preset to a wavelength in the range of 500-1800nm ​​according to the type of hazardous waste; (b2) The controller calculates the critical peak mutation rate ΔS = |S t -S t-1 | / S t-1 ×100%, S t-1 This represents the intensity value of the characteristic absorption peak from the previous sampling period, with a sampling period of 1 second. If ΔS > 30% or the current absorption peak does not match the hazardous waste characteristic spectrum in the pre-stored database, it is determined to be a compositional mutation. (b3) Execute when components change abruptly: Reduce the neutralizer addition rate to 50% of the current flow rate Q; Add phosphate buffer solution with pH 7.0 to the delivery line, the amount added is V. buffer =0.2×Q×ΔS / 100; After a delay of 10-20 seconds, repeat step (b) and temporarily set the coefficients of K1 and K2 to 3.0 L / (min·pH).

3. The hazardous waste collection and treatment method as described in claim 2, characterized in that, After step (b3), add the following steps: (b4) Immobilized phosphatase was implanted in the delivery line 0.5-1.0m downstream of the buffer injection point. The immobilized phosphatase was loaded on the surface of Fe3O4 magnetic nanoparticle carrier with a particle size of 50-100nm. The carrier filling density was 1-5g / L, and the working temperature was maintained at 25-40℃. (b5) When Δ S When the concentration is ≤10% for 30 seconds, the abrupt change in composition is determined to be resolved, and the magnetic separation device is activated with a magnetic field strength ≥0.5T to adsorb and remove the nanoparticle carrier. (b6) The waste after magnetic separation enters a stepped sedimentation tank for three-stage settling: Primary sedimentation: Let stand for 5 minutes to remove suspended solids with a particle size >50μm; Secondary sedimentation: Add 0.1 ppm cationic polyacrylamide flocculant, let stand for 3 minutes, and remove particles with a diameter of 5-50 μm; Three-stage sedimentation: High-frequency ultrasonic dispersion of colloid at 20kHz and 100±10W is applied, and the particles <5μm are removed after standing for 2 minutes.

4. The hazardous waste collection and treatment method as described in claim 3, characterized in that, Add a demulsification enhancement step before the third-stage settlement in step (b6): Electrochemical demulsification pretreatment is performed on the waste after magnetic separation: A pulsed electric field device is installed at the inlet of the stepped sedimentation tank, with an electrode spacing of 10-20 cm, and an applied amplitude of [value missing]. V p =2.0× Frequency f=50 / τ A square wave pulse, wherein: σ The real-time conductivity of the waste was obtained using an online conductivity meter. τ The average particle size of the oil droplets is monitored in real time using a laser particle size analyzer. Simultaneously regulate the waste temperature T, if C o ≥0.01%, T=40+5×ln(C o )℃, if C o <0.01%, T=40℃, where C o The concentration of the oil phase was calculated by inversion from the characteristic peak at 1700 nm using a near-infrared spectrometer, and T was automatically limited to the range of 25-40℃. When the rate of change of dielectric constant Δ ε / Δ t When the rate is ≤0.1% / s for 10 seconds, the demulsification is considered complete.

5. The hazardous waste collection and treatment method as described in claim 4, characterized in that, A dual-function magnetic carrier adsorption is integrated into the stepped sedimentation tank after demulsification: The magnetic nanoparticle carrier was surface-modified with bifunctional components, wherein the hydrophobic end was octyltriethoxysilane (C8H). 17 -Si-(OC2H5)3) modification layer, 5-10nm thick; metalophilic end is a dithiocarbamate chelating group (-N(CSS-)) grafted onto the outside of the hydrophobic layer; When the rate of change of dielectric constant indicates that demulsification is complete, a bifunctional carrier is injected into the primary settling zone of the sedimentation tank at a volume of 0.1-0.5 vol% of the waste volume. A rotating magnetic field with a strength of 0.3-0.8T and a rotation speed of 10-30rpm is applied synchronously to drive the carrier to perform the operation. The hydrophobic end adsorbs free oil droplets with a contact angle >150°; the metalophilic end complexes cadmium ions, lead ions, and mercury ions to form insoluble sulfides. After sedimentation, the carrier is recovered by a magnetic separation device, and heavy metals are desorbed with 0.1M dilute hydrochloric acid. The desorbed liquid enters the electrodeposition recovery unit.

6. A hazardous waste collection and treatment system, characterized in that, include: Collection device for receiving liquid hazardous waste; The pipeline connects to the collection device and is used to transport liquid hazardous waste; Multiple pH sensors are installed in the delivery pipeline to monitor the pH value of liquid hazardous waste in real time; The controller connects to multiple pH sensors to calculate the average pH value measured by the multiple pH sensors as the current pH value of the waste, and generates instructions on the amount of neutralizer to be added based on whether the current pH value of the waste is below 6.0 or above 8.

0. A neutralizer adding device, connected to a controller, is used to add alkaline or acidic neutralizer to the delivery pipeline according to the neutralizer adding amount instruction; The neutralization reaction vessel, connected downstream of the delivery pipeline, is used to receive liquid hazardous waste from the delivery pipeline and alkaline or acidic neutralizing agent added by the neutralizing agent adding device, and to mix and neutralize it. Emergency response tank; The three-way valve has its inlet connected to the outlet of the neutralization reaction tank, its first outlet connected to the inlet of the emergency treatment tank, and its second outlet connected to the final outlet of the system. A near-infrared spectrometer, embedded in the delivery pipeline, is used to scan the characteristic absorption peaks of liquid hazardous waste in real time, providing component data for the controller to generate neutralizing agent instructions; A stepped sedimentation tank is installed between the conveying pipeline and the neutralization reaction tank to pre-separate suspended solid impurities, ensuring that the waste entering the neutralization reaction tank meets the reaction conditions. The controller is connected to a three-way valve. When at least two of the multiple pH sensors simultaneously detect a pH value below 2.0 or above 12.0, the controller switches the three-way valve to the first outlet. When the final pH sensor at the outlet of the neutralization reaction tank detects that the waste pH value is in the range of 6.0 to 8.0 and remains within a dynamic time t seconds, the controller switches the three-way valve to the second outlet.

7. The hazardous waste collection and treatment system as described in claim 6, characterized in that, The controller generates the neutralizer addition command based on the current waste pH value as follows: When the current pH value of the waste is below 6.0, the amount of alkaline neutralizer to be added is determined according to the formula: Amount of alkaline neutralizer added = K1 × (6.0 - current pH value of waste) × θ1; When the current pH value of the waste is higher than 8.0, the amount of acid neutralizer to be added is determined according to the formula: Acid neutralizer addition amount = K2 × (current waste pH value - 8.0) × θ2; Wherein, K1 is the preset addition coefficient of alkaline neutralizer with a value range of 1.0 to 5.0 L / (min·pH), K2 is the preset addition coefficient of acidic neutralizer with a value range of 1.0 to 5.0 L / (min·pH), and θ1 and θ2 are both pH compensation factors, which are determined by the lookup table method. The lookup table method realizes differentiated control in different pH ranges and accurately matches the nonlinear neutralization characteristics under strong acid and strong base environments.

8. The hazardous waste collection and treatment system as described in claim 6, characterized in that, The controller is also equipped with an emergency control module, which performs the following operations: The deviation between the pH sensor's monitored value and the average value is compared in real time. If the value of any sensor deviates from the average value by more than ±2.0 for three consecutive times, the sensor is marked as faulty and an alarm is triggered. When the current waste pH value is below 2.0 or above 12.0, regardless of whether a neutralizer addition instruction is generated, immediately control the three-way valve to switch to the first outlet and start the circulating cooling system of the emergency treatment tank; When the number of faulty sensors exceeds 50% of the total, the automatic neutralization process is shut down and switched to manual intervention mode.

9. The hazardous waste collection and treatment system as described in claim 6, characterized in that, The controller is also equipped with a dynamic adjustment module, which includes: Neutralizing agent optimization unit: Based on real-time data Q from the flow sensor in the delivery pipeline and the waste composition database, dynamically adjusts K1 and K2 to meet the following conditions: When Q > 100 L / min, the values ​​of K1 and K2 are reduced to 0.8 times the original coefficients; When the waste composition contains heavy metal ions, the basic values ​​of K1 and K2 increase by 30%; Delay Adaptive Unit: The dynamic time t is calculated by the formula t=V / (Q×C), where V is the effective volume of the neutralization reaction vessel, C is the reaction sufficiency constant, which takes a value of 0.5-1.5, and t is automatically limited to the range of 60-120 seconds.

10. The hazardous waste collection and treatment system as described in claim 6, characterized in that, The switching action of the three-way valve needs to be confirmed by the safety verification module, including: (1) Before switching to the first outlet, the controller retrieves the pH change rate data of the neutralization reaction tank in the last 10 seconds. If the absolute value of the change rate exceeds 0.5 pH / second, the switching is delayed until the change rate drops below 0.2 pH / second. (2) Before switching to the second exit, two conditions must be met in sequence: Condition 1: The final pH sensor reading remains within the range of 6.0-8.0 for t seconds; Condition 2: The ultrasonic detector reading of the sediment at the bottom of the neutralization reaction vessel is ≤5% of the threshold. Timeout mechanism: If condition 2 is not met within 60 seconds after condition 1 is met, then execute: Start the stirrer at the bottom of the neutralization reaction vessel at 30-50 rpm for 20 seconds; Inject anionic polyacrylamide flocculant into the neutralization reaction vessel at a rate of 0.05-0.1 ppm of the waste volume inside the vessel. After standing for 10 seconds, retest the concentration of the precipitate. If the concentration is still >5%, switch to the first outlet and trigger the precipitate over-limit alarm; (3) An operation log is automatically generated after each switch, recording the switch time, trigger parameters and sensor status.