Papermaking wastewater treatment device

Abstract

The utility model discloses a papermaking wastewater treatment device which comprises a hydrolysis area, a biochemical reaction group and an oxygen elimination area, and the biochemical reaction group is provided with dynamic transition sections and fixed function sections which are alternately distributed along the water flow direction; at least one dynamic transition section is provided with a direction-variable flow guide mechanism; the fixed functional sections are differentiated and integrated into the aeration system, and the gas output directions of the adjacent aeration systems form an angle difference. The dynamic transition sections and the fixed functional sections are alternately arranged, the tangential speed of water flow is regulated and controlled by combining a direction-variable flow guide mechanism, a dissolved oxygen gradient field is constructed by a multi-angle aeration system, the hydrolysis effect is enhanced by utilizing a baffling strengthening assembly, and the real-time feedback control of an adjustable on-off region and a sludge return system are matched, so that the hydrolysis efficiency is improved. Dynamic optimization of the activated sludge concentration and the hydraulic retention time is achieved, and the problems that a traditional device is low in biochemical reaction efficiency and poor in impact load resistance are solved.

Description

Technical Field

[0001] This utility model relates to wastewater treatment devices, and more particularly to a papermaking wastewater treatment device. Background Technology

[0002] The paper industry is one of the world's most important basic industries, but it is also a high-water-consuming and high-polluting sector. Paper wastewater contains large amounts of organic matter, suspended solids, color, and toxic substances; if discharged directly without effective treatment, it will cause serious damage to aquatic ecosystems. Therefore, optimizing existing biological treatment processes and improving the efficiency and effectiveness of paper wastewater treatment is of great significance for alleviating environmental pressure and protecting water resources.

[0003] China has made some progress in the treatment of papermaking wastewater, researching and developing various treatment methods such as anaerobic-aerobic (A / O) processes, sequencing batch reactors (SBR), and membrane bioreactors (MBR). However, these technologies still face problems in practical applications, including high costs, unstable efficiency, and secondary pollution.

[0004] For example, the patent document "A Three-Sludge Aerobic-Hydrolysis-Aerobic-Membrane Bioreactor and Method" published in Chinese patent literature, publication number "CN113603304A", includes aerobic, hydrolysis, and aerobic-membrane treatment units and a water intake and equalization tank; the wastewater in the water intake and equalization tank is output through two pipelines; the first pipeline output passes through the inlet valve of the hydrolysis treatment unit and the inlet pump of the anoxic treatment unit in sequence, and is transported to the reaction zone of the hydrolysis treatment unit; the second pipeline passes through the inlet valve of the aerobic treatment unit and the inlet pump of the aerobic treatment unit in sequence, and is transported to the reaction zone of the aerobic treatment unit. This invention constructs a three-sludge aerobic-hydrolysis-aerobic-membrane bioreactor treatment process, realizing the specific enrichment of sludge microbial populations, combined with the pollutant interception and microbial enrichment capabilities of microfiltration membranes.

[0005] The above-mentioned scheme can achieve efficient removal of high-load organic pollutants and toxic substances from wastewater, but the treatment process in this method has significant limitations and cannot solve the problems of low biochemical reaction efficiency and poor resistance to shock loads in traditional devices. Utility Model Content

[0006] To address the issues of low biochemical reaction efficiency and poor resistance to shock loads in traditional devices mentioned in the background art, this invention utilizes an alternating layout of dynamic transition sections and fixed functional sections, combined with a variable flow guide mechanism to regulate the tangential velocity of the water flow and a multi-angle aeration system to construct a dissolved oxygen gradient field. Furthermore, it employs a flow-enhancing component to improve the hydrolysis effect, and with the real-time feedback control of adjustable on / off zones and a sludge return system, it achieves dynamic optimization of activated sludge concentration and hydraulic retention time.

[0007] To achieve the above objectives, the present invention adopts the following technical solution:

[0008] A papermaking wastewater treatment device includes a hydrolysis zone, a biochemical reaction group, and a deoxygenation zone. The biochemical reaction group is provided with alternating dynamic transition sections and fixed functional sections along the water flow direction. At least one of the dynamic transition sections is equipped with a variable flow guiding mechanism. Each fixed functional section has a differentiated integrated aeration system, and the gas output directions of adjacent aeration systems have angular differences.

[0009] The dynamic transition section includes a series of hypoxic zones and an adjustable on / off zone, while the fixed functional section includes an anaerobic reaction zone and a stepped aerobic zone group.

[0010] The variable flow guidance mechanism consists of multiple arc-shaped flow guide plates, and each flow guide plate is connected to an angle adjustment controller via a universal joint.

[0011] The stepped aerobic zone group includes a first swirl aeration zone, a second micropore aeration zone, and a third diffusion aeration zone, with the axes of the aeration heads in the three zones forming an angle of 10-35° with each other.

[0012] The inner side of the arc-shaped guide plate is provided with guide ribs, and the rib spacing decreases along the water flow direction in increments of Δ=0.2L-0.5L, where L is the length of the plate.

[0013] The adjustable on / off zone is equipped with a liftable weir, and a pressure sensor is embedded on the surface of the weir and is connected to the bottom of the hydrolysis zone.

[0014] The first swirl aeration zone uses an aeration head with an umbrella-shaped diffuser, and the aeration pipe of the second microporous aeration zone is covered with a ceramic membrane layer.

[0015] The protrusion height of the guide rib and the opening D of the umbrella-shaped diffuser satisfy h=0.15D-0.3D.

[0016] The hydrolysis zone is equipped with a flow enhancement component, which forms a sawtooth-shaped water flow channel with an amplitude of 30-50cm.

[0017] The aeration pipe of the third diffusion aeration zone is equipped with a silicone flow-limiting sleeve, and the sleeve has a tapered through hole.

[0018] Therefore, this utility model has the following beneficial effects:

[0019] By alternating the layout of dynamic transition sections and fixed functional sections, and combining the dynamic control of water flow pattern by a variable flow guide mechanism, the problem of low biochemical reaction efficiency caused by the single flow pattern of traditional processes is solved, thereby increasing the COD removal rate to over 92% and enhancing the resistance to load shock by 40%.

[0020] By utilizing the geometric relationship between the decreasing spacing of the guide ribs and the opening of the umbrella-shaped diffuser, a synergistic effect between the bubble trajectory and the tangential velocity of the water flow is formed, overcoming the deficiency of insufficient oxygen mass transfer efficiency in traditional aeration, achieving an oxygen utilization rate of 22% and reducing energy consumption by 18%.

[0021] By using the closed-loop control of the adjustable on / off zone weir and pressure sensor, the hydraulic retention time can be dynamically adjusted by ±30%, which solves the problem of sludge bulking caused by fluctuations in influent load and improves MLSS stability to within ±5%.

[0022] By adopting a stepped aerobic zone multi-angle aeration system and establishing a three-dimensional dissolved oxygen gradient field, the technical bottleneck of nitrification / denitrification environment separation in traditional processes has been overcome. The ammonia nitrogen removal load reaches 0.82 kgN / (m³·d), and the TN removal rate is increased to 86%. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the structure of this utility model.

[0024] In the diagram: Hydrolysis zone 1, baffle enhancement component 11, biochemical reaction group 2, dynamic transition section 21, anoxic zone 211, adjustable on / off zone 212, fixed functional section 22, anaerobic reaction zone 221, stepped aerobic zone group 222, guide plate 23, guide rib 231, universal joint 24, deoxygenation zone 3, first swirl aeration zone a, second microporous aeration zone b, third diffusion aeration zone c, aeration head a1, ceramic membrane layer b1, silicone flow restrictor c1. Detailed Implementation

[0025] The present invention will be further described below with reference to the accompanying drawings and specific embodiments.

[0026] Example 1

[0027] like Figure 1 As shown, a papermaking wastewater treatment device includes a hydrolysis zone 1, a biochemical reaction group 2, and a deoxygenation zone 3. The biochemical reaction group 2 is provided with alternating dynamic transition sections 21 and fixed functional sections 22 along the water flow direction. At least one of the dynamic transition sections 21 is equipped with a variable flow guiding mechanism. Each fixed functional section 22 is a differentially integrated aeration system, and the gas output direction of adjacent aeration systems forms an angular difference.

[0028] In this embodiment, the papermaking wastewater treatment device is based on a transverse layout with a hydrolysis tank width of 23750mm. Within the hydrolysis zone 1, a baffle enhancement component 11 is arranged along the 23.75-meter tank width direction, featuring serrated water flow channels with an amplitude of 30-50cm. The component consists of baffles spaced 800mm apart, with a plate thickness of 188mm, allowing the wastewater to remain in the hydrolysis zone for 3.54 hours. The outlet of the hydrolysis zone connects to the dynamic transition section 21 of the biochemical reaction group 2. The anoxic zone 211, with a total width of 11875mm, is divided into anoxic zone one (1.01 hours) and anoxic zone two (2.37 hours). The two zones are connected by an adjustable on / off zone 212, which includes two 5000mm wide adjustment units. Each unit is equipped with a hydraulically driven, liftable weir 26, with the weir's lifting stroke matching the 1.96-hour hydraulic retention requirement. A variable flow guide mechanism is set at the end of the dynamic transition section. Its arc-shaped flow guide plate 23 adopts an arc structure with a curvature radius R=1500mm. Six plates are evenly spaced along the 5000mm width direction. An angle adjustment controller 25 is connected through a universal joint 24. Flow guide ribs 231 are welded to the inner side of the flow guide plate. The rib spacing is arranged according to the law of decreasing Δ=0.2L-0.5L. Under the condition of L=2000mm plate length, a gradual distribution from 400mm at the beginning to 1000mm at the end is achieved. The stepped aerobic zone group 222 in the fixed functional section 22 includes a first swirl aeration zone a with a width of 5000mm, a second microporous aeration zone b with a width of 10000mm, and a third diffusion aeration zone c with a width of 5000mm. The axes of the aeration heads in each zone are staggered with an angle difference of 25°±5°. The swirl aeration zone a uses an umbrella-shaped diffusion hood aeration head a1. When the opening of the hood D=150mm, the height h=30mm of the guide rib 231 satisfies the relationship h=0.2D. The aeration pipe of the microporous aeration zone b is covered with a ceramic membrane layer b1 with a porosity of 35% and a thickness of 0.8mm. The silicone flow limiting sleeve c1 of the diffusion aeration zone c has a wall thickness of 6mm, and the diameter of the tapered through hole c2 is linearly reduced from 3mm to 1mm. The deoxygenation zone 3, 5000mm wide, is separated from the subsequent anoxic and aerobic zones, both 4813mm wide, by a 188mm thick partition wall. The deoxygenation zone has a 45° angled umbrella-shaped air collection hood at the top and hexagonally arranged aeration pipes with 8mm diameter perforations at a 120mm spacing. The adjustable on / off zone 212's weir 26 has a lifting speed matching the 1.96-hour residence time adjustment requirement. When the influent load fluctuates, the pressure sensor 27 monitors the weir surface pressure changes in real time and uses a PID algorithm to control the lifting amplitude within ±300mm, keeping the overall hydraulic residence time of the dynamic transition section within an adjustable range of 4.34-6.34 hours. The geometric relationship between the guide rib 231 and the umbrella-shaped diffuser allows the bubble group to form a vortex bubble chain with a diameter of Φ3-8mm in the swirling aeration zone a, which, together with the microbubble group with a diameter of Φ0.5-2mm generated in the microporous aeration zone b, forms a three-dimensional gradient field with a dissolved oxygen concentration of 0.5-4mg / L in a 10000mm wide area.The gradually narrowing through-holes c2 in the diffusion aeration zone c increase the airflow velocity from 5 m / s to 12 m / s, working synergistically with the counter-current contact field in the deoxygenation zone to reduce the dissolved oxygen in the effluent to below 0.5 mg / L. The device, through the alternating layout of the dynamic transition section 21 and the fixed functional section 22, forms three independent control units along the 23.75-meter pool width. The sludge concentration gradient difference between each unit reaches 500-800 mg / L, with the MLSS value maintained at 2000-2500 mg / L in the anoxic zone and increased to 3500-4000 mg / L in the aerobic zone. The serrated channels of the baffle enhancement component 11 achieve a hydrolysis efficiency of 58% when the influent COD is 8000 mg / L, a 32% improvement over traditional structures. The differentiated aeration of the stepped aerobic zone group 222 stabilizes the ammonia nitrogen removal load at 0.75 kgN / (m³·d), optimizing the air-to-water ratio to 5.2:1. The dual-unit design of the adjustable on / off zone 212 enables the device to maintain effluent SS ≤ 30 mg / L through the coordinated adjustment of the weir 26 when the influent flow rate fluctuates by ±25%.

[0029] The papermaking wastewater treatment device achieves efficient pollutant degradation through a structured combination and dynamic control mechanism of multi-stage reaction zones. Its core lies in the alternating layout of the biochemical reaction groups and the spatial synergistic effect of the aeration system. The hydrolysis zone employs a baffle-enhanced component to construct a sawtooth-shaped water flow channel with an amplitude of 30-50 cm. This component consists of staggered V-shaped guide plates and arc-shaped buffer units, with the plate spacing gradually decreasing along the water flow direction. This accelerates the decomposition of large organic molecules in the wastewater under turbulent shear force.

[0030] The hydrolysis zone outlet connects to the dynamic transition section of the biochemical reaction group. The anoxic zone employs a gradually expanding cross-section flow channel structure with a rotatable biological packing frame at the top. The adjustable on / off zone utilizes a hydraulically driven, liftable weir to adjust the flow channel cross-sectional area. Pressure sensors embedded in the weir surface monitor the water flow impact force in real time and, through a feedback control system, link with the return valve at the bottom of the hydrolysis zone, forming a hydraulic load adaptive adjustment loop. The variable flow guidance mechanism at the end of the dynamic transition section consists of multiple arc-shaped guide plates with a curvature radius R = 150-300 mm. Each plate is connected to a servo motor-driven angle adjustment controller via a universal joint, creating a spiral propulsion flow before entering the fixed functional section. This enhances the contact efficiency between activated sludge and wastewater. The guide ribs on the inner side of the guide plates have a trapezoidal cross-section, with the rib spacing decreasing along the plate length L by Δ = 0.2L-0.5L. This decreasing gradient has been verified by fluid dynamics simulation to effectively suppress boundary layer separation.

[0031] The anaerobic reaction zone of the fixed functional section is equipped with a multi-layer honeycomb biofilm carrier, with the spacing between the carrier layers increasing by 5-8 cm from bottom to top, forming a non-uniform biofilm distribution to adapt to the growth requirements of different bacterial communities. In the stepped aerobic zone, the first swirl aeration zone uses an aeration head with an umbrella-shaped diffuser. The opening D of the hood and the height h of the guide rib protrusion satisfy the matching relationship of h=0.15D-0.3D, ensuring that the bubble group forms a vortex upward trajectory under the action of the guide rib. The aeration pipe of the second microporous aeration zone is covered with a ceramic membrane layer with a pore size of 0.2-0.5μm. This structure can prevent activated sludge from entering the pipe while ensuring oxygen mass transfer efficiency. The silica gel flow restrictor of the third diffusion aeration zone is equipped with a gradually narrowing through hole. The diameter of the through hole decreases from 3mm at the inlet end to 1mm at the outlet end, so that the airflow velocity gradient and the water flow direction are oppositely distributed. The gas output directions of adjacent aeration zones differ by an angle of 10-35°. This angle range, optimized through computational fluid dynamics, allows the dissolved oxygen concentration to form a wave-like distribution curve in three-dimensional space, promoting the alternating metabolic activity of aerobic microorganisms. The deoxygenation zone adopts a gas-liquid countercurrent contact design, with an umbrella-shaped gas collection hood at the top and a perforated aeration pipe at the bottom forming a convection field, effectively removing residual dissolved oxygen while recovering usable gas.

[0032] During operation, the alternating layout of dynamic transition sections and fixed functional sections creates pulsed hydraulic loads. Combined with the dissolved oxygen gradient field generated by the differentiated aeration system, this couples the hydrolysis-acidification, nitrification-denitrification, and other biochemical reactions in a spatial dimension. When the treatment load fluctuates, the variable flow guidance mechanism adjusts the angle of the guide plates to change the tangential velocity component of the water flow. Simultaneously, the weir in the adjustable on / off zone automatically adjusts its opening based on pressure sensor signals, achieving dynamic optimization of the hydraulic residence time within the reactor. Compared to traditional sequencing batch reactors, this system can improve the COD removal rate per unit volume by more than 40%, and its resistance to shock loads is significantly enhanced, maintaining stable effluent quality even when the influent COD fluctuates within a range of ±30%.

[0033] In this embodiment, the operation process of the papermaking wastewater treatment device is as follows: After pretreatment, the wastewater enters the hydrolysis zone 1 at a flow rate of 0.3-0.5 m / s. A transition zone with a width of 800 mm is set between the hydrolysis zone 1 and the dynamic transition section 21. Three sets of DN300 sludge return pipe groups are arranged at the bottom of the transition zone. The pipe groups are equipped with a dual redundant return system of screw conveyor and air lift device, which returns the activated sludge settled at the end of the dynamic transition section 21 to the front end of the hydrolysis zone 1 at a flow rate of 5-8 m³ / h. The wastewater generates reciprocating turbulence with an amplitude of 35 cm in the sawtooth channel formed by the baffle enhancement component 11. At this time, the hydrolytic bacteria decompose lignin under the flow state of Reynolds number Re=5200. After a residence time of 3.54 hours, the wastewater enters the dynamic transition section 21. The series anoxic zone 211 of the dynamic transition section 21 is divided into anoxic zone one with a residence time of 1.01 hours and anoxic zone two with a residence time of 2.37 hours. The two zones are connected by an adjustable on / off zone 212. The opening of the liftable weir 26 in the two 5000mm wide adjustment units of this zone is adjusted according to the real-time data of the pressure sensor 27: when the COD of the influent exceeds 8000mg / L, the control system will reduce the height of the weir 26 to 70% of the design value, thereby increasing the effective volume of the on / off zone by 15%. At the same time, it will trigger the sludge return pipe group to accelerate the operation, increasing the return ratio from 12% to 18%, so as to avoid the sludge load from exceeding the critical value of 0.15kgCOD / (kgMLSS·d). The angle adjustment controller 25 dynamically adjusts the deflection angle of the arc-shaped guide plate 23 according to the change of influent flow rate. When the flow rate fluctuates by ±20%, the inlet velocity of the fixed functional section 22 is kept stable at 0.25±0.03m / s. The gradient change of the spacing of the guide ribs 231 causes the water flow to form a rotating flow state with a tangential acceleration of 0.6m / s² at the end of the plate. This flow state interacts with the bubble group generated by the umbrella-shaped diffuser aerator a1. When the height of the guide rib h=0.2DD=150mm, the bubble residence time is extended to 28 seconds and the oxygen utilization rate is increased to 22%. In the stepped aerobic zone group 222, the umbrella-shaped diffuser in the first swirl aeration zone a generates a bubble cluster with a diameter of Φ3-5mm at a rotation speed of 45r / min. The ceramic membrane layer b1 in the second microporous aeration zone b outputs microbubbles with a diameter of Φ0.8-1.2mm at a gas pressure of 0.2MPa. The silicone flow-limiting sleeve c1 in the third diffusion aeration zone c increases the airflow velocity gradient from 5m / s to 15m / s. The aeration heads in the three zones are arranged at a 25° angle difference to form a superimposed flow field, generating a dissolved oxygen gradient of 0.5-4.2mg / L in the width direction of the pool, so that the ammonia nitrogen removal rate of nitrifying bacteria reaches 0.82kgN / (m³·d) when MLSS=3800mg / L. During the operation of the deoxygenation zone 3, the gas-liquid countercurrent flow field formed by the top umbrella-shaped gas collection hood and the bottom aeration pipe reduces the dissolved oxygen concentration from 4.5mg / L to below 0.3mg / L within 15 minutes, while recovering 65% of the methane component in the biogas.In practical applications, the following should be noted: the blade gap of the screw conveyor in the sludge return pipe group should be maintained at 3-5mm to prevent fibrous materials from entangled. When the drive current is detected to exceed the rated value by 15%, the air-lift mode should be automatically switched. The ceramic membrane layer b1 needs to be acid-washed monthly with a citric acid solution of pH=2 for 30 minutes, and the membrane flux decay rate should be controlled within 5% / month. The lifting guide rail of the water-retaining weir 26 in the adjustable on / off zone 212 needs to be injected with corrosion-resistant grease every quarter to prevent hydraulic oil emulsification from causing positioning accuracy deviations to exceed ±10mm. In an alternative implementation, a jet pump can be used instead of a screw conveyor for the sludge return pipe assembly, but the diameter of the return pipe needs to be increased to DN400 to compensate for head loss; the guide ribs 231 can be made of fiberglass through molding, with the rib height tolerance controlled within ±0.5mm, and the torque output parameters of the angle adjustment controller 25 need to be adjusted accordingly; the aeration head arrangement of the stepped aerobic zone group 222 can be changed to a radially divergent layout, in which case the angle difference between the three zones needs to be adjusted to 15° to meet the flow field coverage requirements. Production data shows that when treating papermaking wastewater with COD=12000mg / L and TN=350mg / L, the device stabilizes the dissolved oxygen in the anoxic zone at 0.2-0.5mg / L by dynamically adjusting the opening of the weir 26, and with the gradient aeration in the aerobic zone, the compliance rate of effluent COD≤80mg / L and TN≤15mg / L exceeds 98%, and the energy consumption per ton of water treated is reduced by 1.2kW·h compared with the traditional process. The dual-mode design of the transition zone sludge return system enables the device to maintain a return sludge concentration of 8000-12000 mg / L and an SVI value controlled within the ideal range of 80-120 mL / g even when the influent SS fluctuates to 2000-5000 mg / L. Regarding the coupling control of the angle of the guide plate 23 and the aeration intensity, when the influent C / N ratio is lower than 8:1, the deflection angle of the guide plate needs to be increased by 5°, while the air volume in the third diffusion aeration zone c is reduced by 20% to enhance denitrification. Special attention should be paid during installation: the installation error of the sawtooth channel of the baffle enhancement component 11 must be controlled within ±2 mm to avoid short-circuiting of the water flow; the axial clearance of the universal joint 24 should be adjusted to 0.1-0.3 mm to ensure that the rotation angle accuracy of the guide plate 23 reaches ±0.5°; the joint between the ceramic membrane layer b1 and the aeration pipe must use a fluororubber sealing ring with a pressure resistance rating of not less than 0.6 MPa. In a case of continuous operation for 180 days, the device demonstrated good resistance to shock loads. When the influent flow rate increased by 30% instantaneously for 4 hours, the flow rate was reduced by 150mm through the weir 26 and the reflux ratio was increased to 22% in conjunction with the flow rate, and the fluctuation of the effluent water quality was less than 5%.

Claims

1. A papermaking wastewater treatment device, comprising a hydrolysis zone (1), a biochemical reaction group (2) and an oxygen depletion zone (3), characterized in that: the biochemical reaction group (2) is provided with alternating dynamic transition sections (21) and fixed function sections (22) along the water flow direction; at least one of the dynamic transition sections (21) is provided with a variable guide mechanism; each fixed function section (22) is differentially integrated with an aeration system, and the gas output directions of adjacent aeration systems form an angle difference.

2. The papermaking effluent treatment apparatus as claimed in claim 1, wherein: The dynamic transition section (21) comprises a series of anoxic zones (211) and adjustable on-off zones (212), and the fixed function section (22) comprises an anaerobic reaction zone (221) and a stepped aerobic zone group (222).

3. The papermaking wastewater treatment apparatus according to claim 1, characterized by: The variable guide mechanism is composed of multiple arc guide plates (23), and each guide plate is connected to an angle adjustment controller through a universal shaft (24).

4. The papermaking effluent treatment apparatus as claimed in claim 2, wherein: The stepped aerobic zone group (222) includes a first cyclone aeration zone (a), a second microporous aeration zone (b), and a third diffusion aeration zone (c), and the axes of the aeration heads of the three zones form an angle of 10-35° with each other.

5. The papermaking effluent treatment apparatus as claimed in claim 3, wherein: The inner side of the arc guide plate (23) is provided with guide ribs (231), and the rib spacing decreases along the water flow direction by Δ=0.2L-0.5L, where L is the length of the plate body.

6. The papermaking effluent treatment apparatus as claimed in claim 2, wherein: The adjustable on-off zone (212) is provided with a liftable water retaining weir (26), the surface of the weir body is inlaid with a pressure sensor, and the weir body is in communication with the bottom of the hydrolysis zone (1).

7. The papermaking effluent treatment apparatus as claimed in claim 4, wherein: The first cyclone aeration zone (a) uses an aeration head (a1) with an umbrella-shaped diffusion cover, and the aeration pipe of the second microporous aeration zone (b) is coated with a ceramic membrane layer (b1).

8. The papermaking effluent treatment apparatus as claimed in claim 5, wherein: The protrusion height h of the guide rib (231) and the opening degree D of the umbrella-shaped diffusion cover satisfy h=0.15D-0.3D.

9. The papermaking effluent treatment apparatus as claimed in any one of claims 1 to 7, wherein: The hydrolysis zone (1) is provided with a baffling reinforcement assembly (11) inside, which forms a zigzag water flow channel with an amplitude of 30-50 cm.

10. The papermaking effluent treatment apparatus as claimed in claim 4, wherein: The aeration pipe of the third diffusion aeration zone (c) is equipped with a silica gel flow limiting sleeve (c1), and the sleeve body is provided with a tapered through hole.

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