CN113511775A - Finished oil depot sewage treatment system and finished oil depot sewage treatment method - Google Patents

Finished oil depot sewage treatment system and finished oil depot sewage treatment method Download PDF

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Publication number
CN113511775A
CN113511775A CN202010281581.6A CN202010281581A CN113511775A CN 113511775 A CN113511775 A CN 113511775A CN 202010281581 A CN202010281581 A CN 202010281581A CN 113511775 A CN113511775 A CN 113511775A
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Prior art keywords
tank
hours
internal circulation
water
sewage
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CN202010281581.6A
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Chinese (zh)
Inventor
姚猛
周志国
郭亚逢
唐晓丽
卢薇
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China Petroleum and Chemical Corp
Sinopec Qingdao Safety Engineering Institute
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China Petroleum and Chemical Corp
Sinopec Qingdao Safety Engineering Institute
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Priority to CN202010281581.6A priority Critical patent/CN113511775A/en
Publication of CN113511775A publication Critical patent/CN113511775A/en
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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
    • C02F1/40—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
    • C02F1/72—Treatment of water, waste water, or sewage by 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
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • 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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/06—Aerobic processes using submerged filters
    • 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
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1263—Sequencing batch reactors [SBR]
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C02F3/2873—Particular arrangements for anaerobic reactors with internal draft tube circulation

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

The invention relates to the field of wastewater treatment, and discloses a finished oil depot sewage treatment system and a finished oil depot sewage treatment method. The finished oil depot sewage treatment system is sequentially provided with a regulating tank (1), an oil separation tank (2), an air floatation tank (3), an internal circulation anaerobic reactor (4), a pre-oxidation water tank (5), an MBR (membrane bioreactor) (6), an ozone catalytic oxidation tank (7) and an internal circulation BAF (biological aerated filter) tank (8) according to the sewage treatment flow direction. By the system and the method for treating the sewage of the finished oil depot, organic pollutants in the sewage of the finished oil depot can be thoroughly degraded, and the sewage can be discharged up to the standard.

Description

Finished oil depot sewage treatment system and finished oil depot sewage treatment method
Technical Field
The invention relates to the field of wastewater treatment, in particular to a finished oil depot sewage treatment system and a finished oil depot sewage treatment method.
Background
The top water operation of the finished oil depot can generate a large amount of oily sewage, the sewage discharge period is irregular, and the sewage quality has the characteristics of high petroleum, high COD and poor biodegradability (B/C is less than 0.2). At present, the oil removal-air flotation-biochemical treatment process commonly adopted by the oil depot is difficult to realize the standard discharge of sewage because the concentration of sewage pollutants in the oil depot is high and the biodegradability is poor, and the process cannot thoroughly degrade organic pollutants in the sewage.
Disclosure of Invention
The invention aims to solve the problem that the finished oil depot sewage is difficult to completely degrade organic pollutants in the sewage in the prior art, and provides a finished oil depot sewage treatment system and a finished oil depot sewage treatment method.
In order to achieve the above object, in one aspect, the present invention provides a product oil depot sewage treatment system, wherein the product oil depot sewage treatment system is sequentially provided with a regulating tank, an oil separation tank, an air flotation tank, an internal circulation anaerobic reactor, a pre-oxidation water tank, an MBR membrane bioreactor, an ozone catalytic oxidation tank and an internal circulation BAF tank according to a sewage treatment flow direction.
Preferably, the height-diameter ratio of the internal circulation anaerobic reactor is more than or equal to 8, and at least two stages of three-phase separators are arranged in the reactor.
Preferably, the ratio of the height to the diameter of the internal circulation anaerobic reactor 4 is 10 to 20.
Preferably, a catalyst filler layer is arranged in the pre-oxidation water tank, and the catalyst filler layer is gamma-Al loaded with active ingredients2O3A catalyst layer formed by filling the balls.
Preferably, the active ingredient is one or more of cerium nitrate, lanthanum nitrate, potassium nitrate and copper nitrate.
Preferably, the content of the active ingredient is 8 to 20 mass%.
Preferably, gamma-Al loaded with active ingredient2O3The particle size of the ball is 3-5 mm.
Preferably, in the MBR, an MBR membrane bioreactor membrane component is made of Al2O3The pore diameter of the flat inorganic microporous ceramic membrane used as the substrate is 0.1-0.3 μm.
Preferably, the upper part of the ozone catalytic oxidation tank is filled with water, the bottom of the ozone catalytic oxidation tank is filled with water, ozone enters from the bottom of the tank, is dispersed into the water through a pure titanium aeration disc, and is discharged from the top of the tank.
Preferably, the ozone catalytic oxidation tank is filled with a catalyst bed layer.
Preferably, the catalyst is gamma-Al loaded with active components2O3The active component is at least one of manganese dioxide, ferric oxide, titanium dioxide and cerium oxide.
Preferably, the content of the active ingredient is 10 to 22 mass%, preferably 13 to 18 mass%.
Preferably, the catalyst has a particle size of 2 to 8mm, preferably 4 to 6 mm.
Preferably, an ozone tail gas outlet discharged from the top of the ozone catalytic oxidation tank is communicated with the bottom of the pre-oxidation water tank.
Preferably, the ozone tail gas discharged from the top of the ozone catalytic oxidation tank is dispersed into water through a pure titanium aeration disc from the bottom of the pre-oxidation water tank by a draught fan.
Preferably, the internal circulation BAF pool is of an upflow type, sewage enters from the bottom and is discharged from the upper part after passing through the filler layer.
Preferably, the filler layer comprises a supporting layer and a biological filler layer positioned on the upper part of the supporting layer.
Preferably, the supporting layer is filled with pebbles, and the particle size of the pebbles is 4-6 cm.
Preferably, the filler filled in the biological filler layer is at least one selected from volcanic rock particles, ceramsite, coke particles and expanded aluminosilicate particles.
According to a second aspect of the invention, a method for treating the sewage of the finished oil depot is provided, wherein the sewage of the finished oil depot is treated by using the sewage treatment system of the finished oil depot, wherein the sewage of the finished oil depot is sequentially treated in a regulating tank, an oil separation tank, an air flotation tank, an internal circulation anaerobic reactor, a pre-oxidation water tank, an MBR (membrane bioreactor), an ozone catalytic oxidation tank and an internal circulation BAF (biological aerated filter) tank according to the sewage treatment flow direction.
Preferably, the hydraulic retention time of the finished oil depot wastewater in the adjusting tank is more than 20 hours, preferably 20 to 50 hours, and more preferably 20 to 30 hours.
Preferably, the oil separation tank is multistage, preferably more than 2 stages, and more preferably 2-5 stages.
Preferably, the hydraulic retention time of each oil interceptor stage is above 9 hours, preferably 9-25 hours, more preferably 9-15 hours.
Preferably, a flocculating agent is put into the sewage in the air floatation tank.
Preferably, the flocculating agent is polyaluminium chloride and polyacrylamide.
Preferably, the amount of the polyaluminum chloride is 100-400mg/L, preferably 200-300 mg/L.
Preferably, the amount of the polyaluminium chloride is 1-8mg/L, preferably 3-5 mg/L.
Preferably, the hydraulic retention time of the air floatation tank is 1-5 hours, and preferably 2-3 hours.
Preferably, the air-water volume ratio of the air flotation tank is 5-15, and preferably 9-11.
Preferably, the hydraulic retention time of the internal circulation anaerobic reactor is 2 to 10 hours, preferably 4.5 to 7.5 hours.
Preferably, the internal circulation ratio (ratio of the amount of circulating water to the amount of inlet water) of the internal circulation anaerobic reactor is 5 to 25, preferably 10 to 20.
Preferably, the hydraulic retention time of the pre-oxidation basin is between 0.5 and 3 hours, preferably between 1 and 1.5 hours.
Preferably, the hydraulic retention time of the MBR membrane bioreactor is 8-25 hours, preferably 10-23 hours.
Preferably, the hydraulic retention time of the ozone catalytic oxidation tank is 2 to 8 hours, preferably 4 to 6 hours.
Preferably, the ozone dose is 50-100gO3Pert water, preferably 40-90gO3Water per ton.
Preferably, the hydraulic retention time of the internal circulation BAF tank is 2-8 hours, preferably 4-6 hours.
Preferably, the internal circulation ratio (ratio of the amount of circulating water to the amount of inlet water) of the internal circulation BAF tank is 3 to 15, preferably 5 to 9.
Preferably, the gas-water volume ratio of the internal circulation BAF pool is 5-25, preferably 10-20.
According to the invention, the advantages of anaerobic property, ozone catalytic oxidation and a biomembrane method are fully exerted, organic pollutants which cannot be degraded by a traditional biochemical treatment unit can be effectively removed, and the sewage discharge reaching the standard is realized.
Drawings
FIG. 1 is a schematic diagram of a finished oil depot sewage treatment system.
Description of the reference numerals
1: and (3) adjusting the pool 2: oil separation tank
3: and (4) floatation tank: internal circulation anaerobic reactor
5: a pre-oxidation water tank 6: MBR membrane bioreactor
7: ozone catalytic oxidation jar 8: internal circulation BAF pool
9: air inducing unit
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
FIG. 1 is a schematic diagram of a finished oil depot sewage treatment system. As shown in fig. 1, the system for treating the sewage of the finished oil depot according to the first aspect of the present invention sequentially comprises a regulating tank 1, an oil separation tank 2, an air flotation tank 3, an internal circulation anaerobic reactor 4, a pre-oxidation water tank 5, an MBR membrane bioreactor 6, an ozone catalytic oxidation tank 7, and an internal circulation BAF tank 8 according to the sewage treatment flow direction.
According to the present invention, the conditioning tank 1 is used for adjusting the amount of wastewater and the quality of water, and various conditioning tanks generally used in the field for adjusting the amount of wastewater and the quality of water can be used. Through the adjusting tank, a large amount of oil substances in the sewage float to the water surface, and suspended matters with large density water precipitate to the bottom of the tank, so that the effects of preliminary precipitation and oil separation are achieved. The wastewater treated in the regulating reservoir 1 can enter a subsequent treatment unit at a fixed flow rate by a water pump or by self-flow.
According to the invention, the oil interceptor 2 is of a variety of oil interceptors used in the art for oil interceptors. In the oil separation tank 2, the floating oil in the water rises to the water surface by virtue of the oil-water density difference, and the floating oil in the water can be removed through oil separation treatment. The number of stages of the oil interceptor 2 may be 1 stage or multiple stages, preferably 3 stages or more, for example, 2 to 5 stages, and particularly preferably 3 stages.
According to the present invention, the flotation tank 3 is various flotation tanks commonly used in the art. Preferably, the air flotation tank 3 adopts a dissolved air flotation mode, and takes tail gas discharged from the ozone catalytic oxidation tank as an air source, and plays a role in pre-oxidizing sewage. In addition, the air flotation tank 3 is provided with a dosing system, and a flocculating agent (such as polyaluminium chloride and polyacrylamide) and the like can be added at the water inlet end through the dosing system, so that emulsified oil in sewage is demulsified and condensed to float to the water surface along with micro bubbles, and the purpose of removing the emulsified oil in the water is achieved.
According to the present invention, the internal circulation anaerobic reactor 4 may be various internal circulation anaerobic reactors commonly used in the art. Preferably, the height-diameter ratio of the internal circulation anaerobic reactor 4 is more than or equal to 8, and at least two stages of three-phase separators are arranged in the reactor; more preferably, the ratio of the height to the diameter of the internal circulation anaerobic reactor 4 is 10 to 20.
According to the invention, the effluent of the air floatation tank 3 enters the internal circulation anaerobic reactor 4, and the anaerobic sludge in the internal circulation anaerobic reactor is utilized to decompose the organic sewage which is difficult to decompose by aerobic microorganisms in the sewage, so that the biodegradability of the sewage is improved while the organic matters are removed.
According to the present invention, the pre-oxidation water bath 5 may be various pre-oxidation water baths generally used for pre-oxidation in the art.
Preferably, a catalyst filler layer is arranged in the pre-oxidation water tank 5, and the catalyst filler layer is gamma-Al loaded with active ingredients2O3A catalyst layer formed by filling the balls. Preferably, the active ingredient is one or more of cerium nitrate, lanthanum nitrate, potassium nitrate and copper nitrate. The content of the active ingredient may be 8 to 20 mass%, preferably 10 to 15 mass%. In addition, the gamma-Al loaded with active component2O3The particle size of the spheres is preferably 3 to 5 mm.
According to the invention, preferably, the effluent of the internal circulation anaerobic reactor 4 enters from the upper part of the pre-oxidation water tank 5 and flows out from the lower part, the ozone tail gas discharged from the top of the oxygen catalytic oxidation tank 7 is dispersed into water from the bottom of the pre-oxidation water tank 5 through a pure titanium aeration disc through an induced air unit 9, the sewage and the ozone are fully contacted and reacted with a catalyst bed layer, and organic pollutants in the sewage are pre-oxidized in the pre-oxidation water tank 5, so that the biodegradability of the sewage can be further improved, and a part of organic pollutants can be removed.
According to the present invention, the MBR membrane bioreactor 6 is any of various MBR membrane bioreactors commonly used in the art for membrane separation. Preferably, in the MBR membrane bioreactor 6, the membrane component of the MBR membrane bioreactor adopts Al2O3The pore diameter of the flat inorganic microporous ceramic membrane used as the substrate is 0.1-0.3 μm.
According to the invention, the effluent of the pre-oxidation water tank 5 enters the MBR membrane bioreactor 6, sewage is fully contacted with activated sludge and dissolved oxygen, and pollutants in the water are adsorbed and degraded by aerobic microorganisms; an aeration device is arranged in the MBR membrane bioreactor 6, and sewage enters the tank and is fully mixed with activated sludge in the tank immediately; the effluent of the full-mixing aeration tank is filtered by a microporous inorganic ceramic membrane, the concentration of suspended matters in the effluent is low, and a sedimentation tank is not required.
According to the present invention, the ozone catalytic oxidation tank 7 is various ozone catalytic oxidation tanks generally used for ozone catalysis in the art. Preferably, the ozone catalytic oxidation tank 7 is filled with water from the upper part and drained from the bottom, and ozone enters from the bottom of the tank, is dispersed into water through a pure titanium aeration disc and is drained from the top of the tank.
Preferably, the ozone catalytic oxidation tank 7 is filled with a catalyst bed layer. The catalyst is preferably gamma-Al loaded with active components2O3The active component is at least one of manganese dioxide, ferric oxide, titanium dioxide and cerium oxide. The content of the active ingredient is 10 to 22 mass%, preferably 13 to 18 mass%. Furthermore, the particle size of the catalyst is 2 to 8mm, preferably 4 to 6 mm.
According to the invention, preferably, an ozone tail gas outlet discharged from the top of the ozone catalytic oxidation tank 7 is communicated with the bottom of the pre-oxidation water tank; more preferably, the ozone tail gas discharged from the top of the ozone catalytic oxidation tank 7 is dispersed into water from the bottom of the pre-oxidation water tank through a pure titanium aeration disc through an air inducing unit 9. The induced draft unit 9 may be various devices commonly used in the art for inducing draft, for example, an induced draft fan.
According to the invention, the effluent of the MBR membrane bioreactor 6 enters the ozone catalytic oxidation tank 7 from the top of the ozone catalytic oxidation, and pollutants which cannot be biodegraded in the sewage in the treatment unit are oxidized and decomposed in the ozone catalytic oxidation tank 7, and meanwhile, difficultly-degradable organic matters are further degraded, so that the biodegradability of the sewage is improved.
According to the invention, the internal circulation BAF tank 8 is preferably of the upflow type, the sewage entering from the bottom and exiting from the top after passing through the packing layer. Preferably, the filler layer comprises a supporting layer and a biological filler layer positioned on the upper part of the supporting layer.
Preferably, the supporting layer is filled with pebbles, and the particle size of the pebbles is 4-6 cm.
Preferably, the filler filled in the biological filler layer is at least one selected from volcanic rock particles, ceramsite, coke particles and expanded aluminosilicate particles.
In a preferred embodiment of the invention, the biological filler layer is filled with volcanic rock particles, the particle size of the volcanic rock particles is 1.5-3.5cm, and the density is 1.8-2.2g/cm3Specific surface area 8X 104-9×104cm2The filling porosity is 55-65%, and the intra-granular porosity is 20-30%.
In a preferred embodiment of the invention, the biological filler layer 4 is filled with ceramsite, the particle size of the ceramsite is 3-4cm, and the density of the ceramsite is 1.6-1.8g/cm3Specific surface area 4.2X 104cm2The filling porosity is 10-20 percent and the intra-granular porosity is 30-40 percent.
In a preferred embodiment of the present invention, the bio-filler layer 4 is filled with coke particles having a particle size of 1-3cm and a density of 1.8g/cm3Specific surface area 4.2X 104cm2The filling porosity is 35 percent and the intra-granular porosity is 25 percent.
According to the invention, the effluent of the ozone catalytic oxidation tank 7 enters the internal circulation BAF tank 8, pollutants which cannot be biodegraded in the sewage in the treatment unit are further decomposed in the internal circulation BAF tank, the purpose of further purifying the water quality is achieved, and finally the effluent can reach the standard and be discharged.
According to a second aspect of the invention, a method for treating the sewage of the finished oil depot is provided, wherein the sewage of the finished oil depot is treated by using the sewage treatment system of the finished oil depot, wherein the sewage of the finished oil depot is sequentially treated in a regulating tank 1, an oil separation tank 2, an air flotation tank 3, an internal circulation anaerobic reactor 4, a pre-oxidation water tank 5, an MBR (membrane bioreactor) 6, an ozone catalytic oxidation tank 7 and an internal circulation BAF (biological aerated Filter) tank 8 according to the sewage treatment flow direction.
According to the method, the COD of the finished product oil depot sewage can be 2000-4000mg/L, and the COD of the petroleum can be 50-90mg/L, preferably, the COD of the finished product oil depot sewage is 3500-4000mg/L, and the COD of the petroleum is 80-90 mg/L.
The conditions for performing the treatment in each unit will be described below.
1. Treatment conditions in the adjusting tank 1
According to the present invention, preferably, the hydraulic retention time of the finished oil depot wastewater in the adjusting tank 1 may be 20 hours or more, preferably 20 to 50 hours, and more preferably 20 to 30 hours.
In addition, the COD of the effluent of the regulating tank 1 can be 1600-2500mg/L, and the content of petroleum can be 45-70 mg/L; preferably, the COD of the effluent of the adjusting tank 1 can be 1900-2300mg/L, and the COD of the petroleum can be 50-60 mg/L.
Through the adjusting tank 1, a large amount of oil substances in the sewage float to the water surface, and suspended matters with large density water precipitate to the bottom of the tank, so that the effects of preliminary precipitation and oil separation are achieved. The wastewater treated in the regulating reservoir 1 can enter a subsequent treatment unit at a fixed flow rate by a water pump or by self-flow.
2. Treatment conditions in the oil interceptor 2
According to the present invention, the oil separation tank 2 is preferably multi-stage, preferably 3 or more, and more preferably 3 to 5 stages.
Preferably, the hydraulic retention time of each oil interceptor stage is above 9 hours, preferably 9-25 hours, more preferably 9-15 hours.
The COD of the effluent of the oil separation tank 2 can be 1500-2000mg/L, and the COD of the petroleum can be 25-35 mg/L; preferably, the effluent COD of the oil separation tank 2 is 1500-1800mg/L, and the petroleum is 50-60 mg/L.
According to the present invention, in the oil separation tank 2, the floating oil in the water rises to the water surface by the difference in oil-water density, and the floating oil in the water can be removed by oil separation treatment.
3. Treatment conditions of the flotation tank 3
According to the present invention, it is preferable that a flocculant is added to the sewage in the flotation tank 3. The flocculant may be various substances commonly used in the art for flocculation, and preferably, the flocculant is polyaluminum chloride and polyacrylamide.
When polyaluminium chloride and polyacrylamide are used as flocculating agents, the dosage of the polyaluminium chloride is 100-400mg/L, preferably 200-300 mg/L; the dosage of the polyaluminium chloride is 1-8mg/L, preferably 3-5 mg/L.
Preferably, the hydraulic retention time of the air flotation tank 3 is 1-5 hours, and preferably 2-3 hours.
Preferably, the air-water volume ratio of the air flotation tank 3 is 5-15, preferably 9-11.
The COD of the effluent of the air floatation tank 3 can be 900-1400mg/L, and the content of petroleum can be 8-22 mg/L; preferably, the COD of the effluent of the air floatation tank 3 is 1000-1300mg/L, and the content of petroleum is 10-20 mg/L.
4. Treatment conditions of the internal circulation anaerobic reactor 4
According to the present invention, it is preferable that the hydraulic retention time of the internal circulation anaerobic reactor 4 is 2 to 10 hours, preferably 4.5 to 7.5 hours.
Preferably, the internal circulation ratio (ratio of the amount of circulating water to the amount of inlet water) of the internal circulation anaerobic reactor (4) is 5 to 25, preferably 10 to 20.
The COD of the effluent of the internal circulation anaerobic reactor 4 can be 600-850mg/L, and the content of petroleum can be below 7 mg/L; preferably, the effluent COD of the internal circulation anaerobic reactor 4 is 700-800mg/L, and the petroleum is 10-20 mg/L.
According to the invention, the effluent of the air floatation tank 3 enters the internal circulation anaerobic reactor 4, and the anaerobic sludge in the internal circulation anaerobic reactor is utilized to decompose the organic sewage which is difficult to decompose by aerobic microorganisms in the sewage, so that the biodegradability of the sewage is improved while the organic matters are removed.
5. Treatment conditions of the pre-oxidation pond 5
According to the invention, the hydraulic retention time of the pre-oxidation basin 5 is preferably between 0.5 and 3 hours, preferably between 1 and 1.5 hours.
The COD of the effluent of the pre-oxidation water tank 5 can be 500-690mg/L, and the content of petroleum can be below 2 mg/L; preferably, the COD of the effluent of the pre-oxidation water tank 5 is 550-680 mg/L.
According to the invention, preferably, the effluent of the internal circulation anaerobic reactor 4 enters from the upper part of the pre-oxidation water tank 5 and flows out from the lower part, the ozone tail gas discharged from the top of the oxygen catalytic oxidation tank 7 is dispersed into water from the bottom of the pre-oxidation water tank 5 through a pure titanium aeration disc through an induced air unit 9, the sewage and the ozone are fully contacted and reacted with a catalyst bed layer, and organic pollutants in the sewage are pre-oxidized in the pre-oxidation water tank 5, so that the biodegradability of the sewage can be further improved, and a part of organic pollutants can be removed.
6. Treatment conditions of MBR (membrane bioreactor) 6
According to the present invention, the hydraulic retention time of the MBR membrane bioreactor 6 is preferably 8-25 hours, preferably 10-23 hours.
The COD of the effluent of the MBR membrane bioreactor 6 can be 80-150mg/L, and the content of petroleum can be below 1 mg/L; preferably, the COD of the effluent of the MBR membrane bioreactor 6 is 90-120 mg/L.
According to the invention, the effluent of the pre-oxidation water tank 5 enters the MBR membrane bioreactor 6, sewage is fully contacted with activated sludge and dissolved oxygen, and pollutants in the water are adsorbed and degraded by aerobic microorganisms; an aeration device is arranged in the MBR membrane bioreactor 6, and sewage enters the tank and is fully mixed with activated sludge in the tank immediately; the effluent of the full-mixing aeration tank is filtered by a microporous inorganic ceramic membrane, the concentration of suspended matters in the effluent is low, and a sedimentation tank is not required.
7. Treatment conditions of the ozone catalytic oxidation tank 7
According to the invention, the hydraulic retention time of the ozone catalytic oxidation tank 7 is preferably 2 to 8 hours, preferably 4 to 6 hours.
Preferably, the ozone dose is 50-100gO3Pert water, preferably 40-90gO3Water per ton.
The COD of the effluent of the ozone catalytic oxidation tank 7 can be 60-90mg/L, and the content of petroleum can be below 1 mg/L; preferably, the COD of the effluent of the ozone catalytic oxidation tank 7 is 70-88 mg/L.
According to the invention, the effluent of the MBR membrane bioreactor 6 enters the ozone catalytic oxidation tank 7 from the top of the ozone catalytic oxidation, and pollutants which cannot be biodegraded in the sewage in the treatment unit are oxidized and decomposed in the ozone catalytic oxidation tank 7, and meanwhile, difficultly-degradable organic matters are further degraded, so that the biodegradability of the sewage is improved.
8. Treatment conditions of the internal circulation BAF tank 8
According to the invention, the internal circulation BAF basin (8) preferably has a hydraulic retention time of 2 to 8 hours, preferably 4 to 6 hours.
Preferably, the internal circulation ratio (ratio of circulating water amount to inlet water amount) of the internal circulation BAF tank (8) is 3-15, preferably 5-9.
Preferably, the gas-water volume ratio of the internal circulation BAF pool (8) is 5-25, preferably 10-20.
Through the treatment, the COD of the effluent of the internal circulation BAF pool 8 is 66mg/L, and the content of petroleum can be below 1mg/L, so that the effluent reaches the discharge standard.
In addition, when the quality of the effluent water of the internal circulation BAF pool 8 or the ozone catalytic oxidation tank 7 is reduced or the turbidity of the effluent water is increased, an air compressor can be started to provide compressed air, the compressed air is stabilized by an air storage tank and then is introduced from the bottom of the internal circulation BAF pool 8 or the ozone catalytic oxidation tank 7 to flush a packing layer, then a backwashing water pump is started to pump water from a clean water tank and introduce water from the bottom of the internal circulation BAF pool 8 or the ozone catalytic oxidation tank 7, gas and water combined backwashing is performed, backwashing water flows into a backwashing settling tank through a backwashing pipeline, backwashing is performed for 5-10 minutes every time, and after backwashing is finished, the air compressor and the backwashing water pump are closed, and a normal water inlet and outlet flow is recovered.
The present invention will be described in detail below by way of examples, but the present invention is not limited to the following examples.
Examples 1 to 3
The finished oil depot sewage treatment system shown in fig. 1 is adopted to treat the finished oil depot sewage in an adjusting tank 1, an oil separation tank 2, an air flotation tank 3, an internal circulation anaerobic reactor 4, a pre-oxidation water tank 5, an MBR (membrane bioreactor) 6, an ozone catalytic oxidation tank 7 and an internal circulation BAF (bag aeration) tank 8 in sequence. Wherein, the height-diameter ratio of the internal circulation anaerobic reactor 4 is 10, and a two-stage three-phase separator is arranged in the reactor; the catalyst packing layer arranged in the pre-oxidation water tank 5 is gamma-Al loaded with cerous nitrate2O3A catalyst layer packed with spheres, the cerium nitrate content being 15% by mass, and cerium nitrate-loaded gamma-Al2O3The particle size of the ball is 3-5 mm; in the MBR (membrane bioreactor) 6, the membrane component of the MBR adopts Al2O3A flat inorganic microporous ceramic membrane as a substrate, wherein the membrane aperture is 0.2 mu m; the filler of the catalyst bed layer filled in the ozone catalytic oxidation tank 7 is gamma-Al loaded with manganese dioxide2O3Balls containing 15% by mass of manganese dioxide, and manganese dioxide-loaded gamma-Al2O3The grain diameter of the balls is 4-6mm, and in addition, ozone tail gas discharged from the top of the ozone catalytic oxidation tank 7 is dispersed into water from the bottom of the pre-oxidation water tank 5 through a pure titanium aeration disc through an induced draft unit 9 (induced draft fan); the internal circulation BAF pool 8 is of an upflow type, sewage enters from the bottom and is discharged from the upper part after passing through the packing layer, the packing layer comprises a bearing layer and a biological packing layer positioned on the upper part of the bearing layer, the bearing layer is formed by filling pebbles, the particle size of the pebbles is 4-6cm, the biological packing layer is a biological packing layer formed by filling volcanic rock particles, the particle size of the volcanic rock particles is 1.5-3.5cm, and the density is 1.8-2.2g/cm3Specific surface area 8X 104-9×104cm2The filling porosity is 55-65%, and the intra-granular porosity is 20-30%.
Specific parameters and treatment effects of example 1 are shown in table 1.
TABLE 1
Figure BDA0002446774590000131
Specific parameters and treatment effects of example 2 are shown in table 2.
TABLE 2
Figure BDA0002446774590000132
Specific parameters and treatment effects of example 3 are shown in table 2.
TABLE 3
Figure BDA0002446774590000141
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.

Claims (16)

1. The finished oil depot sewage treatment system is characterized in that a regulating tank (1), an oil separation tank (2), an air floatation tank (3), an internal circulation anaerobic reactor (4), a pre-oxidation water tank (5), an MBR membrane bioreactor (6), an ozone catalytic oxidation tank (7) and an internal circulation BAF tank (8) are sequentially arranged according to the sewage treatment flow direction.
2. The system according to claim 1, wherein the height-diameter ratio of the internal circulation anaerobic reactor (4) is more than or equal to 8, and at least two-stage three-phase separators are arranged in the reactor;
preferably, the ratio of the height to the diameter of the internal circulation anaerobic reactor 4 is 10 to 20.
3. The system according to claim 1, wherein a catalyst packing layer is arranged in the pre-oxidation water tank (5), and the catalyst packing layer is gamma-Al loaded with active ingredients2O3A catalyst layer formed by filling the balls;
preferably, the active ingredient is one or more of cerium nitrate, lanthanum nitrate, potassium nitrate and copper nitrate;
preferably, the content of the active component is 8 to 20 mass%;
preferably, gamma-Al loaded with active ingredient2O3The particle size of the ball is 3-5 mm.
4. The system according to any one of claims 1-3, wherein in the MBR (6), MBR membrane modules are used as Al membrane modules2O3Being a substrateThe pore diameter of the flat inorganic microporous ceramic membrane is 0.1-0.3 mu m.
5. The system according to any one of claims 1 to 3, wherein the ozone catalytic oxidation tank (7) is provided with water inlet at the upper part and water outlet at the bottom part, ozone enters from the bottom part of the tank, is dispersed into water through a pure titanium aeration disc and is discharged from the top of the tank;
preferably, the ozone catalytic oxidation tank (7) is filled with a catalyst bed layer;
preferably, the catalyst is gamma-Al loaded with active components2O3The active component is at least one of manganese dioxide, ferric oxide, titanium dioxide and cerium oxide;
preferably, the content of the active ingredient is 10 to 22 mass%, preferably 13 to 18 mass%;
preferably, the catalyst has a particle size of 2 to 8mm, preferably 4 to 6 mm.
6. The system according to any one of claims 1 to 3, wherein an ozone tail gas discharge outlet at the top of the ozone catalytic oxidation tank (7) is communicated with the bottom of the pre-oxidation water tank;
preferably, the ozone tail gas discharged from the top of the ozone catalytic oxidation tank (7) is dispersed into water from the bottom of the pre-oxidation water tank through a pure titanium aeration disc through an air inducing unit (9).
7. A system according to any of claims 1-3, wherein the internal circulation BAF tank (8) is of upflow type, with sewage entering from the bottom and exiting from the top after passing through a packing layer;
preferably, the filler layer comprises a supporting layer and a biological filler layer positioned on the upper part of the supporting layer;
preferably, the supporting layer is filled with pebbles, and the particle size of the pebbles is 4-6 cm;
preferably, the filler filled in the biological filler layer is at least one selected from volcanic rock particles, ceramsite, coke particles and expanded aluminosilicate particles.
8. A treatment method of finished oil depot sewage is characterized in that the finished oil depot sewage treatment system is adopted for treatment, wherein the finished oil depot sewage is treated in a regulating tank (1), an oil separation tank (2), an air flotation tank (3), an internal circulation anaerobic reactor (4), a pre-oxidation water tank (5), an MBR (membrane bioreactor) (6), an ozone catalytic oxidation tank (7) and an internal circulation BAF tank (8) in sequence according to the sewage treatment flow direction.
9. The treatment method according to claim 8, wherein the hydraulic retention time of the finished oil depot wastewater in the conditioning tank (1) is more than 20 hours, preferably 20-50 hours, more preferably 20-30 hours.
10. The treatment method according to claim 8, wherein the oil interceptor (2) is multi-staged, preferably 3 or more, more preferably 3-5;
preferably, the hydraulic retention time of each oil interceptor stage is above 9 hours, preferably 9-25 hours, more preferably 9-15 hours.
11. The treatment method according to any one of claims 8 to 10, wherein a flocculant is added to the wastewater in the flotation tank (3);
preferably, the flocculant is polyaluminium chloride and polyacrylamide;
preferably, the dosage of the polyaluminium chloride is 100-400mg/L, preferably 200-300 mg/L;
preferably, the dosage of the polyaluminium chloride is 1-8mg/L, preferably 3-5 mg/L;
preferably, the hydraulic retention time of the air floatation tank (3) is 1-5 hours, preferably 2-3 hours;
preferably, the air-water volume ratio of the air flotation tank (3) is 5-15, preferably 9-11.
12. The treatment process according to any one of claims 8 to 10, wherein the hydraulic retention time of the internal circulation anaerobic reactor (4) is 2 to 10 hours, preferably 4.5 to 7.5 hours;
preferably, the internal circulation ratio of the internal circulation anaerobic reactor (4) is 5 to 25, preferably 10 to 20.
13. The treatment process according to any one of claims 8 to 10, wherein the hydraulic retention time of the pre-oxidation basin (5) is between 0.5 and 3 hours, preferably between 1 and 1.5 hours.
14. The treatment method according to any one of claims 8-10, wherein the hydraulic retention time of the MBR membrane bioreactor (6) is 8-25 hours, preferably 10-23 hours.
15. The treatment process according to any one of claims 8 to 10, wherein the hydraulic retention time of the ozone catalytic oxidation tank (7) is comprised between 2 and 8 hours, preferably between 4 and 6 hours;
preferably, the ozone dose is 50-100gO3Pert water, preferably 40-90gO3Water per ton.
16. The treatment method according to any one of claims 8-10, wherein the hydraulic retention time of the internal circulation BAF basin (8) is 2-8 hours, preferably 4-6 hours;
preferably, the internal circulation ratio of the internal circulation BAF pool (8) is 3-15, preferably 5-9
Preferably, the gas-water volume ratio of the internal circulation BAF pool (8) is 5-25, preferably 10-20.
CN202010281581.6A 2020-04-10 2020-04-10 Finished oil depot sewage treatment system and finished oil depot sewage treatment method Pending CN113511775A (en)

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