WO2021063425A1 - 一种高cod含酚类污水的处理系统及其处理方法 - Google Patents

一种高cod含酚类污水的处理系统及其处理方法 Download PDF

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WO2021063425A1
WO2021063425A1 PCT/CN2020/125838 CN2020125838W WO2021063425A1 WO 2021063425 A1 WO2021063425 A1 WO 2021063425A1 CN 2020125838 W CN2020125838 W CN 2020125838W WO 2021063425 A1 WO2021063425 A1 WO 2021063425A1
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tank
biochemical
wastewater
sewage
treatment system
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French (fr)
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蒋国强
孙百亚
姜伟伟
赵跃
俞晔虎
万鹏
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南通百川新材料有限公司
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/123—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using belt or band filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/125—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using screw filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C02F2101/345—Phenols
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes

Definitions

  • the invention belongs to the field of sewage treatment, and particularly relates to a treatment system and a treatment method for high-COD phenol-containing sewage.
  • Phenol also known as carbolic acid and hydroxybenzene, is the simplest phenolic organic compound, a weak acid. It is a colorless crystal at room temperature and toxic. Phenol is a common chemical and an important raw material for the production of certain resins, fungicides, preservatives, and drugs (such as aspirin). Phenol is corrosive, slightly soluble in water at room temperature, and easily soluble in organic solutions; when the temperature is higher than 65°C, it can be miscible with water in any ratio. Its solution can be washed on the skin with alcohol, and phenol is pink when exposed to the air.
  • the technical problem to be solved by the present invention is to provide a solution that can solve the problem that the traditional sewage treatment system has poor system tolerance when the concentration of phenols fluctuates, which easily leads to unqualified external drainage after treatment; at the same time, it can effectively reduce the phenols in the product process wastewater.
  • the concentration of high-COD phenolic wastewater treatment system and its treatment method which significantly reduces the load of the subsequent biochemical system, and eliminates the problem of reduced biochemical system activity due to the accumulation of phenols.
  • the technical solution of the present invention is: a high-COD phenol-containing sewage treatment system, its innovation is: including a pretreatment system and a post-treatment system,
  • the pretreatment system includes a physicochemical pretreatment system and a biochemical pretreatment system, the physicochemical pretreatment system and the biochemical pretreatment system are connected in series or in parallel at the outlet end of the process wastewater, and then the process wastewater is pretreated sequentially or independently;
  • the post-treatment system is connected in series with the biochemical pre-treatment system and the pre-treated process wastewater is post-treated;
  • the physical and chemical pretreatment system is a steam stripping treatment system
  • the pretreatment system includes a physical and chemical adjustment tank A for adjusting the water quality and water volume of the process waste water in series, and a tank for treating phenols in the product process waste water.
  • the biochemical pretreatment system is a catalytic oxidation pretreatment system.
  • the pretreatment system includes an oil trap for isolating oily substances in process wastewater, a physical and chemical adjustment tank B for adjusting the water quality and quantity of process wastewater, which are connected in series.
  • Catalytic oxidation reactor for degrading high COD and reducing phenol content, inclined plate sedimentation tank for solid-liquid separation, and sludge thickening tank for thickening sludge at the bottom of the inclined plate sedimentation tank;
  • the input end is connected to the outlet end of the process wastewater, and the input end of the catalytic oxidation reactor is connected to the outlet end of the sewage from the stripping reactor;
  • the post-treatment system includes a biochemical adjustment tank for adjusting the water quality and volume of the supernatant of the sloping plate sedimentation tank or the supernatant of the biochemical sludge thickening tank in series, and the biochemical adjustment tank for adjusting the water after the biochemical adjustment tank.
  • the distribution tank that is mixed with the backwater of the contact oxidation tank, the contact oxidation tank for microbial decomposition, the intermediate tank for buffering wastewater after microbial decomposition, the water after microbial decomposition, and the backwater of the secondary sedimentation tank are used for reprocessing.
  • the aerobic tank for microbial decomposition the secondary sedimentation tank for separating activated sludge, the biochemical sludge thickening tank for thickening activated sludge, and the filter press for pressing and filtering the sludge, and the filter press
  • the water outlet end is also connected to the input end of the intermediate tank.
  • a method for treating high-COD-containing phenol-containing sewage by adopting the above-mentioned high-COD-containing phenol-containing sewage treatment system which is innovative in that: the treatment method includes the following steps:
  • Step 1 Physicochemical pretreatment:
  • the phenolic process wastewater is first passed through the physicochemical adjustment tank A to remove the suspended solids in the sewage, and the sewage is sent to the stripping reactor with a temperature of ⁇ 95°C. Stripping treatment is 3 ⁇ 5h.
  • phenols enter the falling film absorber from the top of the stripping reactor in gaseous phase.
  • the falling film absorber is cooled by circulating water at a temperature of 25 ⁇ 30°C to convert the phenols in the gas phase into Liquid phenols, and finally the liquid phenols are passed into the gas collector for collection, and the recovered phenolic solution can be used as raw material for production or boiler fuel according to the specific situation;
  • Step 2 Biochemical pretreatment: The sewage treated by the stripping reactor in step 1 is sent from the bottom of the stripping reactor to the catalytic oxidation reactor, and hydrogen peroxide, ferrous sulfate heptahydrate, and smallholder are added to the catalytic oxidation reactor.
  • the reaction temperature is 50 ⁇ 65°C
  • the reaction time is ⁇ 15 minutes
  • the phenol removal rate reaches 99%; then it is sent from the bottom of the catalytic oxidation reaction tank to the inclined plate sedimentation tank, and solidification is achieved by adding liquid caustic soda and PAM.
  • the bottom sludge is pumped to the sludge thickening tank, and the sludge is discharged after being filtered by the stacked screw filter press.
  • the PH value, COD and phenol of the supernatant in the inclined plate sedimentation tank The content meets the requirements of subsequent biochemical treatment;
  • Step 3 Post-treatment:
  • the supernatant in the inclined plate sedimentation tank is sent to the biochemical adjustment tank, which can adjust the water volume and quality of the sewage, and the sewage from the biochemical adjustment tank is sent to the distribution tank after pre-aeration and stirring ,
  • the distribution tank mixes the water in the regulating tank and the backwater of the contact oxidation tank, the sewage concentration decreases, and after the microorganisms in the contact oxidation tank are decomposed, it flows to the secondary sedimentation tank, and the secondary sedimentation tank separates the contact
  • the activated sludge in the effluent water of the oxidation tank, the return water in the secondary sedimentation tank is returned to the aerobic tank, and the remaining sludge in the secondary sedimentation tank is filtered through the biochemical sludge thickening tank and discharged by the belt filter press Sludge; at this time, the sewage in the upper and middle part of the secondary sedimentation tank meets the national third-level sewage discharge standard.
  • the ratio of hydrogen peroxide to the volume of sewage in the catalytic oxidation reactor is set to 1:100, and the molar ratio of hydrogen peroxide to ferrous sulfate heptahydrate is 1:3.
  • the pH value of the sewage discharged from the inclined plate sedimentation tank is 5-8, the COD is less than or equal to 3000 mg/L, and the phenol content is less than or equal to 30 mg/L.
  • the pH value of the sewage discharged from the secondary settling tank is 6-9
  • the COD is ⁇ 500mg/L
  • the aldehyde content is ⁇ 5mg/L, which meets the national third-level sewage discharge standard.
  • the high-COD phenol-containing wastewater treatment system of the present invention adds a physical and chemical pretreatment system and a biochemical pretreatment system to the general wastewater treatment system; the phenol in the wastewater is removed by catalytic oxidation, and the wastewater can be further processed. Biochemical treatment; the phenolic solution recovered by the gas collector can be used as a raw material for production or as a boiler heat source for incineration.
  • the phenol-containing sewage after steam stripping treatment can be further subjected to conventional biochemical treatment and treatment After the sewage PH value is 6-9, COD ⁇ 500mg/L, phenol content ⁇ 5mg/L, it reaches the national third-level sewage discharge standard;
  • the physical and chemical pretreatment system is a steam stripping pretreatment system, which can effectively reduce the concentration of phenols in the product process wastewater and significantly reduce the load of the subsequent biochemical system;
  • the catalytic oxidation pretreatment system degrades the remaining phenols in the sewage under the action of hydrogen peroxide and ferrous sulfate heptahydrate to generate small molecular organics that can be treated by the biochemical system.
  • the removal rate of phenols can reach 99%, which is effective It avoids the reduction of sludge activity in the biochemical tank due to the accumulation of phenols; at the same time, the contact oxidation tank can be used to mix the sewage uniformly through air flotation and float the suspended matter in the sewage for removal;
  • the present invention can be used to separate other heat-sensitive and water-soluble substances in the product process wastewater at the same time through the setting of process parameters.
  • the removal rate of phenols is 75%, which reduces the subsequent biochemical properties.
  • the load of the system is 75%, which reduces the subsequent biochemical properties.
  • Fig. 1 is a schematic structural diagram of a treatment system for high COD phenol-containing sewage according to the present invention.
  • the treatment system for high-COD phenolic wastewater in this embodiment includes a pretreatment system and a post-treatment system.
  • the pretreatment system includes a physical and chemical pretreatment system and a biochemical pretreatment system.
  • the physical and chemical pretreatment system and the biochemical pretreatment system are connected in series or in parallel.
  • the process wastewater is pretreated sequentially or independently; the post-treatment system is connected in series with the biochemical pretreatment system and the pre-treated process wastewater is post-treated.
  • the physicochemical pretreatment system is a steam stripping treatment system, which includes a physicochemical adjustment tank A1, which is connected in series for adjusting the water quality and quantity of process wastewater, and is used for processing product processes.
  • the biochemical pretreatment system is a catalytic oxidation pretreatment system, the pretreatment system includes an oil trap 5 connected in series for isolating oily substances in the process wastewater, and is used to adjust the water quality and quantity of the process wastewater
  • the input end of the grease trap 5 is connected to the outlet end of the process wastewater, and the input end of the catalytic oxidation reactor 7 is connected to the outlet end of the sewage from
  • the post-treatment system includes a biochemical adjustment tank 10 connected in series for adjusting the water quality and volume of the supernatant of the sloping plate sedimentation tank or the supernatant of the biochemical sludge thickening tank, and the water after the adjustment of the biochemical adjustment tank 10
  • the distribution tank 11 mixed with the backwater of the contact oxidation tank 12, the contact oxidation tank 12 for microbial decomposition, the intermediate tank 13 for buffering wastewater after microbial decomposition, the water after microbial decomposition, and the secondary sedimentation tank 15
  • the aerobic tank 14 for microbiological decomposition of the backwater again, the secondary settling tank 15 for separating activated sludge, the biochemical sludge thickening tank 16 for concentrating the activated sludge, and the pressure filter for sludge
  • the filter press 17 and the water outlet end of the filter press 17 are also connected to the input end of the intermediate tank 13.
  • Step 1 Physical and chemical pretreatment:
  • the phenol-containing process wastewater is first removed from the suspended solids in the sewage through the physical and chemical adjustment tank A1, and the sewage is sent to the stripping reactor 2 with a temperature of ⁇ 95°C
  • the stripping treatment is carried out for 3 to 5 hours.
  • the phenols enter the falling film absorber 3 from the top of the stripping reactor 2 in the form of gas phase.
  • the falling film absorber 3 is cooled by circulating water at a temperature of 25-30°C to cool the gas phase
  • the phenols are converted into liquid phenols, and finally the liquid phenols are passed into the gas collector 4 for collection.
  • the recovered phenolic solution can be used as production raw material or boiler fuel according to the specific situation;
  • Step 2 Biochemical pretreatment: the sewage treated by stripping reactor 2 in step 1 is sent from the bottom of stripping reactor 2 to catalytic oxidation reactor 7, and hydrogen peroxide and heptahydrate sulfuric acid are added to catalytic oxidation reactor 7. Ferrous and small molecule catalysts, the reaction temperature is 50 ⁇ 65°C, and the reaction time is ⁇ 15 minutes, the removal rate of phenols reaches 99%; then it is sent from the bottom of the catalytic oxidation reactor 7 to the inclined plate sedimentation tank 8, through the addition of liquid Alkali and PAM realize solid-liquid separation. The bottom sludge is pumped to the sludge thickening tank 9, and the sludge is discharged after being filtered by a stacked screw filter press. At this time, the supernatant in the inclined plate sedimentation tank 8 The PH value, COD and phenol content of the liquid meet the requirements of subsequent biochemical treatment;
  • Step 3 Post-processing:
  • the supernatant in the inclined plate sedimentation tank 8 is sent to the biochemical adjustment tank 10, which can adjust the water volume and quality of the sewage, and the sewage of the biochemical adjustment tank 10 is stirred by pre-aeration
  • the distribution tank 11 mixes the water in the biochemical adjustment tank 10 with the backwater of the contact oxidation tank 12, the sewage concentration decreases, and after the microorganisms in the contact oxidation tank 12 decompose, it flows to
  • the secondary settling tank 15 separates the activated sludge in the effluent from the contact oxidation tank 12, the return water in the secondary settling tank 15 returns to the aerobic tank 14, and the remaining sludge in the secondary settling tank 15 is passed through
  • the biochemical sludge thickening tank 16 is filtered by a belt filter press 17 to discharge the sludge; at this time, the sewage in the upper and middle part of the secondary settling tank 15 meets the national third-level sewage discharge standard
  • the ratio of hydrogen peroxide to the volume of sewage in the catalytic oxidation reactor is set to 1:100, and the molar ratio of hydrogen peroxide to ferrous sulfate heptahydrate is 1:3.
  • the pH value of the sewage discharged from the inclined plate sedimentation tank is 5-8, COD ⁇ 3000mg/L, and aldehyde content ⁇ 30mg/L.
  • the pH value of the sewage discharged from the secondary settling tank is 6-9, the COD ⁇ 500mg/L, and the aldehyde content ⁇ 5mg/L, which meets the national third-level sewage discharge standard.
  • the above-mentioned treatment system treats high-COD-containing phenol-containing sewage, taking the phenol-containing sewage volume of 30m 3 /d, in which the COD value is 168200mg/L, the phenol content is about 226mg/L, and the PH value is about 6.4 as an example.
  • the specific steps of the method are as follows:
  • the first step, physical and chemical pretreatment In the steam stripping pretreatment system, the phenolic process wastewater is first removed from the suspended solids in the sewage through the physical and chemical adjustment tank A1, and the sewage is sent to the stripping reactor 2 for stripping treatment
  • the blow-off treatment pressure is 0.6MPa
  • the temperature is 95°C
  • the blow-off time is 4h.
  • the phenols enter the falling film absorber 3 from the top of the blow off reactor 2 in the gas phase, and the falling film absorber 3 is cooled by circulating water.
  • the phenols in the gas phase are converted into liquid phenols, and the circulating water temperature is 25-30°C; finally, the liquid phenols are passed into the gas collector 4 for collection, and the recovered phenol solution can be used as raw material for production or boiler fuel according to the specific situation. ; After treatment by the steam stripping device, the phenol content in the sewage drops to (10-20) mg/L;
  • the second step, biochemical pretreatment the sewage treated by the stripping reactor 2 in the first step is sent from the bottom of the stripping reactor 2 to the catalytic oxidation reactor 7, and hydrogen peroxide is added to the catalytic oxidation reactor 7.
  • Ferrous sulfate heptahydrate small molecule catalyst; the ratio of hydrogen peroxide to the volume of sewage is set to 1:100, the molar ratio of hydrogen peroxide to ferrous sulfate heptahydrate is 1:3, and the amount of catalyst is ten-thousandths of the quality of the influent.
  • the removal rate of phenols reaches 99%, and then it is sent from the bottom of the catalytic oxidation reactor to the mixing tank, and the excess hydrogen peroxide in the sedimentation tank is removed by adding liquid caustic soda and PAM.
  • the bottom sludge is pumped to the sludge thickening tank, and the sludge is discharged after being filtered by a stacked screw filter.
  • the third step, post-treatment the supernatant in the inclined plate sedimentation tank 8 in the second step is sent to the biochemical adjustment tank 10, the biochemical adjustment tank 10 can adjust the water volume and water quality of the sewage, and the sewage from the biochemical adjustment tank 10 passes through the pretreatment After aeration and stirring, it is sent to the distribution tank 11, which mixes the water in the biochemical adjustment tank 10 with the backwater of the contact oxidation tank 12, and the sewage concentration drops below 800mg/L.
  • the secondary settling tank 15 separates the activated sludge in the effluent of the contact oxidation tank 12, the return water in the secondary settling tank 15 returns to the aerobic tank 14, and the remaining sludge in the secondary settling tank 15 Then the sludge is discharged through the biochemical sludge thickening tank 16 through the belt filter press 17 and the sludge is discharged; at this time, the pH value of the sewage in the upper part of the secondary sedimentation tank is 7.6, COD 380mg/L, and the phenol content is 3.8mg/L , Reaching the national three-level sewage discharge standard.

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Abstract

一种高COD含酚类污水的处理系统及其处理方法，包括预处理系统和后处理系统，所述预处理系统包括物化预处理系统和生化预处理系统，所述物化预处理系统和生化预处理系统串联或并联在工艺废水的出水端，进而依次或独立对工艺废水进行预处理；所述后处理系统与生化预处理系统串联并对预处理后的工艺废水进行后处理。所述系统和方法解决了传统污水处理系统在酚类浓度波动时，系统耐受能力差，容易导致处理后外排水不合格的问题；同时有效降低产品工艺废水中酚类的浓度，显著减小后续生化系统的负荷，杜绝因酚类累积致使生化系统活性降低的问题。

Description

一种高COD含酚类污水的处理系统及其处理方法 技术领域
本发明属于污水处理领域，特别涉及一种高COD含酚类污水的处理系统及其处理方法。
背景技术
苯酚，又名石炭酸、羟基苯，是最简单的酚类有机物，一种弱酸。常温下为一种无色晶体，有毒。苯酚是一种常见的化学品，是生产某些树脂、杀菌剂、防腐剂以及药物(如阿司匹林)的重要原料。苯酚有腐蚀性，常温下微溶于水，易溶于有机溶液；当温度高于65℃时，能跟水以任意比例互溶。其溶液沾到皮肤上可用酒精洗涤，苯酚暴露在空气中呈粉红色。
不含酚类的高COD废水处理方法研究较多的是A/O、A2/O、CASS、SBR、UCT等，此类方法处理效果较好，无二次污染，该类方法的缺点如下：
(1)由于其主要利用活性污泥，能通过细菌分解、降解废水高浓度有机物，但酚类属于氧化性物质，能杀死活性细菌
(2)此类技术对污泥中细菌的活性要求较高，故要运用到实际工程上还有很大困难；
(3)从目前生物法处理高COD含酚类废水的研究可以看出，目前运行良好的处理方法中废水中的酚类只是低浓度的，而高COD含酚类废水因其较高的毒性，生物法无法处理。
高浓度(280mg/L左右)、对微生物有强毒性的酚类工艺废水，目前多采用大比例回流稀释生化的工艺，但因缺少有效的物化预处理，不仅增加了动力消耗，同时废水中酚类的累积会抑制生化池内污泥的活性；当发生上述因废水中酚类的累积致使生化池内污泥活性降低时，污水中酚类浓度的增高会导致生化池COD去除率远低于设计值，引起出水COD超标，生化系统处理能力明显降低，污水处理装置外排废水不达标。
发明内容
本发明要解决的技术问题是提供一种能够解决传统污水处理系 统在酚类浓度波动时，系统耐受能力差，容易导致处理后外排水不合格的问题；同时有效降低产品工艺废水中酚类的浓度，显著减小后续生化系统的负荷，杜绝因酚类累积致使生化系统活性降低的问题的高COD含酚类污水的处理系统及其处理方法。
为解决上述技术问题，本发明的技术方案为：一种高COD含酚类污水的处理系统，其创新点在于：包括预处理系统和后处理系统，
所述预处理系统包括物化预处理系统和生化预处理系统，所述物化预处理系统和生化预处理系统串联或并联在工艺废水的出水端，进而依次或独立对工艺废水进行预处理；
所述后处理系统与生化预处理系统串联并对预处理后的工艺废水进行后处理；
其中，所述物化预处理系统为蒸汽吹脱处理系统，该预处理系统包括依次串接的用于对工艺废水进行水质和水量调节的物化调节池A、用于处理产品工艺废水中酚类的吹脱反应器、用于将气相酚类转换成液相酚类的降膜吸收器以及用于收集液体酚类的收集器，且所述物化调节池A的输入端与工艺废水的出水端相连；
所述生化预处理系统为催化氧化预处理系统，该预处理系统包括依次串联的用于隔离工艺废水中油性物质的隔油池、用于对工艺废水进行水质和水量调节的物化调节池B、用于降解高COD及降低酚含量的催化氧化反应釜、用于固液分离的斜板沉淀池以及用于对斜板沉淀池底部污泥进行浓缩的污泥浓缩池；所述隔油池的输入端与工艺废水的出水端相连，所述催化氧化反应釜的输入端与吹脱反应器的污水的出水端相连；
所述后处理系统包括依次串联的用于对斜板沉淀池的上清液或生化污泥浓缩池的上清液进行水质和水量调节的生化调节池、用于将生化调节池调节后的水和接触氧化池的回水进行混合的配水池、用于微生物分解的接触氧化池、用于缓存微生物分解后废水的中间池、用于将微生物分解后的水和二沉池的回水进行再次微生物分解的好氧池、用于分离出活性污泥的二沉池、用于对活性污泥进行浓缩的生化污泥浓缩池以及用于对污泥压滤的压滤机，且压滤机的出水端还与中间池的输入端相连。
一种采用上述高COD含酚类污水的处理系统处理高COD含酚类污水的方法，其创新点在于：所述处理方法包括如下步骤：
步骤1：物化预处理：在蒸汽吹脱预处理系统中，含酚类工艺废水首先通过物化调节池A去除污水中上浮的悬浮物，并污水送至温度≤95℃的吹脱反应器中进行吹脱处理3～5h，吹脱后酚类以气相形式从吹脱反应器顶部进入降膜吸收器中，降膜吸收器通过温度为25～30℃的循环水冷却将气相的酚类转换成液相酚类，最后将液态酚类通入气体收集器中进行收集，回收的酚类溶液可以根据具体情况做生产原料或锅炉燃料；
步骤2：生化预处理：将步骤1中经吹脱反应器处理后的污水从吹脱反应器底部送至催化氧化反应釜中，向催化氧化反应釜中加入双氧水、七水硫酸亚铁、小分子催化剂，反应温度为50～65℃，反应时间≥15分钟时，酚类去除率达99％；然后从催化氧化反应釜底送至斜板沉淀池中，通过添加液碱、PAM，实现固液分离，底部污泥经泵送至所述污泥浓缩池中，经叠螺式压滤机压滤后排出污泥，此时斜板沉淀池中的上清液的PH值、COD及酚含量皆符合后续生化处理要求；
步骤3：后处理：步骤2中斜板沉淀池内的上清液送至生化调节池，生化调节池可对污水的水量和水质进行调节，生化调节池污水通过预曝气搅拌后送至配水池，所述配水池将所述调节池的水和所述接触氧化池的回水进行混合，污水浓度下降，经接触氧化池中微生物分解后，流至二沉池，该二沉池分离出接触氧化池出水中的活性污泥，二沉池中的回流水回流到好氧池中，二沉池中的剩余污泥则经所述生化污泥浓缩池经带式压滤机压滤后排出污泥；此时二沉池中上部的污水达到国家三级污水排放标准。
进一步地，所述步骤2中，催化氧化反应釜中双氧水与污水体积的比值设定为1：100，双氧水与七水硫酸亚铁的摩尔比为1:3。
进一步地，所述步骤2中，斜板沉淀池排出的污水PH值5-8，COD≤3000mg/L，酚类含量≤30mg/L。
进一步地，所述步骤3中，二沉池排出的污水PH值6-9，COD≤500mg/L，醛类含量≤5mg/L，达到国家三级污水排放标准。
本发明的优点在于：
(1)本发明高COD含酚类污水的处理系统，在一般的污水处理系统的基础上增设了物化预处理系统和生化预处理系统；经催化氧化出去污水中的苯酚，污水可以进一步进行常规的生化处理；经气体收集器回收的酚类溶液，可以作为生产原料、亦可作为锅炉热源，进行焚烧，同时经蒸汽吹脱处理后的含酚污水，污水可以进一步进行常规的生化处理，处理后污水PH值6-9，COD≤500mg/L，酚类含量≤5mg/L，达到国家三级污水排放标准；
(2)物化预处理系统为蒸汽吹脱预处理系统，可以有效降低产品工艺废水中酚类的浓度，显著减小后续生化系统的负荷；
(3)催化氧化预处理系统将污水中剩余的酚类在双氧水、七水硫酸亚铁作用下使酚降解，生成可供生化系统处理的小分子有机物，酚类去除率可达99％，有效避免了因酚类的累积致使生化池内污泥活性降低；同时接触氧化池可以用于通过气浮作用使污水混合均匀并使污水中的悬浮物上浮以便去除；
(4)本发明在吹脱处理中，通过工艺参数的设置，可同时用于产品工艺废水中其它热敏性能及水溶性能好的物质的分离，酚类去除率为75％，减小后续生化系统的负荷。
附图说明
下面结合附图和具体实施方式对本发明作进一步详细的说明。
图1为本发明高COD含酚类污水的处理系统的结构示意图。
具体实施方式
下面的实施例可以使本专业的技术人员更全面地理解本发明，但并不因此将本发明限制在所述的实施例范围之中。
实施例
本实施例高COD含酚类污水的处理系统，包括预处理系统和后处理系统，预处理系统包括物化预处理系统和生化预处理系统，所述物化预处理系统和生化预处理系统串联或并联在工艺废水的出水端，进而依次或独立对工艺废水进行预处理；后处理系统与生化预处理系统串联并对预处理后的工艺废水进行后处理。
具体地，如图1所示，物化预处理系统为蒸汽吹脱处理系统，该预处理系统包括依次串接的用于对工艺废水进行水质和水量调节的 物化调节池A1、用于处理产品工艺废水中酚类的吹脱反应器2、用于将气相酚类转换成液相酚类的降膜吸收器3以及用于收集液体酚类的收集器4，且物化调节池A1的输入端与工艺废水的出水端相连；生化预处理系统为催化氧化预处理系统，该预处理系统包括依次串联的用于隔离工艺废水中油性物质的隔油池5、用于对工艺废水进行水质和水量调节的物化调节池B6、用于降解高COD及降低酚含量的催化氧化反应釜7、用于固液分离的斜板沉淀池8以及用于对斜板沉淀池底部污泥进行浓缩的污泥浓缩池9；隔油池5的输入端与工艺废水的出水端相连，催化氧化反应釜7的输入端与吹脱反应器2的污水的出水端相连。
后处理系统包括依次串联的用于对斜板沉淀池的上清液或生化污泥浓缩池的上清液进行水质和水量调节的生化调节池10、用于将生化调节池10调节后的水和接触氧化池12的回水进行混合的配水池11、用于微生物分解的接触氧化池12、用于缓存微生物分解后废水的中间池13、用于将微生物分解后的水和二沉池15的回水进行再次微生物分解的好氧池14、用于分离出活性污泥的二沉池15、用于对活性污泥进行浓缩的生化污泥浓缩池16以及用于对污泥压滤的压滤机17，且压滤机17的出水端还与中间池13的输入端相连。
采用本实施例高COD含酚类污水的处理系统进行处理的具体步骤，如下：
步骤1：物化预处理：在蒸汽吹脱预处理系统中，含酚类工艺废水首先通过物化调节池A1去除污水中上浮的悬浮物，并污水送至温度≤95℃的吹脱反应器2中进行吹脱处理3～5h，吹脱后酚类以气相形式从吹脱反应器2顶部进入降膜吸收器3中，降膜吸收器3通过温度为25～30℃的循环水冷却将气相的酚类转换成液相酚类，最后将液态酚类通入气体收集器4中进行收集，回收的酚类溶液可以根据具体情况做生产原料或锅炉燃料；
步骤2：生化预处理：将步骤1中经吹脱反应器2处理后的污水从吹脱反应器2底部送至催化氧化反应釜7中，向催化氧化反应釜7中加入双氧水、七水硫酸亚铁、小分子催化剂，反应温度为50～65℃，反应时间≥15分钟时，酚类去除率达99％；然后从催化氧化反应釜7 底送至斜板沉淀池8中，通过添加液碱、PAM，实现固液分离，底部污泥经泵送至所述污泥浓缩池9中，经叠螺式压滤机压滤后排出污泥，此时斜板沉淀池8中的上清液的PH值、COD及酚含量皆符合后续生化处理要求；
步骤3：后处理：步骤2中斜板沉淀池8内的上清液送至生化调节池10，生化调节池10可对污水的水量和水质进行调节，生化调节池10污水通过预曝气搅拌后送至配水池11，所述配水池11将所述生化调节池10的水和所述接触氧化池12的回水进行混合，污水浓度下降，经接触氧化池12中微生物分解后，流至二沉池15，该二沉池15分离出接触氧化池12出水中的活性污泥，二沉池15中的回流水回流到好氧池14中，二沉池15中的剩余污泥则经所述生化污泥浓缩池16经带式压滤机17压滤后排出污泥；此时二沉池15中上部的污水达到国家三级污水排放标准。
具体地，所述步骤2中，催化氧化反应釜中双氧水与污水体积的比值设定为1：100，双氧水与七水硫酸亚铁的摩尔比为1:3。
具体地，所述步骤2中，斜板沉淀池排出的污水PH值5-8，COD≤3000mg/L，醛类含量≤30mg/L。
具体地，所述步骤3中，二沉池排出的污水PH值6-9，COD≤500mg/L，醛类含量≤5mg/L，达到国家三级污水排放标准。
上述处理系统处理含高COD含酚类污水的方法，以含酚污水量为30m 3/d，其中COD值为168200mg/L，酚类含量约为226mg/L，PH值约为6.4为例，该方法具体步骤如下：
第一步，物化预处理：在蒸汽吹脱预处理系统中，含酚类工艺废水首先通过物化调节池A1去除污水中上浮的悬浮物，并污水送至吹脱反应器2中进行吹脱处理，吹脱处理压强0.6MPa，温度95℃、吹脱时间4h，吹脱后酚类以气相形式从吹脱反应器2顶部进入降膜吸收器3中，降膜吸收器3通过循环水冷却将气相的酚类转换成液相酚类，该循环水温度25-30℃；最后将液态酚类通入气体收集器4中进行收集，回收的酚类溶液可以根据具体情况做生产原料或锅炉燃料；经蒸汽吹脱装置处理后，污水中酚类含量降至(10-20)mg/L；
第二步，生化预处理：将第一步中经吹脱反应器2处理后的 污水从吹脱反应器2底部送至催化氧化反应釜7中，向加催化氧化反应釜7中加入双氧水、七水硫酸亚铁、小分子催化剂；其中双氧水与污水体积的比值设定为1：100，双氧水与七水硫酸亚铁的摩尔比为1:3，催化剂的量为进水质量的万分之二反应温度为65℃，反应时间≥30分钟时，酚类去除率达99％，然后从催化氧化反应釜底送至混合池中，通过添加液碱、PAM，去除沉渣池中过量的双氧水，底部污泥经泵送至污泥浓缩池中，经叠螺式滤机压滤后排出污泥，此时沉渣池中的上清液的PH值6.8、COD＝2200mg/L及酚含量22mg/L皆符合后续生化处理要求；
第三步，后处理：将第二步中斜板沉淀池8内的上清液送至生化调节池10，生化调节池10可对污水的水量和水质进行调节，生化调节池10污水通过预曝气搅拌后送至配水池11，配水池11将生化调节池10的水和接触氧化池12的回水进行混合，污水浓度下降至800mg/L以下，经接触氧化池12中微生物分解后，流至二沉池15，该二沉池15分离出接触氧化池12出水中的活性污泥，二沉池15中的回流水回流到好氧化池14中，二沉池15中的剩余污泥则经生化污泥浓缩池16经带式压滤机17压滤后排出污泥；此时二沉池二沉池中上部的污水PH值7.6，COD 380mg/L，酚类含量3.8mg/L，达到国家三级污水排放标准。
以上显示和描述了本发明的基本原理和主要特征以及本发明的优点。本行业的技术人员应该了解，本发明不受上述实施例的限制，上述实施例和说明书中描述的只是说明本发明的原理，在不脱离本发明精神和范围的前提下，本发明还会有各种变化和改进，这些变化和改进都落入要求保护的本发明范围内。本发明要求保护范围由所附的权利要求书及其等效物界定。

Claims (5)

  1. 一种高COD含酚类污水的处理系统，其特征在于：包括预处理系统和后处理系统，
    所述预处理系统包括物化预处理系统和生化预处理系统，所述物化预处理系统和生化预处理系统串联或并联在工艺废水的出水端，进而依次或独立对工艺废水进行预处理；
    所述后处理系统与生化预处理系统串联并对预处理后的工艺废水进行后处理；
    其中，所述物化预处理系统为蒸汽吹脱处理系统，该预处理系统包括依次串接的用于对工艺废水进行水质和水量调节的物化调节池A、用于处理产品工艺废水中酚类的吹脱反应器、用于将气相酚类转换成液相酚类的降膜吸收器以及用于收集液体酚类的收集器，且所述物化调节池A的输入端与工艺废水的出水端相连；
    所述生化预处理系统为催化氧化预处理系统，该预处理系统包括依次串联的用于隔离工艺废水中油性物质的隔油池、用于对工艺废水进行水质和水量调节的物化调节池B、用于降解高COD及降低酚含量的催化氧化反应釜、用于固液分离的斜板沉淀池以及用于对斜板沉淀池底部污泥进行浓缩的污泥浓缩池；所述隔油池的输入端与工艺废水的出水端相连，所述催化氧化反应釜的输入端与吹脱反应器的污水的出水端相连；
    所述后处理系统包括依次串联的用于对斜板沉淀池的上清液或生化污泥浓缩池的上清液进行水质和水量调节的生化调节池、用于将生化调节池调节后的水和接触氧化池的回水进行混合的配水池、用于微生物分解的接触氧化池、用于缓存微生物分解后废水的中间池、用于将微生物分解后的水和二沉池的回水进行再次微生物分解的好氧池、用于分离出活性污泥的二沉池、用于对活性污泥进行浓缩的生化污泥浓缩池以及用于对污泥压滤的压滤机，且压滤机的出水端还与中间池的输入端相连。
  2. 一种采用权利要求1所述高COD含酚类污水的处理系统处理高COD含酚类污水的方法，其特征在于：所述处理方法包括如下步骤：
    步骤1：物化预处理：在蒸汽吹脱预处理系统中，含酚类工艺废水首先通过物化调节池A去除污水中上浮的悬浮物，并污水送至温度≤95℃的吹脱反应器中进行吹脱处理3～5h，吹脱后酚类以气相形式从吹脱反应器顶部进入降膜吸收器中，降膜吸收器通过温度为25～30℃的循环水冷却将气相的酚类转换成液相酚类，最后将液态酚类通入气体收集器中进行收集，回收的酚类溶液可以根据具体情况做生产原料或锅炉燃料；
    步骤2：生化预处理：将步骤1中经吹脱反应器处理后的污水从吹脱反应器底部送至催化氧化反应釜中，向催化氧化反应釜中加入双氧水、七水硫酸亚铁、小分子催化剂，反应温度为50～65℃，反应时间≥15分钟时，酚类去除率达99％；然后从催化氧化反应釜底送至斜板沉淀池中，通过添加液碱、PAM，实现固液分离，底部污泥经泵送至所述污泥浓缩池中，经叠螺式压滤机压滤后排出污泥，此时斜板沉淀池中的上清液的PH值、COD及酚含量皆符合后续生化处理要求；
    步骤3：后处理：步骤2中斜板沉淀池内的上清液送至生化调节池，生化调节池可对污水的水量和水质进行调节，生化调节池污水通过预曝气搅拌后送至配水池，所述配水池将所述调节池的水和所述接触氧化池的回水进行混合，污水浓度下降，经接触氧化池中微生物分解后，流至二沉池，该二沉池分离出接触氧化池出水中的活性污泥，二沉池中的回流水回流到好氧池中，二沉池中的剩余污泥则经所述生化污泥浓缩池经带式压滤机压滤后排出污泥；此时二沉池中上部的污水达到国家三级污水排放标准。
  3. 根据权利要求2所述的采用高COD含酚类污水的处理系统处理高COD含酚类污水的方法，其特征在于：所述步骤2中，催化氧化反应釜中双氧水与污水体积的比值设定为1：100，双氧水与七水硫酸亚铁的摩尔比为1:3。
  4. 根据权利要求2所述的采用高COD含酚类污水的处理系统处理高COD含酚类污水的方法，其特征在于：所述步骤2中，斜板沉淀池排出的污水PH值5-8，COD≤3000mg/L，醛类含量≤30mg/L。
  5. 根据权利要求2所述的采用高COD含酚类污水的处理系统处理高COD含酚类污水的方法，其特征在于：所述步骤3中，二沉池排出的污水PH值6-9，COD≤500mg/L，醛类含量≤5mg/L，达到国家三级污水排放标准。
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