CN104529059A - Biological treatment method for phenol-containing oil-refining wastewater - Google Patents
Biological treatment method for phenol-containing oil-refining wastewater Download PDFInfo
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Abstract
The invention provides a biological treatment method for phenol-containing oil-refining wastewater. An independently designed aerated biological fluidized tank (ABFT) is adopted for carrying out biological pretreatment on phenol-containing wastewater treated by a stripping device of an oil refinery, active sludge is selectively added, biofilm culturing is performed sequentially by using intermittent and continuous water feeding approaches, a test apparatus is started, and the hydraulic retention time, gas water ratio, temperature and pH value of the fluidized bed in the stage of stable running are adjusted so as to enhance the removal efficiency of phenol. Results show that when the hydraulic retention time is 10 h, the gas water ratio (volume) is 20:1, the temperature is 30-37 DEG C, and the pH value is 6.5-9, the removal effect of phenol is optimal, and reaches over 90%; and the removal of phenol is mainly implemented in a primary reaction pool, and a secondary reaction pool can achieve a buffer effect when the water quality is deteriorated so as to ensure that phenol in microorganisms is efficiently remove and the stable quality of treated effluent water is obtained.
Description
Technical field
The present invention relates to phenol-containing wastewater process field, particularly one oil refining phenol-containing wastewater bioremediation.
Background technology
Phenolic wastewater source is wide, harm is large, it is the representational class of most in industrial organic waste water, phenolic compound is a kind of protoplasma poisonous substance [PEYTON B M, WILSONA T, YONGE D R.Kinetics of phenol biodegradation in high salt solutions] .Water Res, 2002, 36:4811-4820], there is extremely strong bio-toxicity, one of the harmful waste water needing emphasis to solve in industrial application [Zhang Wei, Wei Chaohai, Peng Pingan, Deng phenols composition and degradation characteristic analysis in .A/O/O biological fluidized bed Treatment of Wastewater in Coking]. environmental engineering journal, 2010, 4 (2): 253-258].The treatment technology of current phenolic wastewater comprises [the BUSCA G such as absorption method, solvent extration, membrane separation process, high-level oxidation technology and biological treatment, BERARDINELLI S, RESINI C, et al.Technologies for the removal of phenol from fluid streams:a short review of recent developments] .J Hazard Materi, 2008,160:265-288].Wherein, biologic treating technique due to low, the green non-secondary pollution of working cost, to fall phenol rate high and be widely used in the process of lower concentration phenolic wastewater.
Aerated biological fludized bed (Aerated Biological Fluidized Tank, ABFT) be by Chemical Engineering Technology, the one that biotechnology and water technology organically combine and formed is based on biomembrance process, activated sludge process is auxiliary novel biochemical treatment process [Rabah F K J, Dahab M F. Biofilm and biomass characteristics in high performance fluidized bed biofilm reactors] .Water Research, 2004, 38 (19): 4262-4270], in U.S., the countries such as day are nitrated for sewage, the process of denitrogenation even depth and coal, weaving, process [the JOU C G of the trade effluents such as pharmacy, HUANG G C.A pilot study for oil refinery wastewater treatment using a fixed film bioreactor [J] .Advances in Environmental Research, 2003, 7:463-469], there is technique simple, efficiency is high, take up an area few, reduced investment, the advantages such as anti impulsion load [Ye Zhengfang, Li Yanfeng, Li Xianzhen, Deng. the research of aeration and biological fluidisation (ABFB) gas treatment waste water]. China Environmental Science, 2002, 22 (1): 32-35].
At present, oil refining enterprise adopts vaporizing extract process desulfurization except ammonia to the waste water containing pollutents such as high-concentration phenol, hydrogen sulfide, ammonia, but the Phenol for Waste Water content after process remains unchanged higher, and this produces follow-up biochemical treatment and impacts; Simultaneously, because phenol has suppression or toxic action to nitrifier, and then affect the Degradation of ammonia nitrogen, reduce the qualified discharge rate [Zhou Rujin of oil refining sewerage, Cheng Lihua, Li Dehao, wait the characteristic research of .HCR art breading oil refining phenolic wastewater]. petrochemical complex Journal of Chinese Universities, 2008,21 (1): 8-11].There is provided a kind of ABFT technique of improvement to certain refinery phenol-containing wastewater (stripping purify waste water water outlet) pretreatment process, for exploitation phenol-containing wastewater Biological Pretreatment new technology provides technical basis for this reason.
Summary of the invention
For solving above-mentioned prior art Problems existing, the object of the present invention is to provide a kind of oil refining phenol-containing wastewater bioremediation.
For achieving the above object, technical scheme of the present invention is:
A kind of oil refining phenol-containing wastewater bioremediation, comprises the steps:
Step one, aerated biological fludized bed Biological Pretreatment: in aerated biological fludized bed reactor, add biologic packing material;
Step 2, monitor to determine that subsequent purification operates to oil refining phenol-containing wastewater water quality;
Step 3, exclusive microbial acclimation;
Step 4, biofilm success post-reactor operation phase Selecting parameter: by investigating the impacts on phenol clearance such as flooding quantity, aeration rate, temperature, pH value, whereby processing parameter, operational condition and operation conditions are analyzed and performance evaluation.
Further, in described step one, aerated biological fludized bed reactor is 2.5m by two useful volumes
3main reaction pond and a useful volume be 1m
3settling tank in series, be made up of carbon steel; Separate with two pieces of dividing plates in each main reaction pond, form the special flow fluidized bed reactor that has internal recycle function, filler upwards promotes from both sides under the promotion of air-flow, falls under gravity, form internal recycling and so forth after arriving dividing plate top in the middle of dividing plate; Settling tank bottom design is sludge bucket, is conducive to carrying out mud-water separation; Microporous aeration disc and homemade aerating system is equipped with at the bottom of main reaction pond; Flooding quantity and aeration rate is controlled by spinner-type flowmeter.
Further, in described step one, biologic packing material chooses columniform polyethylene carrier, its diameter 25mm × high 10mm, and specific surface area is 700m
2/ m
3, porosity reaches more than 90%.
Further, in described step one, the media-filling rate in first order reaction pond is 0.88, and the media-filling rate in second order reaction pond is 0.72.
Further, the concrete operations of described step 3 are: get second pond aerobic sludge from sewage from oil refinery Treatment stations, mud is got in addition from this factory's sewage discharge ditch, the sludge volume ratio that aerobic sludge and discharge ditch are got is 3: 2, add in the lump in reactor after filtration, simultaneously add filler respectively to firsts and seconds biological reaction tank, it is 2: 1 that the filler of one-level biological reaction tank and two stage biological reaction tank adds volume ratio, then adds stripping respectively and purify waste water.In the occasional drive stage, take the mode of being interrupted water inlet, the stripping at every turn the added water yield of purifying waste water progressively increases, and this stage incubation time is 3 days; Carry out cultured continuously subsequently, the water yield progressively promotes.Filler is added in batches according to operating performance of plant and wastewater treatment efficiency between incubation period, and according to active mud content situation in reaction tank, every day, from settling tank refluxing portion mud to first order reaction pond, regularly adds phosphoric acid salt with the nutritive substance needed for supplementary microorganism simultaneously.PH value, phenol and COD concentration in every morning, sampling analysis water inlet in afternoon, water outlet water sample.Water rate control, at 200L/h, after continuous and steady operation two weeks, is treated that on filler, apposition growth goes out in cotton-shaped thicker microbial film and larger biomass, can be born certain current scour and dissolved oxygen bubble impact force, difficult drop-off.
Further, in described step 4, optimum reaction condition is chosen: hydraulic detention time is 10h, and gas-water ratio (volume) is 20: 1, and temperature is at 30 ~ 37 DEG C, and pH value is 6.5 ~ 9.
Relative to prior art, beneficial effect of the present invention is: the present invention's one oil refining phenol-containing wastewater bioremediation, the aerated biological fludized bed (ABFT) of autonomous design is adopted to carry out Biological Pretreatment to the phenolic wastewater after the process of refinery stripper plant, select interpolation active sludge, successively carry out biofilm, starting characteristics test device with the method for interval and continuum micromeehanics, regulate fluidized-bed stable operation stage hydraulic detention time, gas-water ratio, temperature and pH value to strengthen phenol removal effect.Result shows, hydraulic detention time is 10h, and gas-water ratio is 20: 1, and temperature is at 30 ~ 37 DEG C, and pH value is 6.5 ~ 9 time, and the removal effect of phenol is best, reaches more than 90%, for follow-up oil refining sewerage biochemical treatment creates good condition.
Accompanying drawing explanation
Fig. 1 is aerated biological fludized bed reactor experimental installation process flow sheet of the present invention.
Wherein, 1-filler, 2-internal recycle dividing plate, 3-aerating apparatus.
The different flooding quantity of Fig. 2 is on the impact of phenol removal effect.
Fig. 3 temperature is on the impact of phenol removal effect.
Fig. 4 pH value is on the impact of phenol removal effect.
Embodiment
Below in conjunction with the drawings and the specific embodiments, the present invention program is described in further detail
A kind of oil refining phenol-containing wastewater bioremediation, comprises the steps:
Step one, aerated biological fludized bed Biological Pretreatment: in aerated biological fludized bed reactor, add biologic packing material;
Step 2, monitor to determine that subsequent purification operates to oil refining phenol-containing wastewater water quality;
Step 3, exclusive microbial acclimation;
Step 4, biofilm success post-reactor operation phase Selecting parameter: by investigating the impacts on phenol clearance such as flooding quantity, aeration rate, temperature, pH value, whereby processing parameter, operational condition and operation conditions are analyzed and performance evaluation.
Further, in described step one, aerated biological fludized bed reactor is 2.5m by two useful volumes
3main reaction pond and a useful volume be 1m
3settling tank in series, be made up of carbon steel; Separate with two pieces of dividing plates in each main reaction pond, form the special flow fluidized bed reactor that has internal recycle function, filler upwards promotes from both sides under the promotion of air-flow, falls under gravity, form internal recycling and so forth after arriving dividing plate top in the middle of dividing plate; Settling tank bottom design is sludge bucket, is conducive to carrying out mud-water separation; Microporous aeration disc and homemade aerating system is equipped with at the bottom of main reaction pond; Flooding quantity and aeration rate is controlled by spinner-type flowmeter.
Further, in described step one, biologic packing material chooses columniform polyethylene carrier, its diameter 25mm × high 10mm, and specific surface area is 700m
2/ m
3, porosity reaches more than 90%.
Further, in described step one, the media-filling rate in first order reaction pond is 0.88, and the media-filling rate in second order reaction pond is 0.72.
Further, the concrete operations of described step 3 are: get second pond aerobic sludge from sewage from oil refinery Treatment stations, mud is got in addition from this factory's sewage discharge ditch, the sludge volume ratio that aerobic sludge and discharge ditch are got is 3: 2, add in the lump in reactor after filtration, simultaneously add filler respectively to firsts and seconds biological reaction tank, it is 2: 1 that the filler of one-level biological reaction tank and two stage biological reaction tank adds volume ratio, then adds stripping respectively and purify waste water.In the occasional drive stage, take the mode of being interrupted water inlet, the stripping at every turn the added water yield of purifying waste water progressively increases, and this stage incubation time is 3 days; Carry out cultured continuously subsequently, the water yield progressively promotes.Filler is added in batches according to operating performance of plant and wastewater treatment efficiency between incubation period, and according to active mud content situation in reaction tank, every day, from settling tank refluxing portion mud to first order reaction pond, regularly adds phosphoric acid salt with the nutritive substance needed for supplementary microorganism simultaneously.PH value, phenol and COD concentration in every morning, sampling analysis water inlet in afternoon, water outlet water sample.Water rate control, at 200L/h, after continuous and steady operation two weeks, is treated that on filler, apposition growth goes out in cotton-shaped thicker microbial film and larger biomass, can be born certain current scour and dissolved oxygen bubble impact force, difficult drop-off.
Further, in described step 4, optimum reaction condition is chosen: hydraulic detention time is 10h, and gas-water ratio (volume) is 20: 1, and temperature is at 30 ~ 37 DEG C, and pH value is 6.5 ~ 9.
Test example:
1 experimental section
1.1 experimental installation
Aerated biological fludized bed reactor is 2.5m by two useful volumes
3main reaction pond and a useful volume be 1m
3settling tank in series, be made up of carbon steel, as Fig. 1.Separate with two pieces of dividing plates in each main reaction pond, form the special flow fluidized bed reactor that has internal recycle function, filler upwards promotes from both sides under the promotion of air-flow, falls under gravity, form internal recycling and so forth after arriving dividing plate top in the middle of dividing plate; Settling tank bottom design is sludge bucket, is conducive to carrying out mud-water separation.Microporous aeration disc and homemade aerating system is equipped with at the bottom of main reaction pond.Flooding quantity and aeration rate is controlled by spinner-type flowmeter.Because this reactor is different from traditional inner loop three phase fluidized bed reactor, do not design three-phase separation area, therefore with the addition of reflux.
1.2 experiment materials and method
1.2.1 carrier
Experiment bio-carrier is a kind of columniform polyethylene carrier (diameter 25mm × high 10mm), and specific surface area is 700m
2/ m
3, porosity reaches more than 90%, and it is good that this carrier had Water permeability, and mass-transfer efficiency is high, and proportion is easy to the features such as fluidisation close to water.First order reaction pond adds 2.2m
3, second order reaction pond adds 1.8m
3, add 40m altogether
3bio-carrier.Namely the media-filling rate of one-level is 0.88, and the media-filling rate of secondary is 0.72.
1.2.2 oil refining phenol-containing wastewater water quality
Oil refining phenol-containing wastewater Biological Pretreatment testing apparatus test water takes from certain refinery stripping refining plant water outlet, and principal pollutant are the aldehydes matters such as phenol, and its influent quality situation is as follows: volatile phenol is 106 ~ 193mg/L, and average volatile phenol is 136mg/L; COD is 567 ~ 6185mg/L, and average COD is 1616mg/L; PH is 6 ~ 9.5.
1.2.3 analytical procedure
Volatile phenol adopts bromination volumetric determination, and COD adopts potassium dichromate process to measure, and DO adopts portable dissolved oxygen instrument to measure, and pH value pH combined electrode measures.
1.2.4 experimental technique
Exclusive microbial acclimation, biofilm success post-reactor enters the commencement of commercial operation stage, by investigating the impacts on phenol removal effect such as flooding quantity, aeration rate, temperature, pH value, analyzes and performance evaluation whereby to processing parameter, operational condition and operation conditions.
2 results and discussion
2.1 different flooding quantitys are on the impact of phenol removal effect
By changing aeration rate, maintaining dissolved oxygen in reactor and, at about 2.0mg/L, progressively improving flooding quantity, namely change hydraulic detention time (HRT), study different flooding quantity or HRT to the impact of phenol removal effect, result is as Fig. 3.As can be seen from Figure 3, when flooding quantity is brought up to 500L/h (HRT is 10h) by 300L/h (HRT is 17h), phenol clearance has reduction by a small margin, but still can maintain more than 90%, and water outlet phenol concentration is all at below 25mg/L; When flooding quantity is 600L/h (HRT is 8h), phenol clearance maintains about 85%; When the water yield reaches 700L/h (HRT is 7h), phenol clearance is not good, and has the trend of deterioration.Contrast firsts and seconds reaction tank phenol clearance is known, and first order reaction pond is comparatively large to the contribution of phenol removal effect, and the degraded of phenol mainly occurs in first order reaction pond, and the fluctuation of influent quality also has considerable influence to first order reaction pond treatment effect; Although second order reaction pond is less to pollutant removal contribution, shock absorption can be played under variation water quality, to ensure to reach stable effluent quality.In addition, when phenol concentration of intaking increases suddenly suddenly, the removal effect of phenol does not affect by it, illustrates that the impact resistance of this reactor is stronger.
2.2 different aeration rates are on the impact of phenol removal effect
The effect of aeration provides the dissolved oxygen required for microorganism growth on the one hand, simultaneously or the fluidisation power of carrier granule.The shadow considering hydraulic detention time and phenol removal effect to, this experimental selection under flooding quantity 500L/h, by changing aeration rate, aeration rate selects 8 respectively, 9,10,11,12m
3/ h, then, when gas-water ratio is 16: 1,18: 1,20: 1,22: 1,24: 1 respectively, research dissolved oxygen amount is on the impact of phenol clearance, and result is as table 1.
The different aeration rate of table 1 (DO) is on the impact of phenol removal effect
As shown in Table 1, when aeration rate is 10m
3during/h, the clearance of phenol is the highest, and increase along with aeration rate or reduce, the clearance homogeneous phase of phenol should reduce to some extent.When aeration rate is 12m
3during/h, DO in solution is substantially at more than 3mg/L, now dissolved oxygen is sufficient, but phenol degradation effect is degradating trend, its reason one is mainly along with the increase of aeration rate, and flow shear strengthens, to biomembranous souring grow, increase biomembranous coming off, and then the treatment effect of reactor is declined.When aeration rate is 8m
3during/h, the DO concentration in water sample is on the low side, and the respiration of microorganism is obstructed, and the biological oxidation process of phenol is suppressed simultaneously, causes phenol removal effect to decline.Therefore take into account economic principle and except phenol effect, control gas-water ratio better 20: 1.
2.3 temperature are on the impact of phenol removal effect
According to the practical experience of wastewater biochemical process, generally comparatively suitable with 20 ~ 40 DEG C.This test examine 12 ~ January (a), 10 ~ November (b), September (c) three time period differing tempss on the impact of phenol removal effect, result is as Fig. 4.As seen from the figure, the removal effect of temperature phenol 30 ~ 37 DEG C time is best, and high temperature and the removal effect of low temperature to phenol all have a certain impact, but clearance still can be kept to reach more than 80%, and comparatively low temperature is more obvious on the impact of phenol clearance for high temperature in addition.This device runs to next year by the end of January from late July always, and the minimum temperature of water sample also all remains on more than 20 DEG C therebetween, can maintain the normal growth of microorganism.Because this experiment is carried out in south, southern winter temperature also can not be too low, therefore without the need to design apparatus heat-insulation system.
2.4pH value is on the impact of phenol removal effect
Potential of hydrogen is an important indicator of microbiological deterioration waste water, and peracid is crossed alkali and is all not suitable for microorganism growth, affects its degraded to pollutent.The pH value fluctuation range of this stripping purification water outlet is also comparatively large, and this experimental study device is 10m at flooding quantity 500L/h, aeration rate
3the impact of pH value during steady running under/h.The impact of change on phenol clearance of pH value is little; But the rapid increasing of pH value during contrast biofilm, phenol degradation effect can be subject to obvious impact, needs to suspend water inlet, in order to avoid device worsens further, therefore will pay close attention to water pH value between domestication.Occur that the reason of this phenomenon is, after biofilm success, device enters stable operation stage, and biomass is large, and population structure is complicated, and the impact resistance of reactor is comparatively strong, has certain dilution buffer effect; In addition, pH value can not continue too of a specified duration higher than the water quality of 9, and general 3 ~ 4 days, can not produce larger impact to the treatment effect of device, therefore, this technique did not design neutralization tank.But higher water quality is continued to pH value, should consider.
2.5 device stable operating performances are evaluated
Flooding quantity be 500L/h, aeration rate is 10m
3under/h, continuous and steady operation 30 days, investigate device steady running situation, result is as table 2.
The steady running of table 2 device is to oil refining phenol-containing wastewater disposition
Result is known, and the removal effect of phenol is more stable, and average removal rate is 89.93%, and the mean concns of water outlet phenol is 15.35mg/L, when phenol concentration of intaking increases suddenly, can ensure that aqueous concentration is at below 20mg/L, shows good stability too.Along with the removal of phenol, in sewage, the corresponding reduction of COD concentration, reaches 36.31% to the average removal rate of COD.Device process water outlet pH value is all low than water inlet pH value, and its mean ph value difference 1.56, this is under the effect of biting phenol bacterium, change into the small molecules acid such as lower fatty acid due to organism such as phenol, and microorganism carries out the CO that respiration discharges simultaneously
2be dissolved in water, water outlet pH value is reduced.
3 conclusions
(1) the ABFT device of autonomous design has good degradation effect to oil refining phenol-containing wastewater.When HRT is 8h (flooding quantity is 600L/h), phenol clearance can reach more than 85%.The degraded of phenol is mainly carried out in first order reaction pond, and shock absorption is well played when influent quality worsens in second order reaction pond, and this reactor has stronger impact resistance.
(2) optimum range of device to temperature and pH value is wider.When water inlet pH value is 6.5 ~ 9, temperature is at 23 ~ 43 DEG C, and the clearance of phenol all can reach more than 80%, and temperature is 30 ~ 37 DEG C time, and the removal effect of phenol is best, can reach more than 90%; In addition take into account economic principle and except phenol effect, control gas-water ratio better 20: 1.
(3) device flooding quantity be 500L/h, aeration rate is 10m
3/ h continuous and steady operation one month, the removal effect of phenol is more stable, and average removal rate is 89.93%, reaches the object of Biological Pretreatment oil refining phenol-containing wastewater.
The above, be only the specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, and any change of expecting without creative work or replacement, all should be encompassed within protection scope of the present invention.Therefore, the protection domain that protection scope of the present invention should limit with claims is as the criterion.
Claims (6)
1. an oil refining phenol-containing wastewater bioremediation, is characterized in that, comprise the steps:
Step one, aerated biological fludized bed Biological Pretreatment: in aerated biological fludized bed reactor, add biologic packing material;
Step 2, monitor to determine that subsequent purification operates to oil refining phenol-containing wastewater water quality;
Step 3, exclusive microbial acclimation;
Step 4, biofilm success post-reactor operation phase Selecting parameter: flooding quantity, aeration rate, temperature, pH value condition are selected.
2. method according to claim 1, is characterized in that, in described step one, aerated biological fludized bed reactor is 2.5m by two useful volumes
3main reaction pond and a useful volume be 1m
3settling tank in series, be made up of carbon steel; Separate with two pieces of dividing plates in each main reaction pond, form the special flow fluidized bed reactor that has internal recycle function, filler upwards promotes from both sides under the promotion of air-flow, falls under gravity, form internal recycling and so forth after arriving dividing plate top in the middle of dividing plate; Settling tank bottom design is sludge bucket, is conducive to carrying out mud-water separation; Microporous aeration disc and homemade aerating system is equipped with at the bottom of main reaction pond; Flooding quantity and aeration rate is controlled by spinner-type flowmeter.
3. method according to claim 1, is characterized in that, in described step one, biologic packing material chooses columniform polyethylene carrier, its diameter 25mm × high 10mm, and specific surface area is 700m
2/ m
3, porosity reaches more than 90%.
4. method according to claim 3, is characterized in that, in described step one, the media-filling rate in first order reaction pond is 0.88, and the media-filling rate in second order reaction pond is 0.72.
5. method according to claim 1, it is characterized in that, the concrete operations of described step 3 are: get second pond aerobic sludge from sewage from oil refinery Treatment stations, mud is got in addition from sewage discharge ditch, the sludge volume ratio that aerobic sludge and discharge ditch are got is 3: 2, add in the lump in reactor after filtration, add filler respectively to firsts and seconds biological reaction tank simultaneously, it is 2: 1 that the filler of one-level biological reaction tank and two stage biological reaction tank adds volume ratio, add stripping more respectively to purify waste water, the occasional drive stage, take the mode of being interrupted water inlet, the stripping at every turn the added water yield of purifying waste water progressively increases, this stage incubation time is 3 days, carry out cultured continuously subsequently, the water yield progressively promotes, filler is added in batches according to operating performance of plant and wastewater treatment efficiency between incubation period, and according to active mud content situation in reaction tank, every day is from settling tank refluxing portion mud to first order reaction pond, regularly add phosphoric acid salt with the nutritive substance needed for supplementary microorganism simultaneously, every morning, sampling analysis water inlet in afternoon, pH value in water outlet water sample, phenol and COD concentration, water rate control is at 200L/h, after continuous and steady operation two weeks, treat that on filler, apposition growth goes out in cotton-shaped thicker microbial film and larger biomass, certain current scour and dissolved oxygen bubble impact force can be born, difficult drop-off.
6. method according to claim 1, is characterized in that, in described step 4, optimum reaction condition is chosen: hydraulic detention time is 10h, and air water volume ratio is 20: 1, and temperature is at 30 ~ 37 DEG C, and pH value is 6.5 ~ 9.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109534515A (en) * | 2018-12-07 | 2019-03-29 | 大连理工大学 | Phenolic comp ' ds pollution based on moving bed biofilm reactor removes system and method |
| CN111115802A (en) * | 2020-01-17 | 2020-05-08 | 中冶焦耐(大连)工程技术有限公司 | Efficient culture and domestication method for treating coking wastewater activated sludge |
| CN111620446A (en) * | 2020-06-05 | 2020-09-04 | 北京赛富威环境工程技术有限公司 | Treatment method of high-concentration phenol-containing industrial wastewater |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597125A (en) * | 2009-07-09 | 2009-12-09 | 北京科技大学 | A kind of technology for the treatment of coking wastewater by biomembrance process |
| CN202038947U (en) * | 2011-04-23 | 2011-11-16 | 四川达沃斯生态环保科技有限公司 | Integrated sewage treatment system of biological fluidized bed |
-
2014
- 2014-12-11 CN CN201410752160.1A patent/CN104529059A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597125A (en) * | 2009-07-09 | 2009-12-09 | 北京科技大学 | A kind of technology for the treatment of coking wastewater by biomembrance process |
| CN202038947U (en) * | 2011-04-23 | 2011-11-16 | 四川达沃斯生态环保科技有限公司 | Integrated sewage treatment system of biological fluidized bed |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109534515A (en) * | 2018-12-07 | 2019-03-29 | 大连理工大学 | Phenolic comp ' ds pollution based on moving bed biofilm reactor removes system and method |
| CN111115802A (en) * | 2020-01-17 | 2020-05-08 | 中冶焦耐(大连)工程技术有限公司 | Efficient culture and domestication method for treating coking wastewater activated sludge |
| CN111620446A (en) * | 2020-06-05 | 2020-09-04 | 北京赛富威环境工程技术有限公司 | Treatment method of high-concentration phenol-containing industrial wastewater |
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