Cosmetic wastewater treatment device with synergy of electrolysis and nanometer air floatation

Abstract

The utility model relates to the technical field of sewage treatment, and particularly discloses a cosmetic wastewater treatment device with synergy of electrolysis and nano air floatation, which comprises an electrolytic tank with a cathode electrode plate, an anode electrode plate and a PTFE (polytetrafluoroethylene) sleeve stirrer, a nano bubble air floatation tank, an anaerobic tank, a contact oxidation tank and an MBR (membrane bioreactor) membrane treatment tank, water enters the electrolytic tank through a wastewater inlet, the nano-bubble air flotation tank is communicated with the bottom of the electrolytic tank through an electrolytic tank flow guide partition plate, an air flotation nano-bubble generator is arranged, and scum is scraped out or flows back through a chain plate type scum scraper; the anaerobic tank is communicated with the nano-bubble air floatation tank through an air floatation tank water outlet, and an anaerobic tank stirrer and a flow guide partition plate are arranged in the anaerobic tank; the contact oxidation tank is communicated with the anaerobic tank through an anaerobic tank water outlet, and is internally provided with a three-dimensional elastic filler and a contact oxidation tank nano bubble generator; and the MBR membrane treatment tank is communicated with the contact oxidation tank through a water outlet pipe of the contact oxidation tank.

Description

TECHNICAL FIELD

[0001] The utility model relates to sewage treatment technical field, concretely relates to a cosmetic wastewater treatment device of electrolytic cooperation nanometer air floatation. BACKGROUND

[0002] At present, the treatment technology of cosmetic wastewater mainly depends on traditional physical, chemical and biological treatment methods, such as physical filtration, chemical flocculation and biological degradation. These methods have achieved wastewater treatment effect to a certain extent, but still have some technical defects and limitations.

[0003] For example, the electrode is easy to passivate in the electrolysis-air floatation combined process: the iron-carbon electrode is easy to corrode and scale, and the service life is short (<6 months), so the electrode plate needs to be replaced frequently; the energy consumption is high: the dissolved gas pump needs to maintain 0.5kWh / m 3 High energy consumption, and the bubble diameter is large (>50μm), the adsorption efficiency of nanoscale colloids is low (only 60%).

[0004] The biological contact oxidation-MBR process is difficult to degrade organic matter, and no electrolysis or chemical oxidation pretreatment is set, so that macromolecules such as silicone oil and perfume directly enter the biological unit, causing sludge bulking (SVI>150mL / g). Membrane pollution is serious: the MBR membrane backwashing period is short (≤4h), and frequent chemical cleaning (sodium hypochlorite dosage>50mg / L) is needed, and the membrane life is only 6-12 months.

[0005] The reagent cost is high in coagulation sedimentation and Fenton oxidation technology: the Fenton reagent dosage needs to reach more than 2.1 times of the theoretical value (H2O2 / COD ratio>2.12), and the operation cost reaches 1.2 yuan / m 3 . Secondary pollution risk: after mixing iron sludge and chemical sludge, it is difficult to dewater (moisture content>95%), and the disposal cost increases.

[0006] The existing technology has the problems of process fragmentation, low efficiency, high energy consumption and secondary pollution risk, so it is urgent to provide a new wastewater treatment device. INVENTION CONTENTS

[0007] The utility model provides a cosmetic wastewater treatment device of electrolytic cooperation nanometer air floatation, aims at solving the treatment problem of refractory organic matter (such as perfume, emulsifier, oil) and suspended matter in cosmetic wastewater, and aims at the defects of traditional technology, such as easy passivation of electrolytic cell electrode, low removal rate of nanoscale colloids in air floatation process and poor tolerance of biological unit to surfactant. The technology belongs to wastewater treatment technology in the field of environmental engineering, and specifically relates to a utility model device integrating electrolysis, nanometer air floatation and biological cooperative treatment process, which is suitable for high-concentration organic wastewater treatment in cosmetic, daily chemical and other industries, and realizes efficient and low-consumption wastewater treatment through structure optimization and intelligent control.

[0008] The utility model discloses a technical scheme to solve the above technical problems:

[0009] A cosmetic wastewater treatment device of electrolysis and nanometer air floatation cooperation, comprising electrolytic cell, nanometer bubble air floatation tank, anaerobic tank, contact oxidation tank and MBR membrane treatment tank with cathode electrode plate and anode electrode plate and PTFE sleeve stirrer arranged in sequence.

[0010] The electrolytic cell is connected with the direct current pulse power source through the wastewater inlet.

[0011] The nanometer bubble air floatation tank is communicated with the electrolytic cell bottom through the electrolytic cell flow guide baffle, and is provided with the air floatation nanometer bubble generator.

[0012] The anaerobic tank is communicated with the nanometer bubble air floatation tank through the air floatation tank water outlet, and is provided with the anaerobic tank stirrer and flow guide baffle.

[0013] The contact oxidation tank is communicated with the anaerobic tank through the anaerobic tank water outlet, and is provided with the three-dimensional elastic filler and contact oxidation tank nanometer bubble generator.

[0014] The MBR membrane treatment tank is communicated with the contact oxidation tank through the contact oxidation tank water outlet pipe, and is provided with the curtain type hollow fiber ultrafiltration membrane, MBR nanometer bubble generator, mixed liquid reflux pump, dissolved oxygen instrument, turbidimeter, ORP sensor, liquid level meter and flow meter.

[0015] In a specific embodiment, the cathode electrode plate and anode electrode plate are coated with a noble metal oxide catalytic layer on a stainless steel substrate, and the electrode spacing is 10-20 mm.

[0016] In a specific embodiment, the PTFE sleeve stirrer is a variable speed adjustment type, with a rotating speed range of 50-300 rpm, and a wear-resistant coating is coated on the stirring blade.

[0017] In a specific embodiment, the air floatation nanometer bubble generator, MBR nanometer bubble generator and contact oxidation tank nanometer bubble generator are all Venturi-cyclone combined structures.

[0018] In a specific embodiment, the nanometer bubble air floatation tank is provided with an electric field gradient plate matched with the electrolytic cell electrode polarity, so that the charged pollutants are directionally migrated to the nanometer bubble aggregation area.

[0019] In a specific embodiment, a PLC automation control unit is further included, which is electrically connected with the dissolved oxygen meter, turbidity meter, ORP sensor, liquid level meter and flow meter, and dynamically adjusts electrolysis current, gas float dissolved gas pressure, aeration fan rotating speed and mixed liquid reflux pump flow according to real-time sensing signals and fuzzy PID algorithm.

[0020] The utility model discloses the beneficial effect lies in: 1. traditional dissolved air flotation process relies on dissolved air pump (bubble diameter > 50um), and adsorption efficiency of nanometer colloidal and charged pollutant is low (only 60%).

[0021] Nanometer bubble (< 100nm): utilize small size bubble to enhance pollutant adsorption capacity, and removal rate is improved to 92%;

[0022] Electric field cooperation: the charged characteristics of pollutant after electrolysis match with bubble rising path, and adsorption efficiency is strengthened.

[0023] 2. Existing biological process (such as hydrolysis acidification-contact oxidation-MBR) causes refractory organic matter (such as silicone oil, perfume) residue due to lack of pretreatment, and sludge bulking (SVI > 150ml / g) and MBR membrane pollution (backwashing period ≤ 4h) are caused.

[0024] Anaerobic tank acid-proof design: lined with HDPE anticorrosive layer, and pH 4-10 fluctuation is resisted, and the problem of surfactant inhibition is solved;

[0025] Stereoscopic elastic filler: specific surface area ≥ 300m 2 / m 3 , and microbial load is improved by 50%, and complex organic matter degradation is accelerated.

[0026] 3. Traditional process unit (electrolytic cell, air floatation tank, biological tank) is independently designed, and process is long, covers a large area (such as UASB + SBR covers an area of > 100m 2 ) and relies on manual control. The utility model is optimized through modular frame and PLC linkage system:

[0027] Integrated equipment: electrolytic cell, air floatation slag removal tank and biological unit are integrated in ≤ 10m × 3m × 3m frame, and area covered is reduced by 30%;

[0028] Intelligent backflush and parameter linkage: based on transmembrane pressure difference (TMP), MBR backflush frequency is dynamically adjusted, and membrane life is extended to 2 years.

[0029] 4. Existing technology (such as coagulation-Fenton process) has high reagent cost (2-5 yuan / ton of water) and large sludge yield (8kg dry sludge / ton of water). The utility model is improved through sludge reflux and resource design:

[0030] Scum backflow system: the water content of the scum scraped by the air floatation tank is less than 95%, which can be backflowed to the electrolytic cell to assist the reaction and reduce sludge discharge;

[0031] Low energy consumption process: the comprehensive energy consumption is reduced by 50% compared with the traditional process, and the chemical pollution risk of Fenton reagent is avoided. BRIEF DESCRIPTION OF DRAWINGS

[0032] In order to more clearly illustrate the technical solutions of the embodiments or the prior art, the following will briefly introduce the drawings needed to be used in the embodiment or the prior art description. Obviously, the drawings in the following description are only a part of the embodiments of the present application, and for those skilled in the art, other drawings can be obtained without creative labor on the basis of the provided drawings.

[0033] Figure 1 The structure of the present application is shown in the structure diagram;

[0034] In the drawings: 1 - chain plate type scum scraper; 2 - cathode electrode plate; 3 - anode electrode plate; 5 - PTFE sleeve mixer; 6 - electrolytic cell; 8 - nanometer bubble air floatation tank; 9 - anaerobic tank stirrer; 11 - air floatation nanometer bubble generator; 12 - MBR nanometer bubble generator; 13 - contact oxidation tank nanometer bubble generator; 14 - three-dimensional elastic filler; 15 - MBR curtain type membrane; 17 - temperature sensor; 18 - turbidimeter; 19 - MBR membrane treatment tank; 22 - ORP sensor; 23 - liquid level meter; 24 - mixed liquid backflow pump; 25 - dissolved oxygen meter; 26 - flow meter; 27 - contact oxidation tank; 29 - anaerobic tank; 31 - scum outlet tank. DETAILED DESCRIPTION

[0035] The technical solutions in the embodiments of the present application will be described clearly and completely in combination with the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor are within the scope of protection of the present application.

[0036] Embodiment one

[0037] A cosmetic wastewater treatment device with electrolysis and nanometer air floatation comprises, which are sequentially arranged: an electrolytic cell 6 with cathode electrode plate 2 and anode electrode plate 3 and PTFE sleeve mixer 5, nanometer bubble air floatation tank 8, anaerobic tank 29, contact oxidation tank 27 and MBR membrane treatment tank 19;

[0038] The electrolytic cell 6 is watered through the wastewater inlet 4, and the electrode plates are respectively connected with direct current pulse power sources on both sides, which are used for generating ·OH free radicals and charging organic pollutants;

[0039] The nanobubble air floatation tank 8 is communicated with the bottom of the electrolytic tank 6 through the electrolytic tank flow guide baffle 10, and is provided with an air floatation nanobubble generator 11, and the floating dregs are scraped out or backflowed through the chain plate type slag scraper 1;

[0040] The anaerobic tank 29 is communicated with the nanobubble air floatation tank 8 through the air floatation tank water outlet 30, and is internally provided with an anaerobic tank stirrer 9 and a flow guide baffle 7, and is used for preliminary degradation of organic matter and nitrogen and phosphorus;

[0041] The contact oxidation tank 27 is communicated with the anaerobic tank 29 through the anaerobic tank water outlet 28, and is internally provided with a three-dimensional elastic filler 14 and a contact oxidation tank nanobubble generator 13, and is used for biological degradation and increase of dissolved oxygen;

[0042] The MBR membrane treatment tank 19 is communicated with the contact oxidation tank 27 through the contact oxidation tank water outlet pipe 21, and is internally provided with a curtain type hollow fiber ultrafiltration membrane 15, and is provided with an MBR nanobubble generator 12, a mixed liquid backflow pump 24, and a dissolved oxygen meter 25, a turbidity meter 18, an ORP sensor 22, a liquid level meter 23 and a flow meter 26, and is used for membrane biological reaction, solid-liquid separation and online monitoring and automatic control.

[0043] The cathode electrode plate 2 and the anode electrode plate 3 adopt a stainless steel substrate surface coated with a noble metal oxide catalytic layer, and the electrode spacing is 10-20 mm, so as to improve the electrolysis efficiency and inhibit electrode passivation.

[0044] The PTFE sleeve stirrer 5 is a variable speed adjustment type, and the rotating speed range is 50-300 rpm, and a wear-resistant coating is coated outside the stirring paddle, so as to enhance the hydraulic shear dispersion effect of macromolecular organic matter.

[0045] The air floatation nanobubble generator 11, the MBR nanobubble generator 12 and the contact oxidation tank nanobubble generator 13 all adopt a Venturi-cyclone combined structure, and can produce nanobubbles with an average diameter of less than 100 nm at 0.1-0.3 kWh / m 3 under energy consumption.

[0046] The nanobubble air floatation tank 8 is internally provided with an electric field gradient plate, and is matched with the electrode polarity of the electrolytic tank 6, so that the charged pollutants are directionally migrated to the nanobubble aggregation area, so as to realize electric field-air floatation synergistic adsorption.

[0047] Further comprising a PLC automatic control unit, which is electrically connected with the dissolved oxygen meter 25, the turbidity meter 18, the ORP sensor 22, the liquid level meter 23 and the flow meter 26, and dynamically adjusts the electrolysis current, the air floatation gas solubility pressure, the rotating speed of the aeration blower 28 and the flow of the mixed liquid backflow pump 24 according to the real-time sensing signal fuzzy PID algorithm.

[0048] The process flow is as follows: wastewater enters the electrolytic cell 6 from the wastewater inlet 4, is fully stirred by the PTFE sleeve stirrer 5, and the hydroxyl radicals are excited by the pulse current of the cathode electrode plate 2 and the anode electrode plate 3 to decompose macromolecular organic matter (such as silicone oil and LAS). After electrolysis, the pollutants are negatively charged and migrate to the nanobubble air flotation tank 8 under the action of the electric field, thereby improving the air flotation adsorption efficiency. The wastewater flows through the electrolytic cell flow guide partition plate 10 and flows into the nanobubble air flotation tank 8. The nanobubbles generated by the mixed air flotation nanobubble generator 11 make the air flotation sludge float to the surface. The chain plate type sludge scraper 1 (stainless steel chain plate type) scrapes the floating sludge into the sludge outlet tank 31 at a speed of 0.1 m / min. Part of the floating sludge is returned to the electrolytic cell through the pipeline to assist the reaction.

[0049] The treated wastewater flows out of the air flotation tank through the air flotation tank outlet 30, flows into the anaerobic tank 29, and removes part of the organic pollutants and nitrogen and phosphorus substances in the wastewater. After that, the wastewater flows out of the anaerobic tank through the anaerobic tank outlet 28, flows into the contact oxidation tank 27, and generates nanobubbles by the nanobubble generator 13 in the contact oxidation tank according to the parameters of the dissolved oxygen meter 25. The dissolved oxygen content in the wastewater is adjusted, and the wastewater is contacted and decomposed by the microorganism flora on the three-dimensional elastic filler 14 to further remove organic pollutants and nitrogen and phosphorus substances. The wastewater flows into the MBR membrane treatment tank 19 through the contact oxidation tank outlet pipe 21 under the control of the liquid level meter 23. The wastewater fully reacts with the MBR nanobubble generator 12. The activated sludge at the bottom of the treatment tank is returned to the biochemical system by the mixed liquid return pump 24 to improve the degradation effect.

[0050] The reflux ratio is controlled by observing the flow meter 26, and the process is flexibly adjusted and controlled by the temperature sensor 17, the turbidimeter 18, and the ORP sensor 22 to meet different water qualities. The treated wastewater is filtered through the MBR curtain membrane 15 and discharged stably through the MBR membrane outlet pipe 20.

[0051] The various embodiments in the specification are described in a progressive manner, and each embodiment focuses on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other. For the device disclosed in the embodiments, since it corresponds to the method disclosed in the embodiments, the description is relatively simple, and the related parts can be referred to the method part.

[0052] The above description of the disclosed embodiments enables a person skilled in the art to implement or use the present application. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein can be implemented in other embodiments without departing from the spirit or scope of the present application. Therefore, the present application will not be limited to the embodiments shown herein, but will conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A cosmetic wastewater treatment device using electrolysis in conjunction with nanobubble flotation, characterized by, The device comprises electrolytic tank, nanobubble air flotation tank, anaerobic tank, contact oxidation tank and MBR membrane treatment tank with cathode electrode plate, anode electrode plate and PTFE sleeve stirrer arranged in sequence. The electrolytic tank is connected with direct current pulse power source through the wastewater inlet. The nanobubble air flotation tank is communicated with the electrolytic tank through the guide baffle at the bottom of the electrolytic tank, and is provided with air flotation nanobubble generator and chain plate type slag scraper. The anaerobic tank is communicated with the nanobubble air flotation tank through the air flotation tank outlet, and is provided with anaerobic tank stirrer and guide baffle. The contact oxidation tank is communicated with the anaerobic tank through the anaerobic tank outlet, and is provided with three-dimensional elastic filler and contact oxidation tank nanobubble generator. The MBR membrane treatment tank is communicated with the contact oxidation tank through the contact oxidation tank outlet, and is provided with curtain type hollow fiber ultrafiltration membrane, MBR nanobubble generator, mixed liquid reflux pump, dissolved oxygen meter, turbidity meter, ORP sensor, liquid level meter and flow meter.

2. The apparatus of claim 1, wherein, The cathode electrode plate and the anode electrode plate are made of stainless steel substrate coated with noble metal oxide catalytic layer, and the electrode spacing is 10-20 mm.

3. The apparatus of claim 1, wherein, The PTFE sleeve stirrer is a variable speed adjustment type, and the rotating speed ranges from 50 rpm to 300 rpm.

4. The apparatus of claim 1, wherein, The air flotation nanobubble generator, MBR nanobubble generator and contact oxidation tank nanobubble generator are all Venturi-cyclone combined structures.

5. The apparatus of claim 1, wherein, The nanobubble air flotation tank is provided with electric field gradient plate matched with the electrode polarity of the electrolytic tank, so that the charged pollutants are oriented to migrate to the nanobubble aggregation area.

6. The apparatus of claim 1, wherein, The device further comprises PLC automatic control unit electrically connected with the dissolved oxygen meter, turbidity meter, ORP sensor, liquid level meter and flow meter, and dynamically adjusts the electrolytic current, air flotation gas pressure, aeration fan rotating speed and mixed liquid reflux pump flow according to real-time sensing signal fuzzy PID algorithm.

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