CN115536134A - Method and device for treating oily sewage - Google Patents

Method and device for treating oily sewage Download PDF

Info

Publication number
CN115536134A
CN115536134A CN202110727797.5A CN202110727797A CN115536134A CN 115536134 A CN115536134 A CN 115536134A CN 202110727797 A CN202110727797 A CN 202110727797A CN 115536134 A CN115536134 A CN 115536134A
Authority
CN
China
Prior art keywords
concentration
aerogel
filler
sewage treatment
less
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN202110727797.5A
Other languages
Chinese (zh)
Other versions
CN115536134B (en
Inventor
王刚
高会杰
陈明翔
孙丹凤
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
Original Assignee
China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Dalian Research Institute of Petroleum and Petrochemicals filed Critical China Petroleum and Chemical Corp
Priority to CN202110727797.5A priority Critical patent/CN115536134B/en
Publication of CN115536134A publication Critical patent/CN115536134A/en
Application granted granted Critical
Publication of CN115536134B publication Critical patent/CN115536134B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • 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
    • C02F3/08—Aerobic processes using moving contact bodies
    • 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
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/104—Granular carriers
    • 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
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/105—Characterized by the chemical composition
    • 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
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/105—Characterized by the chemical composition
    • C02F3/106—Carbonaceous materials
    • 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
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/109—Characterized by the shape
    • 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
    • C02F3/282—Anaerobic digestion processes using anaerobic sequencing batch reactors
    • 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
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • 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
    • C02F2003/001—Biological treatment of water, waste water, or sewage using granular carriers or supports for the microorganisms
    • C02F2003/003—Biological treatment of water, waste water, or sewage using granular carriers or supports for the microorganisms using activated carbon or the like
    • 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
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • 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
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Abstract

The invention relates to a method for treating oily sewage, which comprises the steps of adding a filler which is activated carbon and an oil-resistant immobilized carrier according to the effective volume of a sewage treatment system not less than 50% in a starting stage, inoculating activated sludge, adding a denitrifying bacteria agent, and carrying out stewing and aeration treatment; starting water inflow, continuously operating in a mode of gradually increasing the water inflow load, finishing starting when the ammonia nitrogen concentration of the effluent of the system is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L when the system is operated at full load, and switching to an operation stage; in the operation stage, the filler is added every 6 to 12 months. The invention simultaneously adds the oil-resistant immobilized carrier and the activated carbon into the oily sewage treatment system, realizes the quick start and stable operation of the system, and has the advantages of good comprehensive treatment effect, clear effluent, good long-period operation stability and the like.

Description

Method and device for treating oily sewage
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a method and a device for treating oily sewage.
Background
In the processes of oil exploitation, refining, processing and the like, a large amount of oily sewage is generated, and oil in the sewage mostly exists in the states of floating oil, dispersed oil, emulsified oil and dissolved oil. The sewage is generally treated by adopting a combined process due to the characteristics of large discharge, complex components, large water quality fluctuation and the like. The floating oil and the dispersed oil can be removed by an oil separation flotation mode, and the dissolved oil and part of emulsified oil which is not easy to remove often enter a terminal biochemical unit along with the wastewater. In order to meet stricter emission standards, a three-stage biochemical treatment unit mainly comprising a biofilm reactor such as MBBR, BAF, FCBR and the like is additionally arranged. However, for oily sewage, the treatment by using the biofilm reactor cannot achieve ideal treatment effect after long-period operation.
In autumn moon of Yangqi (MBBR process for treating refinery sewage, china and foreign energy sources, 2020,25 (1)) a mode of properly adding nutrient salts and high-quality carbon sources at a water inlet of an MBBR pool is adopted to promote normal growth and propagation of microorganisms, so that the problem of difficult biofilm formation is solved. The Sanarmy force and the like (research on treating high-salt-content oil refining sewage by a fluidized composite carrier biomembrane process, petroleum refining and chemical industry, 2017,48 (8)) adopt a novel biomembrane biochemical treatment process (FCBR) of a patent composite carrier, wherein one carrier is attached with microorganisms for reproduction and growth to form a compact biomembrane, the treatment efficiency is improved, the other carrier is uniformly dispersed in water to fix pollutants, the impact resistance is improved, the biological treatment capacity is further enhanced by the fluidized operation of the carrier, and the treatment efficiency is improved.
At present, researchers mostly develop a great deal of work from the aspects of selection and proportioning of carrier materials, combination of carrier modification and immobilization methods and the like.
CN201210246151.6 discloses a coupling treatment method for oily sewage in an oil field, which comprises the steps of firstly carrying out two-stage biological contact oxidation treatment on the oily sewage in a biochemical pool to obtain a water body to be filtered, and then filtering the water body to be filtered; in each stage of biological contact oxidation treatment, aeration is adopted at the lower bottom of the biochemical pool, hydrophilic fiber filler with bacillus adsorbed is adopted above the aeration, oily sewage is introduced into the biochemical pool, and the volume ratio of aerated gas to the oily sewage, the pH value in the biochemical pool, the content ratio of C, N and P and the dissolved oxygen are controlled. The residual emulsified oil which is not completely removed in the front-end sewage system can be thoroughly removed, the efficiency of the biochemical treatment system is improved, and the retention time of sewage in the biochemical system is shortened to about 8 hours from the original 12 hours. However, the invention adopts the hydrophilic fibrous filler with bacillus adsorbed to remove the grease, the matching of specific thalli and materials is needed, and the filler and the thalli are only combined through the adsorption action, so the binding force needs to be further improved.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method and a device for treating oily sewage. The oil-resistant immobilized carrier and the activated carbon are added into the oily sewage treatment system at the same time, so that the system is quickly started and stably operated, and the system has the advantages of good comprehensive treatment effect, clear effluent, good long-period operation stability and the like.
The invention provides a method for treating oily sewage, which mainly comprises two stages of system starting and operation, wherein in the starting stage, a filler is added according to the effective volume of a sewage treatment system not less than 50 percent, preferably 50 to 70 percent, the filler is activated carbon and an oil-resistant immobilized carrier, then activated sludge is inoculated, and a denitrification microbial inoculum is added for braising and aeration treatment; starting water inflow, wherein the water inflow is oily nitrogen-containing sewage, and the continuous operation is carried out in a mode of gradually increasing the water inflow load; when the system runs at full load, the system finishes starting when the ammonia nitrogen concentration of the effluent is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, and then the system is switched to a running stage; in the operation stage, the filler is added every 6 to 12 months.
In the present invention, the sewage treatment system may employ biochemical treatment reactors such as A/O, SBR, BAF and the like conventionally used in the art, preferably BAF reactors.
In the present invention, the activated carbon is granular activated carbon for a sewage treatment system, which is well known in the art, and has a particle size of 50 to 100 mesh.
In the invention, the oil-resistant immobilization carrier is prepared according to the following method: (1) Placing the aerogel in an acetic acid solution for reaction, taking out the aerogel and washing the aerogel to be neutral; (2) Dissolving humic acid in Fe (OH) 3 Adding aerogel into the solution, reacting at 50-70 ℃, and washing to be alkalescent to obtain modified aerogel; (3) Loading active metal on the modified aerogel to obtain a metal-loaded carrier; (4) Adsorbing the microorganisms for producing sugar ester on the metal-loaded carrier, and drying to obtain the immobilized carrier after adsorption.
The aerogel in the step (1) is at least one of carbon aerogel, silicon aerogel, cellulose aerogel and the like, and preferably the carbon aerogel. Is usually obtained by a self-made or commercial purchase mode, and the specific surface area of the aerogel is 600-1100 m 2 The porosity is 80-98 percent.
The concentration of the acetic acid solution in the step (1) is 1.0-2.0 mol/L. Immersing the aerogel in an acetic acid solution for reaction at the temperature of 30-50 ℃ for 1.0-2.0 h. The reaction can be carried out by direct heating or water bath heating, preferably water bath heating to 30-50 ℃. The aerogel is removed and washed to neutral pH, typically 6.5 to 7.5.
Fe (OH) described in step (2) 3 The concentration of the solution is 0.5-0.8 mol/L, fe (OH) 3 The mass ratio of the solution to the humic acid is 1.
Step (2) immersing the aerogel in humic acid and Fe (OH) 3 In the mixed system of the solution, carrying out water bath oscillation reaction for 3-5 h at 50-70 ℃. After being taken out, the solution is washed until the pH value is alkalescent and is generally 7.6 to 8.0.
The active metal in the step (3) is Cu 2+ 、Fe 2+ 、Mg 2+ Etc., preferably Fe 2+ . The supported active metal can be impregnated by the impregnation method conventionally used in the art, for example, the equivalent volume and excess impregnation can be adoptedSoaking, etc. Soluble salt solutions of the active metals are generally used, with the concentration of the metal ions being from 1 to 4mol/L. For example, the modified aerogel can be immersed in an active metal solution for 6 to 10 hours at a temperature of between 60 and 70 ℃.
And (4) soaking the metal-loaded carrier in fermentation liquor of the sugar ester-producing microorganism for adsorbing and growing thalli, wherein the volume ratio of the metal-loaded carrier to the fermentation liquor is 1-3. The adsorption growth conditions are as follows: the temperature is 20-38 ℃, preferably 20-30 ℃, the pH is 6.0-8.5, preferably 6.0-7.0, and the reaction time is 12-36 h.
The microorganism producing sugar ester in the step (4) is a microorganism producing at least one sugar ester of rhamnose ester, algal glycolipid, sophorolipid and sucrose ester by fermentation, such as at least one of pseudomonas aeruginosa producing rhamnose ester, pseudomonas aeruginosa producing algal glycolipid and the like. The preparation method of the microbial fermentation broth for producing sugar ester is conventional in the art.
And (4) drying at 35-50 ℃ for 24-48 h to obtain the immobilized carrier. In the synthesized oil-resistant immobilized carrier, the metal content accounts for 1-20% of the mass of the modified aerogel, the humic acid accounts for 0.1-10% of the mass of the modified aerogel, and the sugar ester-producing microorganisms account for 5-50%, preferably 10-30% of the mass of the modified aerogel. The synthesized immobilized carrier needs to be stored in vacuum before use, and the storage time is generally 1-3 months.
In the invention, the adding volume ratio of the activated carbon to the oil-resistant immobilized carrier is 1-5.
In the invention, before adding the filler, cobblestones with different grain sizes are loaded in the reactor as a supporting layer, and the height of the supporting layer is 10-50cm.
In the invention, the activated sludge is inoculated according to the proportion of 1000-2000mg/L of the mass of the activated sludge to the total volume of the sewage treatment system. The activated sludge is taken from a secondary sedimentation tank or a biochemical unit of a sewage treatment plant.
In the invention, the denitrification microbial inoculum is inoculated according to the proportion of 0.01-0.1 percent of the volume of the denitrification microbial inoculum to the total volume of the sewage treatment system. The denitrifier is well known to those skilled in the art, and can be a combination of single strains with the functions of deamination and total nitrogen removal.
In the invention, after the filler, the activated sludge and the denitriding agent are added, the mixture is stewed and exposed for 5-10 days under the conditions of dissolved oxygen of 2-6mg/L and pH of 7-9.
In the invention, the water quality of the oily nitrogen-containing sewage is as follows: the concentration of petroleum is 15-25mg/L, the concentration of ammonia nitrogen is 50-100mg/L, the total nitrogen is 60-120mg/L, the concentration of COD is 300-400mg/L, and the concentration of suspended matters is 20-50mg/L.
In the invention, the continuous operation is started according to 50% of the water inlet load, and the continuous operation is carried out by gradually increasing the water inlet load until the water outlet reaches the standard, wherein the increasing range is 5% -15% each time until the water inlet load reaches 100%.
In the invention, the operation conditions of the sewage treatment system in the starting stage and the operation stage are as follows: the dissolved oxygen is more than 2mg/L, the pH value is 7.5-8.5, and the temperature is 25-40 ℃.
In the invention, the filler is supplemented every 6-12 months in the operation process, and the supplement amount is that the total amount of the filler accounts for not less than 50%, preferably 50-70% of the effective volume of the sewage treatment system after the supplement.
In the invention, backwashing is carried out every 2-4 months in the operation stage.
The invention also provides a treatment device for the oily sewage treatment method, which mainly comprises a sewage treatment system and a monitoring system, wherein the sewage treatment system is filled with activated carbon and oil-resistant immobilized carriers and is simultaneously inoculated with activated sludge and a denitrification microbial inoculum for sewage treatment; the monitoring system is used for monitoring the system effluent, when the system effluent is in full-load operation, the system effluent ammonia nitrogen concentration is less than 1mg/L, the TN concentration is less than 15mg/L, and the COD concentration is less than 30mg/L, the system effluent ammonia nitrogen concentration is started, and the system effluent is switched to an operation stage.
In the present invention, the sewage treatment system may employ biochemical treatment reactors such as A/O, SBR, BAF and the like conventionally used in the art, preferably BAF reactors.
Compared with the prior art, the invention has the following beneficial effects:
(1) The oil-resistant immobilized carrier and the activated carbon are simultaneously added into the oily sewage treatment system, and the activated sludge and the denitrification microbial inoculum are added in a combined manner, so that the system is quickly started and stably operated under the synergistic action of the oil-resistant immobilized carrier, the activated sludge and the denitrification microbial inoculum, and the system has the advantages of good comprehensive treatment effect, clear effluent, good long-period operation stability and the like.
(2) The oil-resistant immobilized carrier has good oil resistance, can keep the pore structure suitable for the filler after being combined with the active carbon according to a certain proportion, can keep the long-acting property of the filler when being used in the oily sewage treatment process, avoids the blockage and pollution of oil substances on the pore of the carrier, and prolongs the backwashing time.
(3) The used oil-resistant immobilized carrier has a pore structure suitable for adsorption and propagation of functional microorganisms in a treatment system, is beneficial to the initial adhesion of denitrifying microorganisms on the surface of the filler, can ensure the adsorption capacity of decarbonizing and denitrifying microorganisms, and realizes the advanced treatment of oily sewage. The carrier has strong bonding force of each component, the active metal is not easy to lose, and the long-term operation stability is good.
Detailed Description
The method and effects of the present invention will be described in further detail by examples. The embodiments are implemented on the premise of the technical scheme of the invention, and detailed implementation modes and specific operation processes are given, but the protection scope of the invention is not limited by the following embodiments.
The experimental procedures in the following examples are, unless otherwise specified, those conventional in the art. The experimental materials used in the following examples were purchased from a conventional biochemical reagent store unless otherwise specified.
In the embodiment of the invention, the COD concentration is determined by GB11914-89 bichromate method which is used for determining water quality and chemical oxygen demand; the ammonia nitrogen concentration is measured by GB7478-87 method for measuring ammonium water quality by distillation and titration; the total nitrogen concentration is measured by GB11894-89 determination of water quality-total nitrogen-ultraviolet spectrophotometry; the petroleum is measured by HJ970-2018, determination of water quality and petroleum, ultraviolet spectrophotometry; metal ions are measured by adopting an inductively coupled plasma mass spectrometry; the effluent suspended matter is measured by GB11901-89 weight method for measuring water suspended matter.
Example 1
The preparation method of the oil-resistant immobilized carrier adopted by the invention comprises the following steps:
(1) Mixing carbon aerogel (specific surface area is 800 m) 2 And the porosity is 80%) is immersed in 1.5mol/L acetic acid solution for water bath reaction, the reaction temperature is 40 ℃, oscillation is carried out for 1.5h, and the carbon aerogel after being taken out is washed by deionized water to pH7.0, so as to obtain the pretreated carbon aerogel.
(2) According to Fe (OH) 3 Solution to humic acid mass ratio of 2 3 And adding the pretreated carbon aerogel into the solution, oscillating in a water bath at 60 ℃ for 4 hours, taking out, and washing with deionized water to pH8.0 to obtain the modified aerogel.
(3) Preparing a ferrous sulfate solution with iron ion concentration of 1mol/L, adding the modified aerogel, and soaking for 8 hours at 65 ℃ under the stirring condition to obtain the carrier loaded with the active metal.
(4) Mixing a carrier loaded with active metal with a fermentation liquor of pseudomonas aeruginosa for producing rhamnosyl ester, wherein the volume ratio of the carrier to the fermentation liquor is 1. Adsorbing and growing for 12h under the conditions of the temperature of 30 ℃ and the pH value of 6.5 to obtain the carrier for adsorbing the pseudomonas aeruginosa. And taking out the carrier adsorbing the microorganisms, and drying the carrier at 45 ℃ for 24 hours to finally obtain the immobilized carrier.
The rhamnose ester-producing Pseudomonas aeruginosa used in this example was obtained according to the method provided in the literature, "screening of biosurfactant-producing bacteria" (Panglacial, journal of microbiology, 6 months 1996, 39 (3)). The strain which has stable genetic character and produces rhamnose ester is obtained by enrichment culture and screening by using a blood plate and shaking flask fermentation and re-screening, and the strain is identified as pseudomonas aeruginosa by 16SrRNA and the like.
The preparation method of the pseudomonas aeruginosa fermentation liquor comprises the following steps: and selecting the bacterial colony on the inclined plane to inoculate on an LB culture medium, culturing for 24h at 37 ℃ and 200rpm to obtain a seed solution, then inoculating the seed solution on a fermentation culture medium according to 5 percent, and culturing for 7 days at 35 ℃ and 200rpm to obtain a fermentation liquid. The fermentation medium comprises the following components in percentage by mass: glucose 5.0%, yeast extract 0.5%、KH 2 PO 4 、MgSO 4 、FeSO 4 ·7H 2 O and CaCl 2H 2 O is 0.02 percent.
The sewage treatment system adopts a BAF reactor, firstly cobbles with different grain sizes are loaded in the reactor as a bearing layer, and the height of the bearing layer is 15cm.
In the starting stage, adding filler which is active carbon (100 meshes) and the oil-resistant immobilized carrier prepared by the method according to the effective volume of the sewage treatment system of 60 percent, wherein the volume ratio of the active carbon to the oil-resistant immobilized carrier is 1 ＃ ) And stewing and exposing for 5 days.
Starting water inflow, wherein the concentration of petroleum in the inflow water is 20mg/L, the concentration of ammonia nitrogen is 80mg/L, the total nitrogen is 100mg/L, the concentration of COD is 350mg/L, and the concentration of suspended matters is 25mg/L.
The operating conditions of the sewage treatment system are as follows: dissolved oxygen was 3mg/L, pH 7.8, temperature 30 ℃.
Firstly, the operation is continuously carried out according to the water inlet load of 50 percent, and after the operation is carried out until the water outlet reaches the standard, the operation is continuously carried out by gradually increasing the water inlet load, wherein the increasing range is 10 percent each time until the water inlet load reaches 100 percent. When the system runs at full load, the ammonia nitrogen concentration of the effluent of the system is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, the startup is completed, and the running stage is switched to; in the operation stage, the filler is added every 8 months, the composition of the filler is unchanged, and the added amount is 60 percent of the total amount of the filler accounting for the effective volume of the sewage treatment system after the filler is added. And performing backwashing every 3 months.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.6mg/L, the average total nitrogen concentration is 12.3mg/L, and the average COD concentration is 23.5mg/L.
Example 2
The preparation method of the oil-resistant immobilized carrier adopted by the invention comprises the following steps:
(1) Mixing carbon aerogels (Bibiao table)Area of 800m 2 And the porosity is 80%) is immersed in 1mol/L acetic acid solution for water bath reaction, the reaction temperature is 30 ℃, the oscillation is carried out for 1h, the carbon aerogel is taken out and washed by deionized water until the pH value is 6.5, and the pretreated carbon aerogel is obtained.
(2) According to Fe (OH) 3 Solution to humic acid mass ratio of 1 3 And adding the pretreated carbon aerogel into the solution, oscillating the solution in a water bath at 50 ℃ for 3 hours, taking out the solution, and washing the solution with deionized water until the pH value is 7.6 to obtain the modified aerogel.
(3) Preparing a ferrous sulfate solution with the iron ion concentration of 2mol/L, adding the modified aerogel into the solution, and soaking for 6 hours at the temperature of 60 ℃ under the stirring condition to obtain the loaded metal carrier.
(4) Mixing the metal-loaded carrier with the fermentation liquor of pseudomonas aeruginosa for producing the algal glycolipid, wherein the volume ratio of the carrier to the fermentation liquor is 1. Adsorbing and growing for 24h under the conditions of 25 ℃ and pH7.0 to obtain the carrier for adsorbing the microorganisms. Taking out the carrier adsorbing the microorganisms, and drying the carrier at 35 ℃ for 48 hours to finally obtain the immobilized carrier.
Pseudomonas aeruginosa producing trehalose esters used in this example was obtained according to the method described in "screening of biosurfactant-producing bacteria" (Panagram, report on microbiology, 1996, 6.39 (3)). The strain which has stable genetic character and produces trehalose ester is obtained by enrichment culture and screening by using a blood plate, and the strain is identified as pseudomonas aeruginosa by 16SrRNA and the like.
The preparation method of the pseudomonas aeruginosa fermentation liquor comprises the following steps: and selecting the bacterial colony on the inclined plane to inoculate on an LB culture medium, culturing for 24h at 37 ℃ and 200rpm to obtain a seed solution, then inoculating the seed solution on a fermentation culture medium according to 5 percent, and culturing for 7 days at 37 ℃ and 200rpm to obtain a fermentation liquid. The fermentation medium comprises the following components in percentage by mass: 2.0% of glucose, 0.5% of yeast extract, 1.0% of peptone and KH 2 PO 4 、MgSO 4 、FeSO 4 ·7H 2 O and CaCl.2H 2 O is 0.02 percent.
The sewage treatment system adopts a BAF reactor, firstly cobbles with different grain sizes are loaded in the reactor as a bearing layer, and the height of the bearing layer is 35cm.
In the starting stage, adding filler which is activated carbon (100 meshes) and the oil-resistant immobilized carrier prepared by the method according to the effective volume of the sewage treatment system of 60 percent, wherein the volume ratio of the activated carbon to the oil-resistant immobilized carrier is 1 ＃ ) And carrying out soaking and exposure treatment for 5 days.
Starting water inflow, wherein the concentration of petroleum in the inflow water is 20mg/L, the concentration of ammonia nitrogen is 80mg/L, the total nitrogen is 100mg/L, the concentration of COD is 350mg/L, and the concentration of suspended matters is 25mg/L.
The operating conditions of the sewage treatment system are as follows: dissolved oxygen was 3mg/L, pH 7.8, temperature 30 ℃.
Firstly, the operation is continuously carried out according to the water inlet load of 50 percent, and after the operation is carried out until the water outlet reaches the standard, the operation is continuously carried out by gradually increasing the water inlet load, wherein the increasing range is 10 percent each time until the water inlet load reaches 100 percent. When the system runs at full load, the ammonia nitrogen concentration of the effluent of the system is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, the startup is completed, and the running stage is switched to; in the operation stage, the filler is added every 8 months, the composition of the filler is unchanged, and the added amount is 60 percent of the total amount of the filler accounting for the effective volume of the sewage treatment system after the filler is added. And performing backwashing every 3 months.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.8mg/L, the average total nitrogen concentration is 13.6mg/L, and the average COD concentration is 28mg/L.
Example 3
The oil-resistant immobilized carrier was prepared in the same manner as in example 1.
The sewage treatment system adopts a BAF reactor, firstly cobbles with different grain sizes are loaded in the reactor as a bearing layer, and the height of the bearing layer is 15cm.
In the starting stage, filler is added according to 50 percent of the effective volume of the sewage treatment system, and the filler is activated carbon (50 percent)Mesh) and the oil-resistant immobilized carrier prepared in example 1, the volume ratio of the two is 1 ＃ ) And carrying out soaking and exposure treatment for 10 days.
And starting water inflow, wherein the concentration of petroleum in the inflow water is 15mg/L, the concentration of ammonia nitrogen is 50mg/L, the total nitrogen is 60mg/L, the concentration of COD is 300mg/L, and the concentration of suspended matters is 20mg/L.
The operating conditions of the sewage treatment system are as follows: dissolved oxygen was 3.5mg/L, pH8.0, temperature 28 ℃.
Firstly, continuously operating according to 50% of water inlet load, and after the operation reaches the effluent standard, continuously operating by adopting a mode of gradually increasing the water inlet load, wherein the increasing amplitude of each time is 15% until the water inlet load reaches 100%. When the system runs at full load, the ammonia nitrogen concentration of the effluent of the system is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, the startup is completed, and the running stage is switched to; in the operation stage, the filler is added every 6 months, the composition of the filler is unchanged, and the added amount is 50 percent of the total amount of the filler accounting for the effective volume of the sewage treatment system after the filler is added. And performing backwashing every 2 months.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.91mg/L, the average total nitrogen concentration is 14.1mg/L, and the average COD concentration is 27.1mg/L.
Example 4
The oil-resistant immobilization carrier was prepared in the same manner as in example 1.
The sewage treatment system adopts a BAF reactor, firstly cobbles with different grain sizes are loaded in the reactor as a bearing layer, and the height of the bearing layer is 50cm.
In the starting stage, filler is added according to 70% of the effective volume of the sewage treatment system, the filler is activated carbon (80 meshes) and the oil-resistant immobilized carrier prepared in the example 1, the volume ratio of the activated carbon to the oil-resistant immobilized carrier is 1The denitrification microbial inoculum (adopting CN2016110729248, microbial inoculum 1 prepared in example 1) is inoculated at the total volume ratio of 0.01% ＃ ) And carrying out stewing and exposure treatment for 7 days.
And starting water inflow, wherein the concentration of petroleum in the inflow water is 25mg/L, the concentration of ammonia nitrogen is 100mg/L, the total nitrogen is 120mg/L, the concentration of COD is 400mg/L, and the concentration of suspended matters is 50mg/L.
The operating conditions of the sewage treatment system are as follows: dissolved oxygen was 4mg/L, pH 7.5, temperature 30 ℃.
Firstly, the continuous operation is carried out according to the water inlet load of 50 percent, and after the operation is carried out until the water outlet reaches the standard, the continuous operation is carried out by gradually increasing the water inlet load, wherein the increasing range is 5 percent each time until the water inlet load reaches 100 percent. When the system runs at full load, the ammonia nitrogen concentration of the effluent of the system is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, the startup is completed, and the running stage is switched to; in the operation stage, the filler is added every 12 months, the composition of the filler is unchanged, and the added amount is 70 percent of the total amount of the filler accounting for the effective volume of the sewage treatment system after the filler is added. The back washing is carried out every 4 months.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.89mg/L, the average total nitrogen concentration is 14.4mg/L, and the average COD concentration is 27.8mg/L.
Example 5
The same as example 1, except that: in the preparation method of the oil-resistant immobilized carrier, silicon aerogel is adopted to replace carbon aerogel, and the specific surface area of the silicon aerogel is 1000m 2 And the porosity is 85 percent, and finally the oil-resistant immobilized carrier is prepared.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.98mg/L, the average total nitrogen concentration is 14.7mg/L, and the average COD concentration is 28.5mg/L.
Example 6
The difference from example 1 is that: in the preparation method of the oil-resistant immobilization carrier, cellulose aerogel is adopted to replace carbon aerogel, and the specific surface area of the cellulose aerogel is 900m 2 The porosity is 95 percent, and finally the immobilized carrier is prepared.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.96mg/L, the average total nitrogen concentration is 13.3mg/L, and the average COD concentration is 28.1mg/L.
Example 7
The difference from example 1 is that: in the preparation method of the oil-resistant immobilized carrier, cu is adopted as metal ions 2+ And preparing a copper chloride solution of 3mol/L instead of a ferric sulfate solution to finally prepare the immobilized carrier.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.95mg/L, the average total nitrogen concentration is 13.6mg/L, and the average COD concentration is 28.7mg/L.
Example 8
The difference from example 1 is that: in the preparation method of the oil-resistant immobilized carrier, the metal ions are Mg 2+ A4 mol/L magnesium sulfate solution is prepared to replace a ferric sulfate solution. Finally, the immobilized carrier is prepared.
After the operation for one year, the treatment effect of the system is stable, the average ammonia nitrogen concentration of the effluent is 0.98mg/L, the average total nitrogen concentration is 14.3mg/L, and the average COD concentration is 29.3mg/L.
Comparative example 1
The same as example 1, except that: the sewage treatment system does not adopt the oil-resistant immobilized carrier prepared by the method, and only adopts granular activated carbon. After the operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 16.9mg/L, the average total nitrogen concentration is 29.7mg/L and the average COD concentration is 39.3mg/L due to the influence of petroleum substances.
Comparative example 2
The difference from example 1 is that: the sewage treatment system does not adopt active carbon, and only adopts the immobilized carrier prepared by the method. After the operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 10.6mg/L, the average total nitrogen concentration is 20.9mg/L and the average COD concentration is 35.5mg/L because the proper pore channel structure of the filler cannot be maintained.
Comparative example 3
The difference from example 1 is that: in the BAF reactor, volcanic rock filler is used to replace the combined filler of active carbon and immobilized carrier. After the operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 23.4mg/L, the average total nitrogen concentration is 29.8mg/L and the average COD concentration is 45.5mg/L.
Comparative example 4
The same as example 1, except that: only activated sludge is inoculated in the sewage treatment system, and a denitrification microbial inoculum is not inoculated. After the operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 11.7mg/L, the average total nitrogen concentration is 23.5mg/L, and the average COD concentration is 37.6mg/L.
Comparative example 5
The difference from example 1 is that: in the preparation process of the immobilized carrier, the modified aerogel obtained in the step (3) is not loaded with metal ions, and finally the immobilized carrier is prepared. After the operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 12.3mg/L, the average total nitrogen concentration is 24.7mg/L, and the average COD concentration is 36.9mg/L.
Comparative example 6
The difference from example 1 is that: in the preparation process of the immobilized carrier, rhamnolipid is adopted to replace pseudomonas aeruginosa fermentation liquor producing rhamnolipid in the step (4), and the immobilized carrier is finally prepared. After operation for one year, the average ammonia nitrogen concentration of the effluent of the system is 14.3mg/L, the average total nitrogen concentration is 28.8mg/L, the average suspended matter concentration is 67mg/L, and the average COD concentration is 46.3mg/L.

Claims (28)

1. A method for treating oily sewage is characterized by mainly comprising two stages of starting and running, wherein in the starting stage, a filler is added according to the effective volume of a sewage treatment system which is not less than 50 percent, the filler is activated carbon and an oil-resistant immobilized carrier, then activated sludge is inoculated, a denitrification agent is added, and braising and aeration treatment is carried out; starting water inflow, wherein the water inflow is oily nitrogen-containing sewage, and the continuous operation is carried out in a mode of gradually increasing the water inflow load; when the system runs at full load, the system finishes starting when the ammonia nitrogen concentration of the effluent is less than 1mg/L, the TN concentration is less than 15mg/L and the COD concentration is less than 30mg/L, and then the system is switched to a running stage; in the operation stage, the filler is added every 6 to 12 months.
2. The method of claim 1, wherein: the filler is added according to the effective volume of 50-70% of the sewage treatment system.
3. The method of claim 1, wherein: the sewage treatment system adopts A/O, SBR and BAF biochemical treatment reactors, preferably BAF reactors.
4. The method of claim 1, wherein: the activated carbon is granular activated carbon with the grain size of 50-100 meshes.
5. The method of claim 1, wherein: the oil-resistant immobilization carrier is prepared by the following method: (1) Placing the aerogel in an acetic acid solution for reaction, taking out the aerogel and washing the aerogel to be neutral; (2) Dissolving humic acid in Fe (OH) 3 Adding aerogel into the solution, reacting at 50-70 ℃, and washing to be alkalescent to obtain modified aerogel; (3) Loading active metal on the modified aerogel to obtain a metal-loaded carrier; (4) Adsorbing the microorganism producing sugar ester on the carrier loaded with metal, and drying after adsorption to obtain the immobilized carrier.
6. The method of claim 5, wherein: the aerogel in the step (1) is at least one of carbon aerogel, silicon aerogel and cellulose aerogel, and preferably the carbon aerogel.
7. The method according to claim 5 or 6, characterized in that: the specific surface area of the aerogel is 600-1100 m 2 The porosity is 80-98 percent.
8. The method of claim 5, wherein: the concentration of the acetic acid solution in the step (1) is 1.0-2.0 mol/L; immersing the aerogel in an acetic acid solution for reaction at the temperature of between 30 and 50 ℃ for 1.0 to 2.0 hours.
9. The method of claim 5, wherein: step (2) said Fe (OH) 3 The concentration of the solution is 0.5-0.8 mol/L, fe (OH) 3 The mass ratio of the solution to the humic acid is 1.
10. The method of claim 5, wherein: step (2) immersing the aerogel in humic acid and Fe (OH) 3 In a mixed system of the solution, carrying out water bath oscillation reaction for 3-5 h at 50-70 ℃; after being taken out, the mixture is washed until the pH value is alkalescent, generally between 7.6 and 8.0.
11. The method of claim 5, wherein: the active metal in the step (3) is Cu 2+ 、Fe 2+ 、Mg 2+ Preferably Fe 2+ 。
12. The method according to claim 5 or 11, characterized in that: and (3) soaking the substrate for 6 to 10 hours at the temperature of between 60 and 70 ℃ by adopting a soluble salt solution of active metal, wherein the concentration of metal ions is 1 to 4 mol/.
13. The method of claim 5, wherein: and (4) soaking the metal-loaded carrier in fermentation liquor of the sugar ester-producing microorganism for adsorbing and growing thalli, wherein the volume ratio of the metal-loaded carrier to the fermentation liquor is 1-3.
14. The method according to claim 5 or 13, characterized in that: the adsorption growth conditions in the step (4) are as follows: the temperature is 20-38 ℃, preferably 20-30 ℃, the pH is 6.0-8.5, preferably 6.0-7.0, and the reaction time is 12-36 h.
15. The method of claim 5, wherein: the microorganism producing the sugar ester in the step (4) is a microorganism producing at least one sugar ester of rhamnose ester, algal glycolipid, sophorolipid and sucrose ester by fermentation, preferably at least one of pseudomonas aeruginosa producing the rhamnose ester and pseudomonas aeruginosa producing the algal glycolipid.
16. The method of claim 5, wherein: the drying in the step (4) is drying for 24-48 h at 35-50 ℃ to obtain the immobilized carrier.
17. The method of claim 5, wherein: in the synthesized oil-resistant immobilized carrier, the metal content accounts for 1-20% of the mass of the modified aerogel, the humic acid accounts for 0.1-10% of the mass of the modified aerogel, and the sugar ester-producing microorganisms account for 5-50%, preferably 10-30% of the mass of the modified aerogel.
18. The method of claim 1, wherein: the adding volume ratio of the activated carbon to the oil-resistant immobilized carrier is 1-5.
19. The method of claim 1, wherein: before adding the filler, firstly, loading cobbles with different grain sizes in the reactor as a bearing layer, wherein the height of the bearing layer is 10-50cm.
20. The method of claim 1, wherein: inoculating the activated sludge according to the ratio of the mass of the activated sludge to the total volume of the sewage treatment system of 1000-2000 mg/L.
21. The method of claim 1, wherein: inoculating the denitrifying bacteria agent according to the proportion of 0.01-0.1% of the volume of the denitrifying bacteria agent to the total volume of the sewage treatment system.
22. The method of claim 1, wherein: after the filler, the activated sludge and the denitriding agent are added, the mixture is stewed and exposed for 5 to 10 days under the conditions of dissolved oxygen of 2 to 6mg/L and pH of 7 to 9.
23. The method of claim 1, wherein: the water quality of the oily nitrogen-containing sewage is as follows: the concentration of petroleum is 15-25mg/L, the concentration of ammonia nitrogen is 50-100mg/L, the total nitrogen is 60-120mg/L, the concentration of COD is 300-400mg/L, and the concentration of suspended matters is 20-50mg/L.
24. The method of claim 1, wherein: the continuous operation is started according to the water inlet load of 50 percent, and the continuous operation is carried out in a mode of gradually increasing the water inlet load after the water outlet reaches the standard, wherein the increasing range is 5 to 15 percent each time until the water inlet load reaches 100 percent.
25. The method of claim 1, wherein: the starting stage and the running stage, the running conditions of the sewage treatment system are as follows: the dissolved oxygen is more than 2mg/L, the pH value is 7.5-8.5, and the temperature is 25-40 ℃.
26. The method of claim 1, wherein: in the operation process, the filler is supplemented every 6-12 months, and the supplement amount is that the total amount of the filler accounts for not less than 50 percent, preferably 50-70 percent of the effective volume of the sewage treatment system after the supplement.
27. The method of claim 1, wherein: and in the operation stage, backwashing is performed every 2-4 months.
28. A treatment device for the oily sewage treatment method of any one of claims 1 to 27, which mainly comprises a sewage treatment system and a monitoring system, wherein the sewage treatment system is filled with activated carbon and oil-resistant immobilized carriers and is simultaneously inoculated with activated sludge and denitrification microbial inoculum for sewage treatment; the monitoring system is used for monitoring the system effluent, when the system effluent is in full-load operation, the system effluent ammonia nitrogen concentration is less than 1mg/L, the TN concentration is less than 15mg/L, and the COD concentration is less than 30mg/L, the system effluent ammonia nitrogen concentration is started, and the system effluent is switched to an operation stage.
CN202110727797.5A 2021-06-29 2021-06-29 Treatment method and device for oily sewage Active CN115536134B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202110727797.5A CN115536134B (en) 2021-06-29 2021-06-29 Treatment method and device for oily sewage

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202110727797.5A CN115536134B (en) 2021-06-29 2021-06-29 Treatment method and device for oily sewage

Publications (2)

Publication Number Publication Date
CN115536134A true CN115536134A (en) 2022-12-30
CN115536134B CN115536134B (en) 2024-04-05

Family

ID=84705560

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202110727797.5A Active CN115536134B (en) 2021-06-29 2021-06-29 Treatment method and device for oily sewage

Country Status (1)

Country Link
CN (1) CN115536134B (en)

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1565990A (en) * 2003-06-25 2005-01-19 中国石油化工股份有限公司 Biochemical treatment process for recovered waste water in oil field
CN101508509A (en) * 2009-03-24 2009-08-19 同济大学 Interactive treating process for advance treatment and recycle of waster water from oil production
CN101973641A (en) * 2010-10-09 2011-02-16 江苏博大环保股份有限公司 Hyposmosis/super-hyposmosis oil extraction sewage reinjection method in oil field
CN103482765A (en) * 2013-09-22 2014-01-01 北京工业大学 Quick starting method for technology for simultaneous denitrification and COD removal under condition of normal-temperature and low-C/N sewage
CN105417706A (en) * 2015-12-30 2016-03-23 哈尔滨工业大学 Method for treating oil field polymer-containing sewage through A/O process based on anaerobic suspended filler
JP2016047490A (en) * 2014-08-27 2016-04-07 水ｉｎｇ株式会社 Oil- and fat-containing wastewater treatment method and apparatus
CN105800784A (en) * 2016-03-28 2016-07-27 哈尔滨工业大学 Improved UCT step-feed efficient biological denitrification and dephosphorization device based on DEAMOX technology and application method
KR20170060305A (en) * 2015-11-24 2017-06-01 한국과학기술연구원 Fluidizable carrier with attached anaerobic digestion microorganisms and method for fabricating the same
CN107902765A (en) * 2017-11-28 2018-04-13 王金龙 A kind of multistage partial nitrification starts and control method
CN108046433A (en) * 2018-01-25 2018-05-18 哈尔滨工业大学 A kind of floating stuffing colonization method of Anaerobic wastewater treatment
CN109574258A (en) * 2019-01-21 2019-04-05 南京大学 A method of realizing denitrification bio-filter quick start

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1565990A (en) * 2003-06-25 2005-01-19 中国石油化工股份有限公司 Biochemical treatment process for recovered waste water in oil field
CN101508509A (en) * 2009-03-24 2009-08-19 同济大学 Interactive treating process for advance treatment and recycle of waster water from oil production
CN101973641A (en) * 2010-10-09 2011-02-16 江苏博大环保股份有限公司 Hyposmosis/super-hyposmosis oil extraction sewage reinjection method in oil field
CN103482765A (en) * 2013-09-22 2014-01-01 北京工业大学 Quick starting method for technology for simultaneous denitrification and COD removal under condition of normal-temperature and low-C/N sewage
JP2016047490A (en) * 2014-08-27 2016-04-07 水ｉｎｇ株式会社 Oil- and fat-containing wastewater treatment method and apparatus
KR20170060305A (en) * 2015-11-24 2017-06-01 한국과학기술연구원 Fluidizable carrier with attached anaerobic digestion microorganisms and method for fabricating the same
CN105417706A (en) * 2015-12-30 2016-03-23 哈尔滨工业大学 Method for treating oil field polymer-containing sewage through A/O process based on anaerobic suspended filler
CN105800784A (en) * 2016-03-28 2016-07-27 哈尔滨工业大学 Improved UCT step-feed efficient biological denitrification and dephosphorization device based on DEAMOX technology and application method
CN107902765A (en) * 2017-11-28 2018-04-13 王金龙 A kind of multistage partial nitrification starts and control method
CN108046433A (en) * 2018-01-25 2018-05-18 哈尔滨工业大学 A kind of floating stuffing colonization method of Anaerobic wastewater treatment
CN109574258A (en) * 2019-01-21 2019-04-05 南京大学 A method of realizing denitrification bio-filter quick start

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
李南臻等: "产鼠李糖脂铜绿假单胞菌的选育 及其发酵条件的优化研究", 《食品与发酵科技》, vol. 54, no. 1, 31 January 2018 (2018-01-31) *
蔡晓鸣: "曝气生物滤池处理含油废水的研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》, no. 11, 15 November 2008 (2008-11-15), pages 027 - 262 *
陈碧美: "《污水处理系统运行与管理》", 31 July 2015, 厦门大学出版社, pages: 61 - 63 *

Also Published As

Publication number Publication date
CN115536134B (en) 2024-04-05

Similar Documents

Publication Publication Date Title
Tan et al. Enhanced simultaneous organics and nutrients removal in tidal flow constructed wetland using activated alumina as substrate treating domestic wastewater
Zhang et al. Efficient nitrate removal by Pseudomonas mendocina GL6 immobilized on biochar
Schwarzenbeck et al. Aerobic granular sludge in an SBR-system treating wastewater rich in particulate matter
Yan et al. Partial nitrification to nitrite for treating ammonium-rich organic wastewater by immobilized biomass system
CN111470714B (en) Environment-friendly recycling method for aquaculture wastewater
AU2010327173A1 (en) Wastewater pretreatment method and sewage treatment method using the pretreatment method
CN108117221B (en) Treatment method of reverse osmosis concentrated water
Bianco et al. Phenanthrene biodegradation in a fed–batch reactor treating a spent sediment washing solution: Techno–economic implications for the recovery of ethanol as extracting agent
CN113562846A (en) Denitrification efficient carbon source and processing technology thereof
Ren et al. Study on performance and mechanism of enhanced low-concentration ammonia nitrogen removal from low-temperature wastewater by iron-loaded biological activated carbon filter
JP2004524967A (en) Biochemical treatment of wastewater using nanomaterials
Wang et al. Biochar immobilized petroleum degrading consortium for enhanced granulation and treatment of synthetic oil refinery wastewater
CN115536134A (en) Method and device for treating oily sewage
CN101306904B (en) Integration denitrification and dephosphorization method of iron inner electrolysis and bio-coupling
US11180390B2 (en) Method for treating and recycling waste slurry in bobbin paper production
CN115140846A (en) Composite treating agent, preparation method and application thereof in wastewater purification
CN115537412A (en) Oil-resistant immobilized carrier and synthesis method and application thereof
CN115108629B (en) Advanced sewage treatment method and system
CN117003397A (en) Advanced standard treatment method for sewage containing refractory substances
CN111117938A (en) Compound microbial agent, preparation method thereof and treatment method of high-salt nitrogen-containing wastewater
CN114684916B (en) Sewage denitrification and dephosphorization method
CN114684924B (en) Denitrification treatment method for salt-containing wastewater
CN114394673B (en) Biological fermentation pretreatment method for high-concentration organic wastewater and application thereof
CN117003395A (en) Method for quickly recovering biochemical unit after high-load impact on sewage treatment plant
CN113830904B (en) Technology for treating aged garbage leachate by combining iron-oxidizing microorganisms with activated carbon

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
TA01 Transfer of patent application right

Effective date of registration: 20240112

Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Applicant after: CHINA PETROLEUM & CHEMICAL Corp.

Applicant after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd.

Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Applicant before: CHINA PETROLEUM & CHEMICAL Corp.

Applicant before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp.

TA01 Transfer of patent application right
GR01 Patent grant
GR01 Patent grant