WO2022143243A1 - Coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon - Google Patents

Coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon Download PDF

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WO2022143243A1
WO2022143243A1 PCT/CN2021/139512 CN2021139512W WO2022143243A1 WO 2022143243 A1 WO2022143243 A1 WO 2022143243A1 CN 2021139512 W CN2021139512 W CN 2021139512W WO 2022143243 A1 WO2022143243 A1 WO 2022143243A1
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activated carbon
tank
fluidized bed
sedimentation tank
sludge
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French (fr)
Chinese (zh)
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杨飞
杜连喜
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中冶焦耐(大连)工程技术有限公司
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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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • 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
    • C02F1/5281—Installations for water purification using chemical agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/14—NH3-N
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment

Definitions

  • the invention relates to the technical field of coking wastewater treatment, in particular to a coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon.
  • the effluent index of coking wastewater after biochemical treatment is difficult to meet the standard stably.
  • an advanced treatment system is also required.
  • the commonly used advanced treatment systems mainly include HOK biological fluidized bed, advanced oxidation system, activated carbon adsorption system, etc.
  • the advanced oxidation system generally adopts the Fenton (Fenton reagent) catalytic oxidation method and the ozone catalytic oxidation method.
  • the HOK biological fluidized bed has built-in biological fillers, and an aeration oxygen supply facility is installed at the bottom.
  • Biological carriers composite formula materials such as diatom powder and powdered activated carbon
  • the water quality index after precipitation treatment can meet the requirements of the industry or environmental protection department discharge standards, but the ability of the biological carrier in the device to absorb pollutants is limited by the effluent index requirements, and it needs to be discharged before it reaches the saturation level, which will inevitably cause waste and lead to The sludge production is relatively increased, which increases the operating cost invisibly.
  • the Fenton (Fenton reagent) catalytic oxidation method can oxidize organic matter, and is especially suitable for the oxidation treatment of organic wastewater that is difficult to biodegrade or that general chemical oxidation is difficult to achieve.
  • the pH of the wastewater is first adjusted to below 4 with concentrated sulfuric acid, and then a certain amount of ferrous sulfate and hydrogen peroxide are added to carry out Fenton oxidation reaction. Add polymer flocculant, and finally enter into coagulation and sedimentation for clarification and separation.
  • the treated water quality index can meet the discharge standards of the industry or the environmental protection department.
  • the disadvantages are that the operation labor intensity is increased, the sludge output is large, and the treatment cost is relatively high. At the same time, the TDS concentration of the effluent is increased. negative effect.
  • the ozone catalytic oxidation method is a mature coking wastewater treatment process and an effective wastewater treatment method.
  • Ozone can react with most of the inorganic and organic substances in the coking wastewater, but the reaction rate constant K and the reaction gradient are different. It is theoretically feasible to use only ozone to remove sewage pollutants, but it needs to be combined with a catalyst to achieve greater efficiency. In the actual project, the ratio of ozone consumption to COD removal is close to 3 times, resulting in a particularly large power consumption. Therefore, it is necessary to combine other processes to form a multi-level barrier combination technology, so that the ozone process can be economically applied to wastewater treatment projects. Considering Considering the comprehensive factors such as investment and operating costs, ozone oxidation is obviously not an inexpensive wastewater treatment process.
  • Activated carbon contains a large number of micropores, has a huge specific surface area and adsorption capacity, can effectively remove color, odor, and can remove most organic pollutants and some inorganic substances in secondary effluent.
  • the factors that affect the adsorption of activated carbon are: the production process characteristics of activated carbon; the characteristics and concentration of the adsorbate; the pH value of the wastewater; the suspended solid content and other characteristics;
  • Activated carbon adsorption is the most important and effective treatment technology in sewage treatment, and it has been widely used.
  • concentration of the absorbed substance (solute or pollutant) in the solution is in dynamic equilibrium with the concentration of the adsorbed substance on the activated carbon microporous surface, the adsorption reaches equilibrium or "saturation". At this time, it is necessary to replace the activated carbon or implement a backwash operation. program.
  • Powder activated carbon and granular activated carbon can effectively remove color, odor, most organic pollutants and some inorganic substances.
  • powdered activated carbon has a larger contact area, stronger adsorption capacity, and more significant use effect; granular activated carbon has a wider range of use, and can be recycled through regeneration or backwashing, resulting in a wider range of applications; and powdered activated carbon is often used. Once discharged as sludge, it cannot function again. Therefore, it is necessary to tap the powder activated carbon application process to maximize its effectiveness.
  • the invention provides a coking wastewater treatment system and process for realizing the gradient utilization of powder activated carbon, which can ensure that the treated coking wastewater meets the direct discharge of 14 water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standards" It can save construction investment, reduce operating costs and improve environmental benefits.
  • the present invention adopts the following technical solutions to realize:
  • a coking wastewater treatment system for realizing gradient utilization of powdered activated carbon comprising a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a final activated carbon treatment unit and a coagulation and sedimentation unit;
  • the pre-aeration unit includes a pre-aeration tank and a primary sedimentation tank;
  • the biochemical treatment unit includes a first-stage A/O pool, a second-stage anoxic pool, a second-stage aerobic pool, and a second-stage sedimentation tank;
  • the activated carbon treatment unit includes a powdered activated carbon fluidized bed, a fluidized bed sedimentation tank and Powder activated carbon dosing device;
  • the coagulation and sedimentation unit includes a coagulation sedimentation tank;
  • the pretreatment unit is sequentially connected to a pre-aeration tank, a primary sedimentation tank, a first-stage A/O tank, a second-stage anoxic tank, and a second-stage aerobic tank Pool, secondary sedimentation tank,
  • a coking wastewater treatment system for realizing gradient utilization of powdered activated carbon further comprising a sludge concentration tank and a sludge treatment unit; the sludge outlet at the bottom of the initial precipitation and the sludge outlet at the bottom of the coagulation sedimentation tank are respectively connected to the sludge concentration tank , the sludge thickening tank is additionally connected to the sludge treatment unit.
  • the powder activated carbon dosing device is composed of a vacuum feeding device, a material preparation and storage system, a slurry preparation system and a slurry conveying system.
  • the pretreatment unit includes at least a gravity degreasing device and an air flotation degreasing device.
  • the powder activated carbon fluidized bed is provided with a mechanical stirring device or an air stirring device.
  • a coking wastewater treatment process for realizing gradient utilization of powdered activated carbon comprising the following steps:
  • the coking wastewater flows through the first-stage A/O pool, the second-stage anoxic pool and the second-stage aerobic pool in turn to carry out nitrification, denitrification, denitrification, and decarbonization reactions, and biodegrade other pollutants, and then enter the secondary sedimentation.
  • Pool Part of the powdered activated carbon and sludge separated from the secondary sedimentation tank is returned to the water inlet of the second-stage aerobic tank, and the other part is used as a secondary gradient to use powdered activated carbon to return to the water inlet of the pre-aeration tank.
  • the secondary sedimentation tank The effluent enters the powder activated carbon fluidized bed by self-flow;
  • a coking wastewater treatment process for realizing gradient utilization of powdered activated carbon wherein the raw water quality, process water quality and effluent water quality of the coking wastewater meet the following conditions:
  • the raw water quality of coking wastewater meets: petroleum ⁇ 50mg/L; CODcr ⁇ 6000mg/L; released cyanide ⁇ 20mg/L; volatile phenol ⁇ 800mg/L; ammonia nitrogen ⁇ 200mg/L; total nitrogen ⁇ 400mg/L:
  • the raw water temperature is 25 ⁇ 35°C;
  • the water quality of coking wastewater entering the pre-aeration unit shall meet the following requirements: petroleum ⁇ 20mg/L; CODcr ⁇ 5000mg/L; released cyanide ⁇ 20mg/L; volatile phenol ⁇ 800mg /L; Ammonia nitrogen ⁇ 200mg/L;
  • the quality of the coking wastewater entering the biochemical treatment unit satisfies: CODcr ⁇ 2300mg/L; volatile phenols ⁇ 280mg/L; easily released cyanide ⁇ 8mg/L; 6.5 ⁇ 7.5;
  • the water quality of coking wastewater treated by A/O tank satisfies: CODcr ⁇ 300mg/L; Volatile phenol ⁇ 0.5mg/L; easily released cyanide ⁇ 0.5mg/L; oil ⁇ 5mg/L; ammonia nitrogen ⁇ 5mg/L L; total nitrogen ⁇ 50mg/L; pH value 6.5 ⁇ 8.5;
  • the water quality of coking wastewater treated by the second-stage A anoxic tank and the second-stage aerobic tank meets: CODcr ⁇ 200mg/L; Volatile phenol ⁇ 0.3mg/L; Easy-to-release cyanide ⁇ 0.3mg/L; mg/L; ammonia nitrogen ⁇ 1mg/L; total nitrogen ⁇ 20mg/L; pH value 6.5 ⁇ 8.5;
  • the effluent quality of powder activated carbon fluidized bed meets: CODcr ⁇ 100mg/L; volatile phenol ⁇ 0.2mg/L; easy-to-release cyanide ⁇ 0.2mg/L;
  • the effluent index of the coagulation and sedimentation tank meets the requirements of 14 direct discharge limit indexes of water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standard"; the specific indexes are: pH value 7 ⁇ 8; SS ⁇ 50mg /L; CODcr ⁇ 80mg/L; ammonia nitrogen ⁇ 1mg/L; BOD 5 ⁇ 20mg/L; total nitrogen ⁇ 20mg/L; total phosphorus ⁇ 1.0mg/L; petroleum ⁇ 1mg/L; volatile phenol ⁇ 0.1mg/ L; Sulfide ⁇ 0.5mg/L; Benzene ⁇ 0.1mg/L; Cyanide ⁇ 0.2mg/L; Polycyclic Aromatic Hydrocarbons ⁇ 0.05mg/L; Benzo(a)pyrene ⁇ 0.03 ⁇ g/L.
  • the powder activated carbon is wood or coal quality powder activated carbon with irregular shapes, the particle size specification is 180-125 ⁇ m, the iodine adsorption value is greater than 950 mg/g, the methylene blue adsorption value is greater than 180 mg/g, the moisture content is less than or equal to 5%, and the strength is greater than or equal to 90%. .
  • the dosage of powder activated carbon in the powder activated carbon fluidized bed is not less than 400mg/L, and the sludge concentration is not less than 3000mg/L; the sludge concentration in the second-stage aerobic tank is not less than 2000mg/L; the The sludge concentration in the pre-aeration tank is not less than 4000mg/L; the COD value of the water body in the powder activated carbon fluidized bed carrying the initial powder activated carbon is not more than 200mg/L; the COD value of the water body in the second-stage aerobic tank receiving the primary gradient utilization of powder activated carbon is not more than 200mg/L 300mg/L; COD value of water in the pre-aeration tank receiving secondary gradient utilization of powdered activated carbon is not more than 5000mg/L.
  • the second-stage anoxic tank adopts the biofilm method to remove total nitrogen.
  • the present invention can reduce the construction investment by more than 1 million yuan; compared with the granular activated carbon adsorption (excluding the regeneration system) process, the construction investment can be reduced by 150 yuan Compared with the ozone catalytic oxidation process, the construction investment can be reduced by more than 2 million yuan, and the construction investment of the present invention is basically close to that of the Fenton catalytic oxidation process;
  • the invention can save more than 2.5 million yuan of pharmaceutical costs per year; compared with the granular activated carbon adsorption (excluding regeneration system) process, it can save pharmaceuticals every year
  • the cost is more than 1.3 million yuan; compared with the ozone catalytic oxidation process, it can save more than 620,000 yuan in the cost of chemicals per year; compared with the Fenton catalytic oxidation process, it can save more than 450,000 yuan in the cost of chemicals per year;
  • the present invention can reduce the amount of dry sludge treated by more than 368 tons per year; compared with the granular activated carbon adsorption (excluding regeneration system) process, the present invention The amount of dry sludge treated can be reduced by more than 45 tons per year; compared with the Fenton catalytic oxidation process, the present invention can reduce the amount of dry sludge treated by more than 740 tons per year;
  • the primary gradient utilization of powdered activated carbon is sent to the second-stage aerobic tank, realizing the dual effects of biological activated carbon and adsorption, which can improve the pollutant removal rate of the second-stage aerobic tank, reduce the fluidized bed load of powdered activated carbon, and reduce the consumption of powdered activated carbon quantity;
  • the secondary gradient utilization of powdered activated carbon is sent to the pre-aeration tank, which can improve the pollutant removal rate of the pre-aeration tank, reduce the load of the powdered activated carbon fluidized bed, and thus reduce the consumption of powdered activated carbon;
  • the volume of the pre-aeration tank can be reduced, and the generation of foam in the pre-aeration tank can also be suppressed, thereby saving construction investment and operating costs.
  • Fig. 1 is a schematic diagram of a coking wastewater treatment system that realizes the gradient utilization of powdered activated carbon according to the present invention.
  • a coking wastewater treatment system for realizing the gradient utilization of powdered activated carbon includes a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a powder activated carbon treatment unit and a coagulation and sedimentation unit; the described
  • the pre-aeration unit includes a pre-aeration tank and a primary sedimentation tank;
  • the biochemical treatment unit includes a first-stage A/O pool, a second-stage anoxic pool, a second-stage aerobic pool and a second-stage sedimentation tank;
  • the activated carbon treatment unit includes powdered activated carbon Fluidized bed, fluidized bed sedimentation tank and powder activated carbon dosing device;
  • the coagulation sedimentation unit includes a coagulation sedimentation tank;
  • the pretreatment unit is sequentially connected to a pre-aeration tank, a primary sedimentation tank, a first-stage A/O tank, The second-stage anoxic tank, the second-stage aerobic tank, the second sedimentation tank, the powdered activated
  • a coking wastewater treatment system for realizing gradient utilization of powdered activated carbon further comprising a sludge concentration tank and a sludge treatment unit; the sludge outlet at the bottom of the initial precipitation and the sludge outlet at the bottom of the coagulation sedimentation tank are respectively connected to the sludge concentration tank , the sludge thickening tank is additionally connected to the sludge treatment unit.
  • the powder activated carbon dosing device is composed of a vacuum feeding device, a material preparation and storage system, a slurry preparation system and a slurry conveying system.
  • the pretreatment unit includes at least a gravity degreasing device and an air flotation degreasing device.
  • the powder activated carbon fluidized bed is provided with a mechanical stirring device or an air stirring device.
  • a coking wastewater treatment process for realizing gradient utilization of powdered activated carbon comprising the following steps:
  • the coking wastewater flows through the first-stage A/O pool, the second-stage anoxic pool and the second-stage aerobic pool in turn to carry out nitrification, denitrification, denitrification, and decarbonization reactions, and biodegrade other pollutants, and then enter the secondary sedimentation.
  • Pool Part of the powdered activated carbon and sludge separated from the secondary sedimentation tank is returned to the water inlet of the second-stage aerobic tank, and the other part is used as a secondary gradient to use powdered activated carbon to return to the water inlet of the pre-aeration tank.
  • the secondary sedimentation tank The effluent enters the powder activated carbon fluidized bed by self-flow;
  • a coking wastewater treatment process for realizing gradient utilization of powdered activated carbon wherein the raw water quality, process water quality and effluent water quality of the coking wastewater meet the following conditions:
  • the raw water quality of coking wastewater meets: petroleum ⁇ 50mg/L; CODcr ⁇ 6000mg/L; released cyanide ⁇ 20mg/L; volatile phenol ⁇ 800mg/L; ammonia nitrogen ⁇ 200mg/L; total nitrogen ⁇ 400mg/L:
  • the raw water temperature is 25 ⁇ 35°C;
  • the water quality of coking wastewater entering the pre-aeration unit shall meet the following requirements: petroleum ⁇ 20mg/L; CODcr ⁇ 5000mg/L; released cyanide ⁇ 20mg/L; volatile phenol ⁇ 800mg /L; Ammonia nitrogen ⁇ 200mg/L;
  • the quality of the coking wastewater entering the biochemical treatment unit satisfies: CODcr ⁇ 2300mg/L; volatile phenols ⁇ 280mg/L; easily released cyanide ⁇ 8mg/L; 6.5 ⁇ 7.5;
  • the water quality of coking wastewater treated by A/O tank satisfies: CODcr ⁇ 300mg/L; Volatile phenol ⁇ 0.5mg/L; easily released cyanide ⁇ 0.5mg/L; oil ⁇ 5mg/L; ammonia nitrogen ⁇ 5mg/L L; total nitrogen ⁇ 50mg/L; pH value 6.5 ⁇ 8.5;
  • the water quality of coking wastewater treated by the second-stage A anoxic tank and the second-stage aerobic tank meets: CODcr ⁇ 200mg/L; Volatile phenol ⁇ 0.3mg/L; Easy-to-release cyanide ⁇ 0.3mg/L; mg/L; ammonia nitrogen ⁇ 1mg/L; total nitrogen ⁇ 20mg/L; pH value 6.5 ⁇ 8.5;
  • the effluent quality of powder activated carbon fluidized bed meets: CODcr ⁇ 100mg/L; volatile phenol ⁇ 0.2mg/L; easy-to-release cyanide ⁇ 0.2mg/L;
  • the effluent index of the coagulation and sedimentation tank meets the requirements of 14 direct discharge limit indexes of water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standard"; the specific indexes are: pH value 7 ⁇ 8; SS ⁇ 50mg /L; CODcr ⁇ 80mg/L; Ammonia nitrogen ⁇ 1mg/L; BOD 5 ⁇ 20mg/L; Total nitrogen ⁇ 20mg/L; L; Sulfide ⁇ 0.5mg/L; Benzene ⁇ 0.1mg/L; Cyanide ⁇ 0.2mg/L; Polycyclic Aromatic Hydrocarbons ⁇ 0.05mg/L; Benzo(a)pyrene ⁇ 0.03 ⁇ g/L.
  • the powder activated carbon is wood or coal quality powder activated carbon with irregular shapes, the particle size specification is 180-125 ⁇ m, the iodine adsorption value is greater than 950 mg/g, the methylene blue adsorption value is greater than 180 mg/g, the moisture content is less than or equal to 5%, and the strength is greater than or equal to 90%. .
  • the dosage of powder activated carbon in the powder activated carbon fluidized bed is not less than 400mg/L, and the sludge concentration is not less than 3000mg/L; the sludge concentration in the second-stage aerobic tank is not less than 2000mg/L; the The sludge concentration in the pre-aeration tank is not less than 4000mg/L; the COD value of the water body in the powder activated carbon fluidized bed carrying the initial powder activated carbon is not more than 200mg/L; the COD value of the water body in the second-stage aerobic tank receiving the primary gradient utilization of powder activated carbon is not more than 200mg/L 300mg/L; COD value of water in the pre-aeration tank receiving secondary gradient utilization of powdered activated carbon is not more than 5000mg/L.
  • the second-stage anoxic tank adopts the biofilm method to remove total nitrogen.
  • the advantages of the coking wastewater treatment process for realizing the gradient utilization of powdered activated carbon in the present invention are mainly reflected in the following aspects: 1) gradient utilization of powdered activated carbon reduces the dosage of activated carbon; 2) the supporting equipment is easy to operate and low in construction investment; 3) Reduce sludge production and reduce operating costs; 4) can achieve stable compliance; 5) improve the level of automated operation.
  • the secondary gradient using powdered activated carbon can play the same adsorption role in the pre-aeration tank and the second-stage aerobic tank. It is not difficult to understand that the present invention has the same characteristics as the powdered carbon activated sludge process (PACT).
  • the operating conditions and the dosing species of the pretreatment unit, the biochemical treatment unit and the coagulation sedimentation tank of the present invention are basically the same as the existing technological operation requirements.
  • the coking wastewater treatment system is designed according to the treatment scale of 100m 3 /h, and the coking wastewater treatment system is composed of a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a powder activated carbon treatment unit, a coagulation sedimentation unit and a sludge treatment unit.
  • the pretreatment unit adopts gravity degreasing + air flotation degreasing technology to control the main indicators of effluent oil ⁇ 20mg/L.
  • the pre-aeration unit is composed of a pre-aeration tank and a primary sedimentation tank.
  • the effluent of the primary sedimentation tank meets: CODcr ⁇ 2300mg/L; The value is between 6.5 and 7.5.
  • the biochemical treatment unit adopts two-stage A/O biological denitrification treatment technology, and the effluent quality of the first A/O tank meets: CODcr ⁇ 300mg/L, volatile phenols ⁇ 0.5mg/L, easily released cyanide ⁇ 0.5mg/L, oil ⁇ 5mg/L, ammonia nitrogen ⁇ 5mg/L, total nitrogen ⁇ 50mg/L, pH value between 6.5 and 8.5; the effluent quality of the second-stage A/O system meets: CODcr ⁇ 200mg/L, volatile phenol ⁇ 0.3mg/L, Easy to release cyanide ⁇ 0.3mg/L, oil ⁇ 2.5mg/L, ammonia nitrogen ⁇ 1mg/L, total nitrogen ⁇ 20mg/L, pH value to 6.5 ⁇ 8.5.
  • the carbon slurry is added into the powder activated carbon fluidized bed through the automatic powder activated carbon dosing device, and mechanical or air stirring is used. Phenol ⁇ 0.2mg/L, easily released cyanide ⁇ 0.2mg/L, chromaticity ⁇ 30 degrees.
  • the pH value of the effluent from the coagulation sedimentation tank is 7-8, SS ⁇ 50mg/L, CODcr ⁇ 80mg/L, and ammonia nitrogen ⁇ 1mg/ L, BOD5 ⁇ 20mg/L, total nitrogen ⁇ 20mg/L, total phosphorus ⁇ 1.0mg/L, petroleum ⁇ 1mg/L, volatile phenol ⁇ 0.1mg/L, sulfide ⁇ 0.5mg/L, benzene ⁇ 0.1mg /L, cyanide ⁇ 0.2mg/L, polycyclic aromatic hydrocarbons ⁇ 0.05mg/L, benzo(a)pyrene ⁇ 0.03 ⁇ g/L.
  • the construction investment can be saved by about 1.5 million yuan, accounting for about 5% of the total investment; the annual saving of the operating cost of chemicals is about 1.2175 million yuan; The amount of sludge is about 384 tons.

Abstract

The present invention relates to a coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon. The system comprises a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a powdered activated carbon treatment unit, and a coagulating sedimentation unit; the pre-aeration unit comprises a pre-aeration tank and a primary sedimentation tank; the biochemical treatment unit comprises a first-section A/O tank, a second-section anoxic tank, a second-section aerobic tank, and a secondary sedimentation tank; the powdered activated carbon treatment unit comprises a powdered activated carbon fluidized bed, a fluidized bed sedimentation tank, and a powdered activated carbon feeding means; and the coagulating sedimentation unit comprises a coagulating sedimentation tank. The present invention can ensure that the treated coking wastewater can achieve 14 water pollutant direct emission limit indicators required by Table 2 of GB16171-2012 Emission Standard of Pollutants for Coking Chemical Industry, such that the construction investment can be saved, the operation cost can be reduced, and the environmental benefit can be improved.

Description

一种实现粉末活性炭梯度利用的焦化废水处理系统及工艺A coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon 技术领域technical field
本发明涉及焦化废水处理技术领域，尤其涉及一种实现粉末活性炭梯度利用的焦化废水处理系统及工艺。The invention relates to the technical field of coking wastewater treatment, in particular to a coking wastewater treatment system and process for realizing gradient utilization of powdered activated carbon.
背景技术Background technique
生化处理后的焦化废水出水指标很难稳定达标，除增加混凝处理单元外，还需要配套深度处理系统，常用的深度处理系统主要有HOK生物流化床、高级氧化系统、活性炭吸附系统等，其中高级氧化系统一般采用芬顿(Fenton试剂)催化氧化法和臭氧催化氧化法，这几种方法各有如下缺点：The effluent index of coking wastewater after biochemical treatment is difficult to meet the standard stably. In addition to adding a coagulation treatment unit, an advanced treatment system is also required. The commonly used advanced treatment systems mainly include HOK biological fluidized bed, advanced oxidation system, activated carbon adsorption system, etc. Among them, the advanced oxidation system generally adopts the Fenton (Fenton reagent) catalytic oxidation method and the ozone catalytic oxidation method. Each of these methods has the following disadvantages:
(1)HOK生物流化床内置生物填料，底部设曝气供氧设施，装置内投加生物载体(硅藻精粉和粉末活性炭等复合配方材料)，HOK生物流化床出水再经混凝沉淀处理后的水质指标可以满足行业或环保部门排放标准的要求，但其装置内生物载体吸附污染物的能力受出水指标要求限制，还远没有达到饱和的程度就需要排放，势必造成浪费，导致污泥产量相对提高，无形中增加了运行成本。(1) The HOK biological fluidized bed has built-in biological fillers, and an aeration oxygen supply facility is installed at the bottom. Biological carriers (composite formula materials such as diatom powder and powdered activated carbon) are added to the device, and the effluent from the HOK biological fluidized bed is coagulated. The water quality index after precipitation treatment can meet the requirements of the industry or environmental protection department discharge standards, but the ability of the biological carrier in the device to absorb pollutants is limited by the effluent index requirements, and it needs to be discharged before it reaches the saturation level, which will inevitably cause waste and lead to The sludge production is relatively increased, which increases the operating cost invisibly.
(2)芬顿(Fenton试剂)催化氧化法，能够氧化有机物，特别适用于生物难降解或一般化学氧化难以奏效的有机废水的氧化处理。该技术首先用浓硫酸将废水pH调至4以下，然后加入一定量的硫酸亚铁和双氧水，进行Fenton氧化反应，反应一段时间后用石灰乳溶液将废水的pH值调到7以上，然后再投加高分子絮凝剂，最后进入混凝沉淀进行澄清分离。其处理后的水质指标可以满足行业或环保部门排放标准的要求，缺点是操作劳动强度 加大、污泥产量多、处理成本相对高，同时增加出水的TDS浓度,对后续的膜处理脱盐造成非常不利的影响。(2) The Fenton (Fenton reagent) catalytic oxidation method can oxidize organic matter, and is especially suitable for the oxidation treatment of organic wastewater that is difficult to biodegrade or that general chemical oxidation is difficult to achieve. In this technology, the pH of the wastewater is first adjusted to below 4 with concentrated sulfuric acid, and then a certain amount of ferrous sulfate and hydrogen peroxide are added to carry out Fenton oxidation reaction. Add polymer flocculant, and finally enter into coagulation and sedimentation for clarification and separation. The treated water quality index can meet the discharge standards of the industry or the environmental protection department. The disadvantages are that the operation labor intensity is increased, the sludge output is large, and the treatment cost is relatively high. At the same time, the TDS concentration of the effluent is increased. negative effect.
(3)臭氧催化氧化法，是成熟的焦化废水处理工艺，也是一种有效的废水处理手段，臭氧可与焦化废水中大部分无机物和有机物反应，只是反应速度常数K和反应梯度不同，若仅用臭氧去除污水污染物，理论上是可行性的，但需要配合催化剂才能发挥更大效率。实际工程中，臭氧耗量与COD去除量比例接近3倍，导致耗电量特别大，因此，必须结合其它工艺构成多级屏障组合技术，才能使臭氧工艺比较经济的应用于废水处理工程，考虑到投资和运行成本等综合因素，臭氧氧化法显然不是一种低廉的废水处理工艺。(3) The ozone catalytic oxidation method is a mature coking wastewater treatment process and an effective wastewater treatment method. Ozone can react with most of the inorganic and organic substances in the coking wastewater, but the reaction rate constant K and the reaction gradient are different. It is theoretically feasible to use only ozone to remove sewage pollutants, but it needs to be combined with a catalyst to achieve greater efficiency. In the actual project, the ratio of ozone consumption to COD removal is close to 3 times, resulting in a particularly large power consumption. Therefore, it is necessary to combine other processes to form a multi-level barrier combination technology, so that the ozone process can be economically applied to wastewater treatment projects. Considering Considering the comprehensive factors such as investment and operating costs, ozone oxidation is obviously not an inexpensive wastewater treatment process.
活性炭含有大量微孔，具有巨大的比表面积和吸附能力，能有效地去除色度、臭味，可去除二级出水中大多数有机污染物和某些无机物。影响活性炭吸附的因素有：活性炭的生产工艺特性；被吸附物的特性和浓度；废水的PH值；悬浮固体含量等特性；接触系统时间及运行方式等。活性炭吸附是污水处理中最重要最有效的处理技术，目前已经得到了广泛的应用。当溶液中被吸收物质(溶质或污染物)的浓度与活性炭微孔表面被吸附物质的浓度处于动态平衡时，吸附就达到平衡或“饱和”，此时，就需要更换活性炭或实施反冲洗操作程序。Activated carbon contains a large number of micropores, has a huge specific surface area and adsorption capacity, can effectively remove color, odor, and can remove most organic pollutants and some inorganic substances in secondary effluent. The factors that affect the adsorption of activated carbon are: the production process characteristics of activated carbon; the characteristics and concentration of the adsorbate; the pH value of the wastewater; the suspended solid content and other characteristics; Activated carbon adsorption is the most important and effective treatment technology in sewage treatment, and it has been widely used. When the concentration of the absorbed substance (solute or pollutant) in the solution is in dynamic equilibrium with the concentration of the adsorbed substance on the activated carbon microporous surface, the adsorption reaches equilibrium or "saturation". At this time, it is necessary to replace the activated carbon or implement a backwash operation. program.
粉末活性炭和颗粒活性炭，都能效地去除色度、臭味、大多数有机污染物和某些无机物。比较而言，粉末活性炭接触面积更大，吸附能力更强，使用效果更显著；颗粒活性炭使用范围较广，可以通过再生或反洗环节达到循环使用，导致其应用更加广泛；而粉末活性炭往往使用一次就作为污泥而排放，无法再次发挥作用。因此，有必要挖掘粉末活性炭应用工艺，使其发挥 最大效力。Powder activated carbon and granular activated carbon can effectively remove color, odor, most organic pollutants and some inorganic substances. In comparison, powdered activated carbon has a larger contact area, stronger adsorption capacity, and more significant use effect; granular activated carbon has a wider range of use, and can be recycled through regeneration or backwashing, resulting in a wider range of applications; and powdered activated carbon is often used. Once discharged as sludge, it cannot function again. Therefore, it is necessary to tap the powder activated carbon application process to maximize its effectiveness.
发明内容SUMMARY OF THE INVENTION
本发明提供了一种实现粉末活性炭梯度利用的焦化废水处理系统及工艺，能够确保处理后的焦化废水达到GB16171-2012《炼焦化学工业污染物排放标准》表2要求的14项水污染物直接排放极限指标，并且能够节省建设投资、降低运行成本、提高环境效益。The invention provides a coking wastewater treatment system and process for realizing the gradient utilization of powder activated carbon, which can ensure that the treated coking wastewater meets the direct discharge of 14 water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standards" It can save construction investment, reduce operating costs and improve environmental benefits.
为了达到上述目的，本发明采用以下技术方案实现：In order to achieve the above object, the present invention adopts the following technical solutions to realize:
一种实现粉末活性炭梯度利用的焦化废水处理系统，包括预处理单元、预曝气单元、生化处理单元、料末活性炭处理单元及混凝沉淀单元；所述预曝气单元包括预曝气池及初沉池；所述生化处理单元包括一段A/O池、二段缺氧池、二段好氧池及二沉池；所述活性炭处理单元包括粉末活性炭流化床、流化床沉淀池及粉末活性炭投加装置；所述混凝沉淀单元包括混凝沉淀池；所述预处理单元依次连接预曝气池、初沉池、一段A/O池、二段缺氧池、二段好氧池、二沉池、粉末活性炭流化床、流化床沉淀池及混凝沉淀池；所述粉末活性炭流化床另外连接粉末活性炭投加装置；所述混凝沉淀池另外连接复合混凝剂及助凝剂投加装置；所述初沉池通过回流污泥管道一连接预曝气池；所述二沉池通过回流污泥管道二连接二段好氧池的进水端及预曝气池的进水端；所述流化床沉淀池通过活性炭管道连接粉末活性炭流化床及二段好氧池。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon, comprising a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a final activated carbon treatment unit and a coagulation and sedimentation unit; the pre-aeration unit includes a pre-aeration tank and a primary sedimentation tank; the biochemical treatment unit includes a first-stage A/O pool, a second-stage anoxic pool, a second-stage aerobic pool, and a second-stage sedimentation tank; the activated carbon treatment unit includes a powdered activated carbon fluidized bed, a fluidized bed sedimentation tank and Powder activated carbon dosing device; the coagulation and sedimentation unit includes a coagulation sedimentation tank; the pretreatment unit is sequentially connected to a pre-aeration tank, a primary sedimentation tank, a first-stage A/O tank, a second-stage anoxic tank, and a second-stage aerobic tank Pool, secondary sedimentation tank, powder activated carbon fluidized bed, fluidized bed sedimentation tank and coagulation sedimentation tank; the powder activated carbon fluidized bed is additionally connected to a powder activated carbon dosing device; the coagulation sedimentation tank is additionally connected to a composite coagulant and a coagulant dosing device; the primary sedimentation tank is connected to the pre-aeration tank through the return sludge pipeline 1; the secondary sedimentation tank is connected to the water inlet end of the second-stage aerobic tank and the pre-aeration tank through the return sludge pipeline 2 The inlet end of the tank; the fluidized bed sedimentation tank is connected to the powder activated carbon fluidized bed and the second-stage aerobic tank through an activated carbon pipeline.
一种实现粉末活性炭梯度利用的焦化废水处理系统，还包括污泥浓缩池及污泥处理单元；所述初沉淀底部的污泥出口及混凝沉淀池底部的污泥出口分别连接污泥浓缩池，污泥浓缩池另外连接污泥处理单元。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon, further comprising a sludge concentration tank and a sludge treatment unit; the sludge outlet at the bottom of the initial precipitation and the sludge outlet at the bottom of the coagulation sedimentation tank are respectively connected to the sludge concentration tank , the sludge thickening tank is additionally connected to the sludge treatment unit.
所述粉末活性炭投加装置由真空上料装置、备料和储料系统、浆料准备系统及浆料输送系统组成。The powder activated carbon dosing device is composed of a vacuum feeding device, a material preparation and storage system, a slurry preparation system and a slurry conveying system.
所述预处理单元至少包括重力除油装置及气浮除油装置。The pretreatment unit includes at least a gravity degreasing device and an air flotation degreasing device.
所述粉末活性炭流化床内设机械搅拌装置或空气搅拌装置。The powder activated carbon fluidized bed is provided with a mechanical stirring device or an air stirring device.
一种实现粉末活性炭梯度利用的焦化废水处理工艺，包括如下步骤：A coking wastewater treatment process for realizing gradient utilization of powdered activated carbon, comprising the following steps:
1)焦化废水先进入预处理单元，进行重力除油及气浮除油处理；1) The coking wastewater first enters the pretreatment unit for gravity degreasing and air flotation degreasing;
2)预处理单元出水靠自流依次进入预曝气池及初沉池，在此过程中，实现生物絮凝吸附，同时发生不完全氧化反应；初沉池出水自流进入一段A/O池；2) The effluent of the pretreatment unit enters the pre-aeration tank and the primary sedimentation tank in turn by self-flow. In this process, biological flocculation and adsorption are realized, and incomplete oxidation reaction occurs at the same time;
3)焦化废水依次流经一段A/O池、二段缺氧池及二段好氧池，进行硝化、反硝化脱氮、脱碳反应，并对其它污染物进行生物降解，然后进入二沉池；二沉池分离出的粉末活性炭及污泥，一部分回流到二段好氧池的进水端，另一部分作为二次梯度利用粉末活性炭回流到预曝气池的进水端，二沉池出水靠自流进入粉末活性炭流化床；3) The coking wastewater flows through the first-stage A/O pool, the second-stage anoxic pool and the second-stage aerobic pool in turn to carry out nitrification, denitrification, denitrification, and decarbonization reactions, and biodegrade other pollutants, and then enter the secondary sedimentation. Pool; Part of the powdered activated carbon and sludge separated from the secondary sedimentation tank is returned to the water inlet of the second-stage aerobic tank, and the other part is used as a secondary gradient to use powdered activated carbon to return to the water inlet of the pre-aeration tank. The secondary sedimentation tank The effluent enters the powder activated carbon fluidized bed by self-flow;
4)通过粉末活性炭投加装置向粉末活性炭流化床内投加设定量的炭浆，在粉末活性炭流化床内吸附一段时间后的炭浆混合液进入流化床沉淀池，经过沉淀澄清分离后，出水进入混凝沉淀池，混凝沉淀池内投加复合混凝剂及助凝剂；流化床沉淀池底部的炭浆污泥一部分回流到粉末活性炭流化床的进水端，以增加粉末活性炭流化床中粉末活性炭的浓度，另一部分作为一次梯度利用粉末活性炭回流到二段好氧池的进水端；4) Add a set amount of carbon slurry into the powder activated carbon fluidized bed through the powder activated carbon dosing device, and the carbon slurry mixture after being adsorbed in the powder activated carbon fluidized bed for a period of time enters the fluidized bed sedimentation tank, and is clarified by precipitation After separation, the effluent enters the coagulation sedimentation tank, and the composite coagulant and coagulant aid are added to the coagulation sedimentation tank; a part of the carbon slurry sludge at the bottom of the fluidized bed sedimentation tank is returned to the inlet end of the powder activated carbon fluidized bed, so that the Increase the concentration of powdered activated carbon in the fluidized bed of powdered activated carbon, and the other part is used as a primary gradient to use powdered activated carbon to return to the water inlet of the second-stage aerobic tank;
5)初沉池底部剩余污泥、混凝沉淀池底部化学污泥分别送往污泥浓缩池，经浓缩后的污泥送往污泥处理单元进一步处理。5) The residual sludge at the bottom of the primary sedimentation tank and the chemical sludge at the bottom of the coagulation sedimentation tank are respectively sent to the sludge thickening tank, and the concentrated sludge is sent to the sludge treatment unit for further treatment.
一种实现粉末活性炭梯度利用的焦化废水处理工艺，所述焦化废水的原水水质、过程水质及出水水质满足以下条件：A coking wastewater treatment process for realizing gradient utilization of powdered activated carbon, wherein the raw water quality, process water quality and effluent water quality of the coking wastewater meet the following conditions:
1)焦化废水的原水水质满足：石油类≤50mg/L；CODcr≤6000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；总氮≤400mg/L：原水温度为25～35℃；1) The raw water quality of coking wastewater meets: petroleum ≤50mg/L; CODcr ≤6000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg/L; ammonia nitrogen ≤200mg/L; total nitrogen ≤400mg/L: The raw water temperature is 25～35℃;
2)经重力除油及气浮除油处理后，进预曝气单元的焦化废水水质满足：石油类≤20mg/L；CODcr≤5000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；2) After gravity degreasing and air flotation degreasing, the water quality of coking wastewater entering the pre-aeration unit shall meet the following requirements: petroleum ≤20mg/L; CODcr ≤5000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg /L; Ammonia nitrogen≤200mg/L;
3)经预曝气池处理后，进生化处理单元的焦化废水水质满足：CODcr≤2300mg/L；挥发酚≤280mg/L；易释放氰化物≤8mg/L；油≤5mg/L，pH值6.5～7.5；3) After the pre-aeration tank treatment, the quality of the coking wastewater entering the biochemical treatment unit satisfies: CODcr≤2300mg/L; volatile phenols≤280mg/L; easily released cyanide≤8mg/L; 6.5～7.5;
4)经一段A/O池处理后的焦化废水水质满足：CODcr≤300mg/L；挥发酚≤0.5mg/L；易释放氰化物≤0.5mg/L；油≤5mg/L；氨氮≤5mg/L；总氮≤50mg/L；pH值6.5～8.5；4) The water quality of coking wastewater treated by A/O tank satisfies: CODcr≤300mg/L; Volatile phenol≤0.5mg/L; easily released cyanide≤0.5mg/L; oil≤5mg/L; ammonia nitrogen≤5mg/L L; total nitrogen≤50mg/L; pH value 6.5～8.5;
5)经二段A缺氧池和二段好氧池处理后的焦化废水水质满足：CODcr≤200mg/L；挥发酚≤0.3mg/L；易释放氰化物≤0.3mg/L；油≤2.5mg/L；氨氮≤1mg/L；总氮≤20mg/L；pH值6.5～8.5；5) The water quality of coking wastewater treated by the second-stage A anoxic tank and the second-stage aerobic tank meets: CODcr≤200mg/L; Volatile phenol≤0.3mg/L; Easy-to-release cyanide≤0.3mg/L; mg/L; ammonia nitrogen≤1mg/L; total nitrogen≤20mg/L; pH value 6.5～8.5;
6)粉末活性炭流化床出水水质满足：CODcr≤100mg/L；挥发酚≤0.2mg/L；易释放氰化物≤0.2mg/L；6) The effluent quality of powder activated carbon fluidized bed meets: CODcr≤100mg/L; volatile phenol≤0.2mg/L; easy-to-release cyanide≤0.2mg/L;
7)混凝沉淀池出水指标，满足GB16171-2012《炼焦化学工业污染物排放标准》表2要求的14项水污染物直接排放极限指标要求；具体指标为：pH值7～8；SS≤50mg/L；CODcr≤80mg/L；氨氮≤1mg/L；BOD 5≤20mg/L； 总氮≤20mg/L；总磷≤1.0mg/L；石油类≤1mg/L；挥发酚≤0.1mg/L；硫化物≤0.5mg/L；苯≤0.1mg/L；氰化物≤0.2mg/L；多环芳烃≤0.05mg/L；苯并(a)芘≤0.03μg/L。7) The effluent index of the coagulation and sedimentation tank meets the requirements of 14 direct discharge limit indexes of water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standard"; the specific indexes are: pH value 7～8; SS≤50mg /L; CODcr≤80mg/L; ammonia nitrogen≤1mg/L; BOD 5≤20mg/L; total nitrogen≤20mg/L; total phosphorus≤1.0mg/L; petroleum≤1mg/L; volatile phenol≤0.1mg/ L; Sulfide≤0.5mg/L; Benzene≤0.1mg/L; Cyanide≤0.2mg/L; Polycyclic Aromatic Hydrocarbons≤0.05mg/L; Benzo(a)pyrene≤0.03μg/L.
所述粉末活性炭为木质或煤质且具有不规则形状的粉末活性炭，粒度规格为180～125μm，碘吸附值大于950mg/g，亚甲基蓝吸附值大于180mg/g，水分≤5％，强度≥90％。The powder activated carbon is wood or coal quality powder activated carbon with irregular shapes, the particle size specification is 180-125 μm, the iodine adsorption value is greater than 950 mg/g, the methylene blue adsorption value is greater than 180 mg/g, the moisture content is less than or equal to 5%, and the strength is greater than or equal to 90%. .
所述粉末活性炭流化床内的粉末活性炭投加量不低于400mg/L，污泥浓度不低于3000mg/L；所述二段好氧池内污泥浓度不低于2000mg/L；所述预曝气池内污泥浓度不低于4000mg/L；承载初始粉末活性炭的粉末活性炭流化床内水体COD值不大于200mg/L；接受一次梯度利用粉末活性炭的二段好氧池内水体COD不大于300mg/L；接受二次梯度利用粉末活性炭的预曝气池内水体COD值不大于5000mg/L。The dosage of powder activated carbon in the powder activated carbon fluidized bed is not less than 400mg/L, and the sludge concentration is not less than 3000mg/L; the sludge concentration in the second-stage aerobic tank is not less than 2000mg/L; the The sludge concentration in the pre-aeration tank is not less than 4000mg/L; the COD value of the water body in the powder activated carbon fluidized bed carrying the initial powder activated carbon is not more than 200mg/L; the COD value of the water body in the second-stage aerobic tank receiving the primary gradient utilization of powder activated carbon is not more than 200mg/L 300mg/L; COD value of water in the pre-aeration tank receiving secondary gradient utilization of powdered activated carbon is not more than 5000mg/L.
所述二段缺氧池采用生物膜法脱总氮。The second-stage anoxic tank adopts the biofilm method to remove total nitrogen.
与现有技术相比，本发明的有益效果是：Compared with the prior art, the beneficial effects of the present invention are:
1)充分利用活性炭具有良好的吸附有机污染物和某些无机物的吸附特性，达到高效率去除废水中污染物目的，同时大大降低废水色度，确保处理后的焦化废水能够实现稳定达到《炼焦化学工业污染物排放标准》GB16171-2012表2要求的14项水污染物直接排放极限指标，既减少污染物的排放量，又能提高环境效益；1) Make full use of the good adsorption characteristics of activated carbon to adsorb organic pollutants and some inorganic substances, achieve the purpose of efficiently removing pollutants in wastewater, and at the same time greatly reduce the chromaticity of wastewater, to ensure that the treated coking wastewater can stably achieve "coking wastewater". The 14 direct discharge limit indicators of water pollutants required in Table 2 of the Chemical Industry Pollutant Discharge Standard GB16171-2012 can not only reduce the discharge of pollutants, but also improve environmental benefits;
2)按处理焦化废水量100m 3/h核算，与生物流化床工艺比较，本发明可以减少建设投资100万元以上；与颗粒活性炭吸附(不包括再生系统)工艺比较，可以减少建设投资150万元以上；与臭氧催化氧化工艺比较，可以 减少建设投资200万元以上，本发明与芬顿催化氧化工艺的建设投资基本接近； 2) Calculated according to the amount of coking wastewater treated at 100m 3 /h, compared with the biological fluidized bed process, the present invention can reduce the construction investment by more than 1 million yuan; compared with the granular activated carbon adsorption (excluding the regeneration system) process, the construction investment can be reduced by 150 yuan Compared with the ozone catalytic oxidation process, the construction investment can be reduced by more than 2 million yuan, and the construction investment of the present invention is basically close to that of the Fenton catalytic oxidation process;
3)按处理焦化废水量100m 3/h核算，与生物流化床工艺比较，本发明每年可以节省药剂成本250万元以上；与颗粒活性炭吸附(不包括再生系统)工艺比较，每年可以节省药剂成本130万元以上；与臭氧催化氧化工艺比较，每年可以节省药剂成本62万元以上；和芬顿催化氧化工艺比较，每年可以节省药剂成本45万元以上； 3) Calculated according to the amount of treated coking wastewater 100m 3 /h, compared with the biological fluidized bed process, the invention can save more than 2.5 million yuan of pharmaceutical costs per year; compared with the granular activated carbon adsorption (excluding regeneration system) process, it can save pharmaceuticals every year The cost is more than 1.3 million yuan; compared with the ozone catalytic oxidation process, it can save more than 620,000 yuan in the cost of chemicals per year; compared with the Fenton catalytic oxidation process, it can save more than 450,000 yuan in the cost of chemicals per year;
4)按处理焦化废水量100m 3/h核算，与生物流化床工艺比较，本发明每年可以减少干污泥处理量368吨以上；与颗粒活性炭吸附(不包括再生系统)工艺比较，本发明每年可以减少干污泥处理量45吨以上；和芬顿催化氧化工艺比较，本发明每年可以减少干污泥处理量740吨以上； 4) Calculated according to the amount of treated coking wastewater 100m 3 /h, compared with the biological fluidized bed process, the present invention can reduce the amount of dry sludge treated by more than 368 tons per year; compared with the granular activated carbon adsorption (excluding regeneration system) process, the present invention The amount of dry sludge treated can be reduced by more than 45 tons per year; compared with the Fenton catalytic oxidation process, the present invention can reduce the amount of dry sludge treated by more than 740 tons per year;
5)将一次梯度利用粉末活性炭送至二段好氧池，实现了生物活性炭及吸附双重效应，可以提高二段好氧池污染物去除率，降低粉末活性炭流化床负荷，从而减少粉末活性炭消耗量；5) The primary gradient utilization of powdered activated carbon is sent to the second-stage aerobic tank, realizing the dual effects of biological activated carbon and adsorption, which can improve the pollutant removal rate of the second-stage aerobic tank, reduce the fluidized bed load of powdered activated carbon, and reduce the consumption of powdered activated carbon quantity;
6)将二次梯度利用粉末活性炭送至预曝气池，可以提高预曝气池污染物去除率，降低粉末活性炭流化床负荷，从而减少粉末活性炭消耗量；6) The secondary gradient utilization of powdered activated carbon is sent to the pre-aeration tank, which can improve the pollutant removal rate of the pre-aeration tank, reduce the load of the powdered activated carbon fluidized bed, and thus reduce the consumption of powdered activated carbon;
7)投加一次梯度利用粉末活性炭后，二段好氧池的容积可以减小，从而节省建设投资；7) After adding one-time gradient utilization powder activated carbon, the volume of the second-stage aerobic tank can be reduced, thereby saving construction investment;
8)投加二次梯度利用粉末活性炭后，预曝气池容积可以减小，还可以抑制预曝气池泡沫发生量，从而节省建设投资及运行成本。8) After adding the secondary gradient utilization powder activated carbon, the volume of the pre-aeration tank can be reduced, and the generation of foam in the pre-aeration tank can also be suppressed, thereby saving construction investment and operating costs.
附图说明Description of drawings
图1是本发明一种实现粉末活性炭梯度利用的焦化废水处理系统的示意 图。Fig. 1 is a schematic diagram of a coking wastewater treatment system that realizes the gradient utilization of powdered activated carbon according to the present invention.
具体实施方式Detailed ways
下面结合附图对本发明的具体实施方式作进一步说明：The specific embodiments of the present invention will be further described below in conjunction with the accompanying drawings:
如图1所示，本发明所述一种实现粉末活性炭梯度利用的焦化废水处理系统，包括预处理单元、预曝气单元、生化处理单元、料末活性炭处理单元及混凝沉淀单元；所述预曝气单元包括预曝气池及初沉池；所述生化处理单元包括一段A/O池、二段缺氧池、二段好氧池及二沉池；所述活性炭处理单元包括粉末活性炭流化床、流化床沉淀池及粉末活性炭投加装置；所述混凝沉淀单元包括混凝沉淀池；所述预处理单元依次连接预曝气池、初沉池、一段A/O池、二段缺氧池、二段好氧池、二沉池、粉末活性炭流化床、流化床沉淀池及混凝沉淀池；所述粉末活性炭流化床另外连接粉末活性炭投加装置；所述混凝沉淀池另外连接复合混凝剂及助凝剂投加装置；所述初沉池通过回流污泥管道一连接预曝气池；所述二沉池通过回流污泥管道二连接二段好氧池的进水端及预曝气池的进水端；所述流化床沉淀池通过活性炭管道连接粉末活性炭流化床及二段好氧池。As shown in Figure 1, a coking wastewater treatment system for realizing the gradient utilization of powdered activated carbon according to the present invention includes a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a powder activated carbon treatment unit and a coagulation and sedimentation unit; the described The pre-aeration unit includes a pre-aeration tank and a primary sedimentation tank; the biochemical treatment unit includes a first-stage A/O pool, a second-stage anoxic pool, a second-stage aerobic pool and a second-stage sedimentation tank; the activated carbon treatment unit includes powdered activated carbon Fluidized bed, fluidized bed sedimentation tank and powder activated carbon dosing device; the coagulation sedimentation unit includes a coagulation sedimentation tank; the pretreatment unit is sequentially connected to a pre-aeration tank, a primary sedimentation tank, a first-stage A/O tank, The second-stage anoxic tank, the second-stage aerobic tank, the second sedimentation tank, the powdered activated carbon fluidized bed, the fluidized bed sedimentation tank and the coagulation sedimentation tank; the powdered activated carbon fluidized bed is additionally connected to a powdered activated carbon dosing device; The coagulation sedimentation tank is additionally connected to the compound coagulant and coagulant aid dosing device; the primary sedimentation tank is connected to the pre-aeration tank through the return sludge pipeline 1; the secondary sedimentation tank is connected to the second stage through the return sludge pipeline 2. The water inlet end of the oxygen tank and the water inlet end of the pre-aeration tank; the fluidized bed sedimentation tank is connected to the powder activated carbon fluidized bed and the second-stage aerobic tank through an activated carbon pipeline.
一种实现粉末活性炭梯度利用的焦化废水处理系统，还包括污泥浓缩池及污泥处理单元；所述初沉淀底部的污泥出口及混凝沉淀池底部的污泥出口分别连接污泥浓缩池，污泥浓缩池另外连接污泥处理单元。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon, further comprising a sludge concentration tank and a sludge treatment unit; the sludge outlet at the bottom of the initial precipitation and the sludge outlet at the bottom of the coagulation sedimentation tank are respectively connected to the sludge concentration tank , the sludge thickening tank is additionally connected to the sludge treatment unit.
所述粉末活性炭投加装置由真空上料装置、备料和储料系统、浆料准备系统及浆料输送系统组成。The powder activated carbon dosing device is composed of a vacuum feeding device, a material preparation and storage system, a slurry preparation system and a slurry conveying system.
所述预处理单元至少包括重力除油装置及气浮除油装置。The pretreatment unit includes at least a gravity degreasing device and an air flotation degreasing device.
所述粉末活性炭流化床内设机械搅拌装置或空气搅拌装置。The powder activated carbon fluidized bed is provided with a mechanical stirring device or an air stirring device.
一种实现粉末活性炭梯度利用的焦化废水处理工艺，包括如下步骤：A coking wastewater treatment process for realizing gradient utilization of powdered activated carbon, comprising the following steps:
1)焦化废水先进入预处理单元，进行重力除油及气浮除油处理；1) The coking wastewater first enters the pretreatment unit for gravity degreasing and air flotation degreasing;
2)预处理单元出水靠自流依次进入预曝气池及初沉池，在此过程中，实现生物絮凝吸附，同时发生不完全氧化反应；初沉池出水自流进入一段A/O池；2) The effluent of the pretreatment unit enters the pre-aeration tank and the primary sedimentation tank in turn by self-flow. In this process, biological flocculation and adsorption are realized, and incomplete oxidation reaction occurs at the same time;
3)焦化废水依次流经一段A/O池、二段缺氧池及二段好氧池，进行硝化、反硝化脱氮、脱碳反应，并对其它污染物进行生物降解，然后进入二沉池；二沉池分离出的粉末活性炭及污泥，一部分回流到二段好氧池的进水端，另一部分作为二次梯度利用粉末活性炭回流到预曝气池的进水端，二沉池出水靠自流进入粉末活性炭流化床；3) The coking wastewater flows through the first-stage A/O pool, the second-stage anoxic pool and the second-stage aerobic pool in turn to carry out nitrification, denitrification, denitrification, and decarbonization reactions, and biodegrade other pollutants, and then enter the secondary sedimentation. Pool; Part of the powdered activated carbon and sludge separated from the secondary sedimentation tank is returned to the water inlet of the second-stage aerobic tank, and the other part is used as a secondary gradient to use powdered activated carbon to return to the water inlet of the pre-aeration tank. The secondary sedimentation tank The effluent enters the powder activated carbon fluidized bed by self-flow;
4)通过粉末活性炭投加装置向粉末活性炭流化床内投加设定量的炭浆，在粉末活性炭流化床内吸附一段时间后的炭浆混合液进入流化床沉淀池，经过沉淀澄清分离后，出水进入混凝沉淀池，混凝沉淀池内投加复合混凝剂及助凝剂；流化床沉淀池底部的炭浆污泥一部分回流到粉末活性炭流化床的进水端，以增加粉末活性炭流化床中粉末活性炭的浓度，另一部分作为一次梯度利用粉末活性炭回流到二段好氧池的进水端；4) Add a set amount of carbon slurry into the powder activated carbon fluidized bed through the powder activated carbon dosing device, and the carbon slurry mixture after being adsorbed in the powder activated carbon fluidized bed for a period of time enters the fluidized bed sedimentation tank, and is clarified by precipitation After separation, the effluent enters the coagulation sedimentation tank, and the composite coagulant and coagulant aid are added to the coagulation sedimentation tank; a part of the carbon slurry sludge at the bottom of the fluidized bed sedimentation tank is returned to the inlet end of the powder activated carbon fluidized bed, so that the Increase the concentration of powdered activated carbon in the fluidized bed of powdered activated carbon, and the other part is used as a primary gradient to use powdered activated carbon to return to the water inlet of the second-stage aerobic tank;
5)初沉池底部剩余污泥、混凝沉淀池底部化学污泥分别送往污泥浓缩池，经浓缩后的污泥送往污泥处理单元进一步处理。5) The residual sludge at the bottom of the primary sedimentation tank and the chemical sludge at the bottom of the coagulation sedimentation tank are respectively sent to the sludge thickening tank, and the concentrated sludge is sent to the sludge treatment unit for further treatment.
一种实现粉末活性炭梯度利用的焦化废水处理工艺，所述焦化废水的原水水质、过程水质及出水水质满足以下条件：A coking wastewater treatment process for realizing gradient utilization of powdered activated carbon, wherein the raw water quality, process water quality and effluent water quality of the coking wastewater meet the following conditions:
1)焦化废水的原水水质满足：石油类≤50mg/L；CODcr≤6000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；总氮≤400mg/L： 原水温度为25～35℃；1) The raw water quality of coking wastewater meets: petroleum ≤50mg/L; CODcr ≤6000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg/L; ammonia nitrogen ≤200mg/L; total nitrogen ≤400mg/L: The raw water temperature is 25～35℃;
2)经重力除油及气浮除油处理后，进预曝气单元的焦化废水水质满足：石油类≤20mg/L；CODcr≤5000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；2) After gravity degreasing and air flotation degreasing, the water quality of coking wastewater entering the pre-aeration unit shall meet the following requirements: petroleum ≤20mg/L; CODcr ≤5000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg /L; Ammonia nitrogen≤200mg/L;
3)经预曝气池处理后，进生化处理单元的焦化废水水质满足：CODcr≤2300mg/L；挥发酚≤280mg/L；易释放氰化物≤8mg/L；油≤5mg/L，pH值6.5～7.5；3) After the pre-aeration tank treatment, the quality of the coking wastewater entering the biochemical treatment unit satisfies: CODcr≤2300mg/L; volatile phenols≤280mg/L; easily released cyanide≤8mg/L; 6.5～7.5;
4)经一段A/O池处理后的焦化废水水质满足：CODcr≤300mg/L；挥发酚≤0.5mg/L；易释放氰化物≤0.5mg/L；油≤5mg/L；氨氮≤5mg/L；总氮≤50mg/L；pH值6.5～8.5；4) The water quality of coking wastewater treated by A/O tank satisfies: CODcr≤300mg/L; Volatile phenol≤0.5mg/L; easily released cyanide≤0.5mg/L; oil≤5mg/L; ammonia nitrogen≤5mg/L L; total nitrogen≤50mg/L; pH value 6.5～8.5;
5)经二段A缺氧池和二段好氧池处理后的焦化废水水质满足：CODcr≤200mg/L；挥发酚≤0.3mg/L；易释放氰化物≤0.3mg/L；油≤2.5mg/L；氨氮≤1mg/L；总氮≤20mg/L；pH值6.5～8.5；5) The water quality of coking wastewater treated by the second-stage A anoxic tank and the second-stage aerobic tank meets: CODcr≤200mg/L; Volatile phenol≤0.3mg/L; Easy-to-release cyanide≤0.3mg/L; mg/L; ammonia nitrogen≤1mg/L; total nitrogen≤20mg/L; pH value 6.5～8.5;
6)粉末活性炭流化床出水水质满足：CODcr≤100mg/L；挥发酚≤0.2mg/L；易释放氰化物≤0.2mg/L；6) The effluent quality of powder activated carbon fluidized bed meets: CODcr≤100mg/L; volatile phenol≤0.2mg/L; easy-to-release cyanide≤0.2mg/L;
7)混凝沉淀池出水指标，满足GB16171-2012《炼焦化学工业污染物排放标准》表2要求的14项水污染物直接排放极限指标要求；具体指标为：pH值7～8；SS≤50mg/L；CODcr≤80mg/L；氨氮≤1mg/L；BOD 5≤20mg/L；总氮≤20mg/L；总磷≤1.0mg/L；石油类≤1mg/L；挥发酚≤0.1mg/L；硫化物≤0.5mg/L；苯≤0.1mg/L；氰化物≤0.2mg/L；多环芳烃≤0.05mg/L；苯并(a)芘≤0.03μg/L。7) The effluent index of the coagulation and sedimentation tank meets the requirements of 14 direct discharge limit indexes of water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standard"; the specific indexes are: pH value 7～8; SS≤50mg /L; CODcr≤80mg/L; Ammonia nitrogen≤1mg/L; BOD 5≤20mg/L; Total nitrogen≤20mg/L; L; Sulfide≤0.5mg/L; Benzene≤0.1mg/L; Cyanide≤0.2mg/L; Polycyclic Aromatic Hydrocarbons≤0.05mg/L; Benzo(a)pyrene≤0.03μg/L.
所述粉末活性炭为木质或煤质且具有不规则形状的粉末活性炭，粒度规 格为180～125μm，碘吸附值大于950mg/g，亚甲基蓝吸附值大于180mg/g，水分≤5％，强度≥90％。The powder activated carbon is wood or coal quality powder activated carbon with irregular shapes, the particle size specification is 180-125 μm, the iodine adsorption value is greater than 950 mg/g, the methylene blue adsorption value is greater than 180 mg/g, the moisture content is less than or equal to 5%, and the strength is greater than or equal to 90%. .
所述粉末活性炭流化床内的粉末活性炭投加量不低于400mg/L，污泥浓度不低于3000mg/L；所述二段好氧池内污泥浓度不低于2000mg/L；所述预曝气池内污泥浓度不低于4000mg/L；承载初始粉末活性炭的粉末活性炭流化床内水体COD值不大于200mg/L；接受一次梯度利用粉末活性炭的二段好氧池内水体COD不大于300mg/L；接受二次梯度利用粉末活性炭的预曝气池内水体COD值不大于5000mg/L。The dosage of powder activated carbon in the powder activated carbon fluidized bed is not less than 400mg/L, and the sludge concentration is not less than 3000mg/L; the sludge concentration in the second-stage aerobic tank is not less than 2000mg/L; the The sludge concentration in the pre-aeration tank is not less than 4000mg/L; the COD value of the water body in the powder activated carbon fluidized bed carrying the initial powder activated carbon is not more than 200mg/L; the COD value of the water body in the second-stage aerobic tank receiving the primary gradient utilization of powder activated carbon is not more than 200mg/L 300mg/L; COD value of water in the pre-aeration tank receiving secondary gradient utilization of powdered activated carbon is not more than 5000mg/L.
所述二段缺氧池采用生物膜法脱总氮。The second-stage anoxic tank adopts the biofilm method to remove total nitrogen.
本发明一种实现粉末活性炭梯度利用的焦化废水处理工艺的优点主要体现在如下几方面：1)梯度利用粉末活性炭，减少活性炭的投加量；2)配套设备操作简单，建设投资低；3)减少污泥产量，降低运行成本；4)能够实现稳定达标；5)提高自动化操作水平。The advantages of the coking wastewater treatment process for realizing the gradient utilization of powdered activated carbon in the present invention are mainly reflected in the following aspects: 1) gradient utilization of powdered activated carbon reduces the dosage of activated carbon; 2) the supporting equipment is easy to operate and low in construction investment; 3) Reduce sludge production and reduce operating costs; 4) can achieve stable compliance; 5) improve the level of automated operation.
二次梯度利用粉末活性炭在预曝气池及二段好氧池内可以发挥同样的吸附作用。不难理解，本发明与粉炭活性污泥法(PACT)具有同样的特点。The secondary gradient using powdered activated carbon can play the same adsorption role in the pre-aeration tank and the second-stage aerobic tank. It is not difficult to understand that the present invention has the same characteristics as the powdered carbon activated sludge process (PACT).
除特殊说明外，本发明所述预处理单元、生化处理单元及混凝沉淀池的操作条件、药剂投加品种基本同现有工艺操作要求一致。Unless otherwise specified, the operating conditions and the dosing species of the pretreatment unit, the biochemical treatment unit and the coagulation sedimentation tank of the present invention are basically the same as the existing technological operation requirements.
以下实施例在以本发明技术方案为前提下进行实施，给出了详细的实施方式和具体的操作过程，但本发明的保护范围不限于下述的实施例。下述实施例中所用方法如无特别说明均为常规方法。The following examples are implemented on the premise of the technical solutions of the present invention, and provide detailed embodiments and specific operation processes, but the protection scope of the present invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
【实施例】【Example】
本实施例中，按处理焦化废水规模100m 3/h设计，焦化废水处理系统由预处理单元、预曝气单元、生化处理单元、粉末活性炭处理单元、混凝沉淀单元及污泥处理单元组成。 In this embodiment, the coking wastewater treatment system is designed according to the treatment scale of 100m 3 /h, and the coking wastewater treatment system is composed of a pretreatment unit, a pre-aeration unit, a biochemical treatment unit, a powder activated carbon treatment unit, a coagulation sedimentation unit and a sludge treatment unit.
预处理单元采用重力除油+气浮除油技术，控制出水主要指标石油类≤20mg/L。The pretreatment unit adopts gravity degreasing + air flotation degreasing technology to control the main indicators of effluent oil ≤20mg/L.
预曝气单元由预曝气池和初沉池组成，初沉池出水满足：CODcr≤2300mg/L；挥发酚≤280mg/L；易释放氰化物≤8mg/L；油≤5mg/L，pH值至6.5～7.5之间。The pre-aeration unit is composed of a pre-aeration tank and a primary sedimentation tank. The effluent of the primary sedimentation tank meets: CODcr≤2300mg/L; The value is between 6.5 and 7.5.
生化处理单元采用两级A/O生物脱氮处理技术，一段A/O池出水水质满足：CODcr≤300mg/L、挥发酚≤0.5mg/L、易释放氰化物≤0.5mg/L、油≤5mg/L、氨氮≤5mg/L、总氮≤50mg/L、pH值至6.5～8.5之间；二段A/O系统出水水质满足：CODcr≤200mg/L、挥发酚≤0.3mg/L、易释放氰化物≤0.3mg/L、油≤2.5mg/L、氨氮≤1mg/L、总氮≤20mg/L、pH值至6.5～8.5。The biochemical treatment unit adopts two-stage A/O biological denitrification treatment technology, and the effluent quality of the first A/O tank meets: CODcr≤300mg/L, volatile phenols≤0.5mg/L, easily released cyanide≤0.5mg/L, oil≤ 5mg/L, ammonia nitrogen ≤ 5mg/L, total nitrogen ≤ 50mg/L, pH value between 6.5 and 8.5; the effluent quality of the second-stage A/O system meets: CODcr ≤ 200mg/L, volatile phenol ≤ 0.3mg/L, Easy to release cyanide≤0.3mg/L, oil≤2.5mg/L, ammonia nitrogen≤1mg/L, total nitrogen≤20mg/L, pH value to 6.5～8.5.
在粉末活性炭处理单元中，通过全自动粉末活性炭投加装置向粉末活性炭流化床内投加炭浆，采用机械或空气搅拌，粉末活性炭流化床系统出水水质满足：CODcr≤100mg/L、挥发酚≤0.2mg/L、易释放氰化物≤0.2mg/L，色度≤30度。In the powder activated carbon treatment unit, the carbon slurry is added into the powder activated carbon fluidized bed through the automatic powder activated carbon dosing device, and mechanical or air stirring is used. Phenol≤0.2mg/L, easily released cyanide≤0.2mg/L, chromaticity≤30 degrees.
在混凝沉淀单元，向混凝反应池投加高效复合混凝剂及助凝剂，混凝沉淀池出水pH值7～8、SS≤50mg/L、CODcr≤80mg/L、氨氮≤1mg/L、BOD5≤20mg/L、总氮≤20mg/L、总磷≤1.0mg/L、石油类≤1mg/L、挥发酚≤0.1mg/L、硫化物≤0.5mg/L、苯≤0.1mg/L、氰化物≤0.2mg/L、多环芳烃≤0.05mg/L、苯并(a)芘≤0.03μg/L。In the coagulation and sedimentation unit, high-efficiency composite coagulants and coagulants are added to the coagulation reaction tank. The pH value of the effluent from the coagulation sedimentation tank is 7-8, SS≤50mg/L, CODcr≤80mg/L, and ammonia nitrogen≤1mg/ L, BOD5≤20mg/L, total nitrogen≤20mg/L, total phosphorus≤1.0mg/L, petroleum≤1mg/L, volatile phenol≤0.1mg/L, sulfide≤0.5mg/L, benzene≤0.1mg /L, cyanide≤0.2mg/L, polycyclic aromatic hydrocarbons≤0.05mg/L, benzo(a)pyrene≤0.03μg/L.
本实施例实施后，与常用的焦化废水处理工艺的平均值比较，节省建设投资约150万元，占总投资的5％左右；年节省药剂方面的运行成本约121.75万元；每年少产生干污泥量约384吨。After the implementation of this example, compared with the average value of the commonly used coking wastewater treatment process, the construction investment can be saved by about 1.5 million yuan, accounting for about 5% of the total investment; the annual saving of the operating cost of chemicals is about 1.2175 million yuan; The amount of sludge is about 384 tons.
以上所述，仅为本发明较佳的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，根据本发明的技术方案及其发明构思加以等同替换或改变，都应涵盖在本发明的保护范围之内。The above description is only a preferred embodiment of the present invention, but the protection scope of the present invention is not limited to this. The equivalent replacement or change of the inventive concept thereof shall be included within the protection scope of the present invention.

Claims (10)

  1. 一种实现粉末活性炭梯度利用的焦化废水处理系统，其特征在于，包括预处理单元、预曝气单元、生化处理单元、料末活性炭处理单元及混凝沉淀单元；所述预曝气单元包括预曝气池及初沉池；所述生化处理单元包括一段A/O池、二段缺氧池、二段好氧池及二沉池；所述活性炭处理单元包括粉末活性炭流化床、流化床沉淀池及粉末活性炭投加装置；所述混凝沉淀单元包括混凝沉淀池；所述预处理单元依次连接预曝气池、初沉池、一段A/O池、二段缺氧池、二段好氧池、二沉池、粉末活性炭流化床、流化床沉淀池及混凝沉淀池；所述粉末活性炭流化床另外连接粉末活性炭投加装置；所述混凝沉淀池另外连接复合混凝剂及助凝剂投加装置；所述初沉池通过回流污泥管道一连接预曝气池；所述二沉池通过回流污泥管道二连接二段好氧池的进水端及预曝气池的进水端；所述流化床沉淀池通过活性炭管道连接粉末活性炭流化床及二段好氧池。A coking wastewater treatment system for realizing the gradient utilization of powdered activated carbon is characterized in that it includes a pretreatment unit, a preaeration unit, a biochemical treatment unit, a powder activated carbon treatment unit and a coagulation sedimentation unit; the preaeration unit includes a pretreatment unit. an aeration tank and a primary sedimentation tank; the biochemical treatment unit includes a first-stage A/O pool, a second-stage anoxic pool, a second-stage aerobic pool, and a second-stage sedimentation tank; the activated carbon treatment unit includes a powdered activated carbon fluidized bed, a fluidized bed sedimentation tank and powder activated carbon dosing device; the coagulation sedimentation unit includes a coagulation sedimentation tank; the pretreatment unit is sequentially connected to a pre-aeration tank, a primary sedimentation tank, a first-stage A/O tank, a second-stage anoxic tank, Two-stage aerobic tank, secondary sedimentation tank, powder activated carbon fluidized bed, fluidized bed sedimentation tank and coagulation sedimentation tank; the powder activated carbon fluidized bed is additionally connected to a powder activated carbon dosing device; the coagulation sedimentation tank is additionally connected Compound coagulant and coagulant aid dosing device; the primary sedimentation tank is connected to the pre-aeration tank through the return sludge pipeline 1; the secondary sedimentation tank is connected to the water inlet end of the second-stage aerobic tank through the return sludge pipeline 2 and the inlet end of the pre-aeration tank; the fluidized bed sedimentation tank is connected to the powder activated carbon fluidized bed and the second-stage aerobic tank through an activated carbon pipeline.
  2. 根据权利要求1所述的一种实现粉末活性炭梯度利用的焦化废水处理系统，其特征在于，还包括污泥浓缩池及污泥处理单元；所述初沉淀底部的污泥出口及混凝沉淀池底部的污泥出口分别连接污泥浓缩池，污泥浓缩池另外连接污泥处理单元。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon according to claim 1, further comprising a sludge concentration tank and a sludge treatment unit; a sludge outlet and a coagulation sedimentation tank at the bottom of the primary sedimentation The sludge outlet at the bottom is respectively connected to the sludge thickening tank, and the sludge thickening tank is additionally connected to the sludge treatment unit.
  3. 根据权利要求1所述的一种实现粉末活性炭梯度利用的焦化废水处理系统，其特征在于，所述粉末活性炭投加装置由真空上料装置、备料和储料系统、浆料准备系统及浆料输送系统组成。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon according to claim 1, wherein the powdered activated carbon dosing device is composed of a vacuum feeding device, a material preparation and storage system, a slurry preparation system and a slurry Conveying system composition.
  4. 根据权利要求1所述的一种实现粉末活性炭梯度利用的焦化废水处理系统，其特征在于，所述预处理单元至少包括重力除油装置及气浮除油装置。A coking wastewater treatment system for realizing gradient utilization of powdered activated carbon according to claim 1, wherein the pretreatment unit at least comprises a gravity degreasing device and an air flotation degreasing device.
  5. 根据权利要求1所述的一种实现粉末活性炭梯度利用的焦化废水处理 系统，其特征在于，所述粉末活性炭流化床内设机械搅拌装置或空气搅拌装置。A kind of coking wastewater treatment system realizing powder activated carbon gradient utilization according to claim 1, is characterized in that, described powder activated carbon fluidized bed is provided with mechanical stirring device or air stirring device.
  6. 基于权利要求1～5任意一种所述系统的实现粉末活性炭梯度利用的焦化废水处理工艺，其特征在于，包括如下步骤：The coking wastewater treatment process for realizing the gradient utilization of powdered activated carbon based on any one of the systems of claims 1 to 5, is characterized in that, it includes the following steps:
    1)焦化废水先进入预处理单元，进行重力除油及气浮除油处理；1) The coking wastewater first enters the pretreatment unit for gravity degreasing and air flotation degreasing;
    2)预处理单元出水靠自流依次进入预曝气池及初沉池，在此过程中，实现生物絮凝吸附，同时发生不完全氧化反应；初沉池出水自流进入一段A/O池；2) The effluent of the pretreatment unit enters the pre-aeration tank and the primary sedimentation tank in turn by self-flow. In this process, biological flocculation and adsorption are realized, and incomplete oxidation reaction occurs at the same time;
    3)焦化废水依次流经一段A/O池、二段缺氧池及二段好氧池，进行硝化、反硝化脱氮、脱碳反应，并对其它污染物进行生物降解，然后进入二沉池；二沉池分离出的粉末活性炭及污泥，一部分回流到二段好氧池的进水端，另一部分作为二次梯度利用粉末活性炭回流到预曝气池的进水端，二沉池出水靠自流进入粉末活性炭流化床；3) The coking wastewater flows through the first-stage A/O pool, the second-stage anoxic pool and the second-stage aerobic pool in turn to carry out nitrification, denitrification, denitrification, and decarbonization reactions, and biodegrade other pollutants, and then enter the secondary sedimentation. Pool; Part of the powdered activated carbon and sludge separated from the secondary sedimentation tank is returned to the water inlet of the second-stage aerobic tank, and the other part is used as a secondary gradient to use powdered activated carbon to return to the water inlet of the pre-aeration tank. The secondary sedimentation tank The effluent enters the powder activated carbon fluidized bed by self-flow;
    4)通过粉末活性炭投加装置向粉末活性炭流化床内投加设定量的炭浆，在粉末活性炭流化床内吸附一段时间后的炭浆混合液进入流化床沉淀池，经过沉淀澄清分离后，出水进入混凝沉淀池，混凝沉淀池内投加复合混凝剂及助凝剂；流化床沉淀池底部的炭浆污泥一部分回流到粉末活性炭流化床的进水端，以增加粉末活性炭流化床中粉末活性炭的浓度，另一部分作为一次梯度利用粉末活性炭回流到二段好氧池的进水端；4) Add a set amount of carbon slurry into the powder activated carbon fluidized bed through the powder activated carbon dosing device, and the carbon slurry mixture after being adsorbed in the powder activated carbon fluidized bed for a period of time enters the fluidized bed sedimentation tank, and is clarified by precipitation After separation, the effluent enters the coagulation sedimentation tank, and the composite coagulant and coagulant aid are added to the coagulation sedimentation tank; a part of the carbon slurry sludge at the bottom of the fluidized bed sedimentation tank is returned to the inlet end of the powder activated carbon fluidized bed, so that the Increase the concentration of powdered activated carbon in the fluidized bed of powdered activated carbon, and the other part is used as a primary gradient to use powdered activated carbon to return to the water inlet of the second-stage aerobic tank;
    5)初沉池底部剩余污泥、混凝沉淀池底部化学污泥分别送往污泥浓缩池，经浓缩后的污泥送往污泥处理单元进一步处理。5) The residual sludge at the bottom of the primary sedimentation tank and the chemical sludge at the bottom of the coagulation sedimentation tank are respectively sent to the sludge thickening tank, and the concentrated sludge is sent to the sludge treatment unit for further treatment.
  7. 根据权利要求6所述的一种实现粉末活性炭梯度利用的焦化废水处理 工艺，其特征在于，所述焦化废水的原水水质、过程水质及出水水质满足以下条件：A kind of coking wastewater treatment process realizing powder activated carbon gradient utilization according to claim 6, is characterized in that, the raw water quality, process water quality and effluent water quality of described coking wastewater meet the following conditions:
    1)焦化废水的原水水质满足：石油类≤50mg/L；CODcr≤6000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；总氮≤400mg/L：原水温度为25～35℃；1) The raw water quality of coking wastewater meets: petroleum ≤50mg/L; CODcr ≤6000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg/L; ammonia nitrogen ≤200mg/L; total nitrogen ≤400mg/L: The raw water temperature is 25～35℃;
    2)经重力除油及气浮除油处理后，进预曝气单元的焦化废水水质满足：石油类≤20mg/L；CODcr≤5000mg/L；释放氰化物≤20mg/L；挥发酚≤800mg/L；氨氮≤200mg/L；2) After gravity degreasing and air flotation degreasing, the water quality of coking wastewater entering the pre-aeration unit shall meet the following requirements: petroleum ≤20mg/L; CODcr ≤5000mg/L; released cyanide ≤20mg/L; volatile phenol ≤800mg /L; Ammonia nitrogen≤200mg/L;
    3)经预曝气池处理后，进生化处理单元的焦化废水水质满足：CODcr≤2300mg/L；挥发酚≤280mg/L；易释放氰化物≤8mg/L；油≤5mg/L，pH值6.5～7.5；3) After the pre-aeration tank treatment, the quality of the coking wastewater entering the biochemical treatment unit satisfies: CODcr≤2300mg/L; volatile phenols≤280mg/L; easily released cyanide≤8mg/L; 6.5～7.5;
    4)经一段A/O池处理后的焦化废水水质满足：CODcr≤300mg/L；挥发酚≤0.5mg/L；易释放氰化物≤0.5mg/L；油≤5mg/L；氨氮≤5mg/L；总氮≤50mg/L；pH值6.5～8.5；4) The water quality of coking wastewater treated by A/O tank satisfies: CODcr≤300mg/L; Volatile phenol≤0.5mg/L; easily released cyanide≤0.5mg/L; oil≤5mg/L; ammonia nitrogen≤5mg/L L; total nitrogen≤50mg/L; pH value 6.5～8.5;
    5)经二段A缺氧池和二段好氧池处理后的焦化废水水质满足：CODcr≤200mg/L；挥发酚≤0.3mg/L；易释放氰化物≤0.3mg/L；油≤2.5mg/L；氨氮≤1mg/L；总氮≤20mg/L；pH值6.5～8.5；5) The water quality of coking wastewater treated by the second-stage A anoxic tank and the second-stage aerobic tank meets: CODcr≤200mg/L; Volatile phenol≤0.3mg/L; Easy-to-release cyanide≤0.3mg/L; mg/L; ammonia nitrogen≤1mg/L; total nitrogen≤20mg/L; pH value 6.5～8.5;
    6)粉末活性炭流化床出水水质满足：CODcr≤100mg/L；挥发酚≤0.2mg/L；易释放氰化物≤0.2mg/L；6) The effluent quality of powder activated carbon fluidized bed meets: CODcr≤100mg/L; volatile phenol≤0.2mg/L; easy-to-release cyanide≤0.2mg/L;
    7)混凝沉淀池出水指标，满足GB16171-2012《炼焦化学工业污染物排放标准》表2要求的14项水污染物直接排放极限指标要求；具体指标为：pH值7～8；SS≤50mg/L；CODcr≤80mg/L；氨氮≤1mg/L；BOD5≤20mg/L； 总氮≤20mg/L；总磷≤1.0mg/L；石油类≤1mg/L；挥发酚≤0.1mg/L；硫化物≤0.5mg/L；苯≤0.1mg/L；氰化物≤0.2mg/L；多环芳烃≤0.05mg/L；苯并(a)芘≤0.03μg/L。7) The effluent index of the coagulation and sedimentation tank meets the requirements of 14 direct discharge limit indexes of water pollutants required in Table 2 of GB16171-2012 "Coking Chemical Industry Pollutant Discharge Standard"; the specific indexes are: pH value 7～8; SS≤50mg /L; CODcr≤80mg/L; ammonia nitrogen≤1mg/L; BOD5≤20mg/L; total nitrogen≤20mg/L; total phosphorus≤1.0mg/L; petroleum≤1mg/L; volatile phenol≤0.1mg/L ; Sulfide≤0.5mg/L; Benzene≤0.1mg/L; Cyanide≤0.2mg/L; Polycyclic aromatic hydrocarbons≤0.05mg/L; Benzo(a)pyrene≤0.03μg/L.
  8. 根据权利要求6所述的一种实现粉末活性炭梯度利用的焦化废水处理工艺，其特征在于，所述粉末活性炭为木质或煤质且具有不规则形状的粉末活性炭，粒度规格为180～125μm，碘吸附值大于950mg/g，亚甲基蓝吸附值大于180mg/g，水分≤5％，强度≥90％。The coking wastewater treatment process for realizing the gradient utilization of powdered activated carbon according to claim 6, wherein the powdered activated carbon is wood or coal-like powdered activated carbon with irregular shape, the particle size specification is 180-125 μm, the iodine The adsorption value is greater than 950mg/g, the methylene blue adsorption value is greater than 180mg/g, the moisture content is less than or equal to 5%, and the strength is greater than or equal to 90%.
  9. 根据权利要求6所述的一种实现粉末活性炭梯度利用的焦化废水处理工艺，其特征在于，所述粉末活性炭流化床内的粉末活性炭投加量不低于400mg/L，污泥浓度不低于3000mg/L；所述二段好氧池内污泥浓度不低于2000mg/L；所述预曝气池内污泥浓度不低于4000mg/L；承载初始粉末活性炭的粉末活性炭流化床内水体COD值不大于200mg/L；接受一次梯度利用粉末活性炭的二段好氧池内水体COD不大于300mg/L；接受二次梯度利用粉末活性炭的预曝气池内水体COD值不大于5000mg/L。The coking wastewater treatment process for realizing gradient utilization of powdered activated carbon according to claim 6, wherein the dosage of powdered activated carbon in the powdered activated carbon fluidized bed is not less than 400 mg/L, and the sludge concentration is not low The sludge concentration in the second-stage aerobic tank is not less than 2000mg/L; the sludge concentration in the pre-aeration tank is not less than 4000mg/L; the water body in the powder activated carbon fluidized bed carrying the initial powder activated carbon The COD value is not more than 200mg/L; the COD of the water body in the second-stage aerobic tank receiving the primary gradient utilization of powder activated carbon is not more than 300mg/L; the COD value of the water body in the pre-aeration tank receiving the secondary gradient utilization of powder activated carbon is not more than 5000mg/L.
  10. 根据权利要求6所述的一种实现粉末活性炭梯度利用的焦化废水处理工艺，其特征在于，所述二段缺氧池采用生物膜法脱总氮。The coking wastewater treatment process for realizing the gradient utilization of powdered activated carbon according to claim 6, wherein the second-stage anoxic tank adopts a biofilm method to remove total nitrogen.
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