CN104098228A - Organic amine wastewater treatment method - Google Patents
Organic amine wastewater treatment method Download PDFInfo
- Publication number
- CN104098228A CN104098228A CN201410351298.0A CN201410351298A CN104098228A CN 104098228 A CN104098228 A CN 104098228A CN 201410351298 A CN201410351298 A CN 201410351298A CN 104098228 A CN104098228 A CN 104098228A
- Authority
- CN
- China
- Prior art keywords
- waste water
- hour
- treatment process
- water outlet
- treatment
- 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
Links
- 150000001412 amines Chemical class 0.000 title claims abstract description 20
- 238000004065 wastewater treatment Methods 0.000 title abstract description 10
- 238000000034 method Methods 0.000 claims abstract description 53
- 239000002351 wastewater Substances 0.000 claims abstract description 40
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 230000003647 oxidation Effects 0.000 claims abstract description 30
- 230000015271 coagulation Effects 0.000 claims abstract description 25
- 238000005345 coagulation Methods 0.000 claims abstract description 25
- 239000000126 substance Substances 0.000 claims abstract description 13
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 18
- 239000001301 oxygen Substances 0.000 claims description 18
- 229910052760 oxygen Inorganic materials 0.000 claims description 18
- 239000010802 sludge Substances 0.000 claims description 14
- 238000001556 precipitation Methods 0.000 claims description 12
- 238000011068 loading method Methods 0.000 claims description 10
- -1 hydroxyl radical free radical Chemical class 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 239000011790 ferrous sulphate Substances 0.000 claims description 6
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 6
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 6
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 6
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 6
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 6
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000010865 sewage Substances 0.000 claims description 5
- 230000007935 neutral effect Effects 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 229920002401 polyacrylamide Polymers 0.000 claims description 4
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 claims description 3
- 229960004418 trolamine Drugs 0.000 claims description 3
- 230000031018 biological processes and functions Effects 0.000 claims description 2
- 231100001261 hazardous Toxicity 0.000 claims description 2
- 230000002209 hydrophobic effect Effects 0.000 claims description 2
- 231100000053 low toxicity Toxicity 0.000 claims description 2
- 230000014759 maintenance of location Effects 0.000 claims description 2
- 231100000252 nontoxic Toxicity 0.000 claims description 2
- 230000003000 nontoxic effect Effects 0.000 claims description 2
- 230000001473 noxious effect Effects 0.000 claims description 2
- 150000002894 organic compounds Chemical class 0.000 claims description 2
- 150000003384 small molecules Chemical class 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 238000002306 biochemical method Methods 0.000 abstract 1
- 231100000331 toxic Toxicity 0.000 abstract 1
- 230000002588 toxic effect Effects 0.000 abstract 1
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 22
- 230000000694 effects Effects 0.000 description 7
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 description 6
- 239000012528 membrane Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000004308 accommodation Effects 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- GETQZCLCWQTVFV-UHFFFAOYSA-N trimethylamine Chemical compound CN(C)C GETQZCLCWQTVFV-UHFFFAOYSA-N 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- KGWDUNBJIMUFAP-KVVVOXFISA-N Ethanolamine Oleate Chemical compound NCCO.CCCCCCCC\C=C/CCCCCCCC(O)=O KGWDUNBJIMUFAP-KVVVOXFISA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 1
- 206010073310 Occupational exposures Diseases 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000007269 microbial metabolism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 231100000675 occupational exposure Toxicity 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- GOLXNESZZPUPJE-UHFFFAOYSA-N spiromesifen Chemical compound CC1=CC(C)=CC(C)=C1C(C(O1)=O)=C(OC(=O)CC(C)(C)C)C11CCCC1 GOLXNESZZPUPJE-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention provides an organic amine wastewater treatment method. According to the method, organic amine in wastewater can be removed mainly by performing pre-oxidation and anaerobic treatment on wastewater, allowing treated wastewater to pass an anoxic-aerobic biological reactor, then performing enhanced coagulation and advanced oxidation, and finally allowing the treated wastewater to pass an aerating biological filter. By the adoption of the method, toxic and harmful substances in wastewater can be foundationally removed, and difficulties in the follow-up treatment of the wastewater through a biochemical method can be reduced; the organic amine wastewater treatment method is efficient in operation, and is stable and safe in discharged water.
Description
Technical field
The present invention relates to organic amine amine field of waste water treatment, specifically a kind of removal organic amine treatment process.
Background technology
Organic amine product is broad-spectrum important industrial chemicals, mainly comprises the derived product of Monomethylamine, dimethylamine, Trimethylamine 99 and methylamine product: dimethyl formamide, N,N-DIMETHYLACETAMIDE etc.These products inevitably produce some byproducts and waste water in production building-up process, and part material also can enter factory effluent.Along with the development of China's economy, the demand of fine chemical material is increased gradually, the wastewater flow rate that these products produce in process of production also increases day by day.In organic amine factory effluent, most of material all contains amino, the feature of high COD (1g/L~10g/L) and high salinity (10~30g/L), these compositions can discharge ammonia nitrogen in biodegradation process, if directly enter natural water, probably can cause the eutrophication of water body, so this kind of waste water must effectively be processed before entering water body.
Organic amine waste water belongs to more unmanageable organism, and waste water N/C is higher, at present domestic waste water treatment process, generally adopt conventional biochemical processing process, but effect is limited, and effluent quality is not good.This treatment process is for organic amine chemistry stable in properties, and difficult for biological degradation, by adding a small amount of oxygenant preoxidation, improves the biodegradability of waste water, largely improves the removal effect of follow-up bioprocess technology to COD; For reaching emission standard organic amine bio-chemical effluent tradition, adopt oxygenant direct oxidation up to standard, though effective but expense is high, present method adopts enhanced coagulation-advanced oxidation-biological combination process for advanced treatment to process bio-chemical effluent, under identical treatment effect, reduce oxygenant consumption, reduced the cost of operation.
Summary of the invention
For the deficiency of order organic amine method of wastewater treatment, the present invention aims to provide a kind of effective organic amine method of wastewater treatment.The method specifically comprises the steps:
A. preoxidation
Organic amine waste water is carried out to preoxidation with Fenton or O3, decompose hazardous and noxious substances, improve the biodegradability of waste water; Waste water after preoxidation is adjusted to neutrality, enters settling tank precipitation 2-4 hour;
B anaerobism
Waste water through precipitation is carried out to anaerobic treatment, remove organism;
C. Anoxybiotic-aerobic biologic reactor
Anaerobic effluent is entered to Anoxybiotic-aerobic biologic reactor, remove COD and nitrogen in sewage;
D. enhanced coagulation
To Anoxybiotic-aerobic biologic reactor, enhanced coagulation is carried out in water outlet, removes the hydrophobic organic compound matter of bio-chemical effluent;
E. advanced oxidation
Water outlet after enhanced coagulation is carried out to advanced oxidation, produce the hydroxyl radical free radical (OH) with strong oxidation capacity, make macromole hardly degraded organic substance be oxidized to low toxicity or nontoxic small-molecule substance;
F. biological process advanced treatment
Advanced oxidation water outlet enters BAF, controls the residence time, dissolved oxygen, further removes COD, makes water outlet qualified discharge.
The enhanced coagulation step of this treatment process further comprises: regulate Anoxybiotic-aerobic biologic reactor water outlet PH to 4-8, according to the ratio of 100-400mg/L, add bodied ferric sulfate and carry out coagulation, stir 15 minutes, according to 2-4mg/L ratio, add polyacrylamide, then enter settling tank precipitation.
The advanced oxidation of this treatment process can adopt following steps:
With Fenton, regulate pH value to 1-5 the water outlet of enhanced coagulation, wherein, H2O2 dosage 100-600mg/L, and the ratio between 1/10-1/6 adds ferrous sulfate according to Fe2+/H2O2, oxidation 1-6 hour, adds alkali and regulates PH to neutral after oxidation, water outlet enters settling tank precipitation.
The advanced oxidation of this treatment process also can adopt following steps:
Anoxybiotic-aerobic biologic reactor is gone out to water ph value and be adjusted to 7-10, according to 100-400mg/L, add O3, use low pressure ultraviolet ray to irradiate simultaneously, reaction 1-4 hour.
The step C of present method also comprises, anoxic denitrification technique residence time HRT >=24 hour, aerobe reactor load 0.1-0.2kgCOD/kgMLSS.d, sludge concentration MLSS >=4000mg/L, dissolved oxygen is controlled at 2-4mg/L, hydraulic detention time HRT >=24 hour, second pond mud is back to anoxic pond by 50-80%, denitrification internal reflux ratio 200-400%.
In the step F of present method, waste water pH value in BAF is 6-8, dissolved oxygen 2-5mg/L, retention time of sewage >=6h.
Organic amine described in present method is: N methyldiethanol amine, DMF, N-N,N-DIMETHYLACETAMIDE, trolamine.
Present method can adopt USAB or ABR anaerobic treatment process, anaerobism temperature 30-40 ℃, and anaerobism volumetric loading 3-6kgCOD/m3.d, waste water PH is controlled between 7-8.
Accompanying drawing explanation
Fig. 1 present method is carried out the schematic flow sheet of organic amine wastewater treatment.
Embodiment
For making the object, technical solutions and advantages of the present invention more cheer and bright, below in conjunction with embodiment and with reference to accompanying drawing, the present invention is described in more detail.Should be appreciated that, these descriptions are exemplary, and do not really want to limit the scope of the invention.In addition, in the following description, omitted the description to known configurations and technology, to avoid unnecessarily obscuring concept of the present invention.
For overcoming problems of the prior art, organic amine waste water treatment process involved in the present invention adopts " preoxidation-anaerobic-anoxic/aerobe reactor-enhanced coagulation/advanced oxidation-biological advanced treatment " combination process, and concrete technical scheme is as follows:
1 preoxidation: can adopt two kinds of methods: 1. hydrogen peroxide (H2O2) oxidation capacity is limited separately, adopt Fenton oxidation to its essence is that H2O2 generates the hydroxyl radical free radical (OH) with high reaction activity under the katalysis of Fe2+, OH can make its degraded with most of organism effects, Fenton oxidation acid adding (hydrochloric acid, sulfuric acid) regulate PH to 1-5, H2O2 dosage 100-400mg/L, ferrous sulfate adds by Fe2+/H2O2 mol ratio 1/10-1/6, oxidization time 1-4 hour, after oxidation, add alkali (sodium hydroxide or lime) and be adjusted to neutrality, enter settling tank precipitation 2-4 hour, 2. O3 oxidation, adds acid-alkali accommodation PH to 7-10, dosage 100-600mg/L, oxidization time 1-4 hour.
2. anaerobism can adopt the anaerobic treatment process such as UASB or ABR, and waste water keeps anaerobism temperature 30-40 ℃ with steam, anaerobism volumetric loading 3-6kgCOD/m3.d, and waste water PH is controlled between 7-8, residence time HRT >=24 hour.
3. anaerobic effluent enters Anoxybiotic-aerobic biologic reactor, anoxic section is for denitrogenation, aerobic section is for removing the organism of water, ammonia nitrogen is oxidized to nitric nitrogen simultaneously, anoxic denitrification technique hydraulic detention time 24-48 hour, be controlled at≤0.5mg/L of dissolved oxygen, (implication of sludge loading aspect microbial metabolism is exactly F/M ratio to aerobe reactor load 0.1-0.2kgCOD/kgMLSS.d, the amount of the pollutent that the active sludge of representation unit quality is removed within the unit time, units/kg COD (BOD)/kg mud d), sludge concentration MLSS >=8000mg/L, dissolved oxygen is controlled at 2-4mg/L, PH is controlled between 7-8, hydraulic detention time HRT >=24 hour, second pond mud is back to anoxic pond by 50-80%, denitrification internal reflux ratio 200-400%, if with membrane bioreactor membrane flux 10-20L/m2.h, denitrification internal reflux ratio 200-400%.
4. enhanced coagulation
Enhanced coagulation is point in source water dosing coagulant and control certain pH value, thereby organic removal effect in raising conventional processing, the water outlet of Anoxybiotic-aerobic biologic reactor is added to acid-alkali accommodation PH to 4-8, add 100-400mg/L bodied ferric sulfate (PFS) coagulation, churning time 15 minutes, add 2-4mg/L anionic polyacrylamide (PAM) and contribute to flco to become large, after enter settling tank residence time 2-4 hour.
5. advanced oxidation
Coagulation water outlet can adopt two kinds of methods to carry out advanced oxidation, 1. Fenton oxidation: coagulation water outlet acid adding regulates PH to 1-5, H2O2 dosage 100-600mg/L, ferrous sulfate adds by Fe2+/H2O2 mol ratio 1/10-1/6, oxidization time 1-6 hour, water outlet adds alkali and regulates PH to 7-9, enters settling tank precipitation 2-4 hour; 2. a lot of petroleum chemical enterprises consider to forbid transportation and storage oxygenant (H2O2 from security standpoint, clorox), therefore can adopt online generation oxygenant technology ultraviolet-ozone oxidation, with acid and alkali, regulate PH to 7-10, low pressure ultraviolet lamp 15-45KW, ultraviolet wavelength 254nm, ultra violet lamp passes into O3 simultaneously, O3 dosage 100-400mg/L, reaction times 1-4 hour, O3 produces OH under the effect of ultraviolet, the hydrophilic organics hydrophilicity of difficult degradation in oxidized waste water, and the biodegradability of waste water improves simultaneously.
6. BAF is a kind of aerobic activated sludge and the technology of filtering combination, there is working cost low, effluent quality is the feature such as safely, waste water pH value in BAF is 6-8, adopt 2-4mm haydite to do filler, the residence time is greater than 6 hours, and dissolved oxygen is controlled at 2-5mg/L, once, water outlet reaches outer row's standard in back flushing in 24-72 hour.
Embodiment 1
At present, the de-H2S of oil refinery dry gas adopts alcohol amine absorption process more, and hydramine is mainly thanomin, diethanolamine, trolamine and N methyldiethanol amine, wherein uses comparatively generally N methyldiethanol amine.Compare with traditional method, alcohol amine absorption process has the advantages such as desulfuration efficiency is high, technical process simple, absorption liquid loop cycle is long.Because absorption liquid recycles, in device steady running process, can not produce the waste water containing hydramine, but device shutting down or be affected by other factors and while causing the fluctuation of certain operations, can cause the discharge of part hydramine, the Wastewater Treated by Activated Sludge Process process to downstream when sewage work impacts.
N methyldiethanol amine waste liquid COD7000-10000mg/L, TN=400-450mg/L, TDS=1%-3%, adopts present method anaerobic UASB-anoxic/aerobic membrane bioreactor-enhanced coagulation-UV/ozone oxidation-BAF; UASB temperature 30-35 ℃, residence time HRT=48 hour, volumetric loading 6kgCOD/m3.d; Waste water is in the residence time of anoxic section HRT=24 hour, dissolved oxygen≤0.5mg/L, internal reflux ratio 300%; Membrane bioreactor hydraulic detention time HRT=48 hour, sludge concentration 10400mg/L, sludge loading 0.17kgCOD/kgMLSS.d, dissolved oxygen 3-4mg/L, flat sheet membrane membrane flux 15L/m2.h; Bodied ferric sulfate coagulation PH is 5, and dosage 250mg/L, precipitates 2 hours at 15 minutes coagulation time; Ultraviolet-ozone reaction PH=10,, low pressure ultraviolet lamp 15KW, ultraviolet 254nm, the reacting weight 300mg/L of O3,2 hours reaction times; BAF dissolved oxygen is 3-4mg/L, residence time HRT=8 hour.Get the water outlet of each processing unit and carry out COD, NH3-N detection, test-results is as table 1.
Table 1 is used processing unit provided by the invention in the removal process of each unit COD and TN, NH3-N
Embodiment 2
DMF (N, N-dimethylformamide are called for short DMF) is a kind of organic solvent of excellent property, can dissolve each other with water and most organic solvent, therefore has the title of menstruum universale, in chemical industry, has a wide range of applications.China's Occupational Exposure harm of poison grading determines that DMF is II level (moderate harm), and the U.S. determines that DMF is that human body may carcinogenic substance.DMF waste water enters in water and can cause biological chemistry oxygen-consumption and nitrogen content to increase, and water quality is worsened rapidly, and be difficult to biological degradation, the at present domestic and international rarely seen report to DMF purification of waste water and processing.Therefore it is very necessary the waste water that contains DMF being processed
N methyldiethanol amine waste water COD 7000-10000mg/L, TN=400-450mg/L, adopts O3 preoxidation-anaerobic UASB-anoxic/aerobic membrane bioreactor-enhanced coagulation-Fenton oxidizing-biological biological filtering tank.O3 preoxidation dosage 300mg/L,, reaction PH=10,2 hours reaction times; UASB temperature 30-35 ℃, residence time HRT=48 hour, volumetric loading 3-5kgCOD/m3.d; Waste water is in the residence time of anoxic section HRT=24 hour, dissolved oxygen≤0.5mg/L, internal reflux ratio 300%; Membrane bioreactor hydraulic detention time HRT=48 hour, sludge concentration 9200mg/L, sludge loading 0.18 kgCOD/kgMLSS.d, dissolved oxygen 3-4mg/L, flat sheet membrane membrane flux 15L/m2.h; Enhanced coagulation bodied ferric sulfate coagulation PH is 5, dosage 250mg/L; Fenton oxidation regulates PH=3.5, H2O2 dosage 200-400mg/L, and ferrous sulfate adds by Fe2+/H2O2 mol ratio 1/6, oxidization time 2 hours, water outlet regulates PH to neutral, enters settling tank precipitation HRT=4 hour; BAF dissolved oxygen=3mg/L, residence time HRT=12 hour.Get the water outlet of each processing unit and carry out COD, NH3-N detection, test-results is as table 2.
Table 2 is used processing unit provided by the invention in the removal process of each unit COD and NH3-N
Embodiment 3
A methylamine waste liquid, waste water COD 5000-6000mg/L, TN=200-360mg/L; Adopt anaerobic UASB-anoxia/aerobic biological reactor-enhanced coagulation-Fenton oxidizing-biological biological filtering tank.UASB temperature 30-35 ℃, residence time HRT=24 hour, volumetric loading 5-6kgCOD/m3.d; Waste water is in the residence time of anoxic section HRT=24 hour, dissolved oxygen≤0.5mg/L, return sludge ratio 60%, internal reflux ratio 300%; Aerobe reactor hydraulic detention time HRT=48 hour, sludge concentration 5000mg/L, sludge loading 0.15kgCOD/kgMLSS.d, dissolved oxygen 3-4mg/L; Enhanced coagulation bodied ferric sulfate coagulation PH is 7, dosage 250mg/L, and Fenton oxidation regulates PH=3.5, H2O2=200-400mg/L, ferrous sulfate adds by Fe2+/H2O2 mol ratio 1/6, oxidization time 2 hours, water outlet regulates PH to neutral, enters settling tank precipitation HRT=4 hour; BAF dissolved oxygen=3mg/L, residence time HRT=8 hour.Get the water outlet of each processing unit and carry out COD, NH3-N detection, test-results is as table 3.
Table 3 is used processing unit provided by the invention in the removal process of each unit COD and NH3-N
Claims (8)
1. a treatment process for organic amine waste water, is characterized in that treatment step is as follows:
A. preoxidation
Organic amine waste water is carried out to preoxidation with Fenton or O3, decompose hazardous and noxious substances, improve the biodegradability of waste water; Waste water after preoxidation is adjusted to neutrality, enters settling tank precipitation 2-4 hour;
B anaerobism
Waste water through precipitation is carried out to anaerobic treatment, remove organism;
C. Anoxybiotic-aerobic biologic reactor
Anaerobic effluent is entered to Anoxybiotic-aerobic biologic reactor, remove COD and nitrogen in sewage;
D. enhanced coagulation
To Anoxybiotic-aerobic biologic reactor, enhanced coagulation is carried out in water outlet, removes the hydrophobic organic compound matter of bio-chemical effluent;
E. advanced oxidation
Water outlet after enhanced coagulation is carried out to advanced oxidation, produce the hydroxyl radical free radical (OH) with strong oxidation capacity, make macromole hardly degraded organic substance be oxidized to low toxicity or nontoxic small-molecule substance;
F. biological process advanced treatment
Advanced oxidation water outlet enters BAF, controls the residence time, dissolved oxygen, further removes COD, makes water outlet qualified discharge.
2. treatment process according to claim 1, is characterized in that described enhanced coagulation step comprises:
Regulate Anoxybiotic-aerobic biologic reactor water outlet PH to 4-8, according to the ratio of 100-400mg/L, add bodied ferric sulfate and carry out coagulation, stir 15 minutes, according to 2-4mg/L ratio, add polyacrylamide, then enter settling tank precipitation.
3. treatment process according to claim 2, is characterized in that described advanced oxidation step comprises:
With Fenton, regulate pH value to 1-5 the water outlet of enhanced coagulation, wherein, H2O2 dosage 100-600mg/L, and the ratio between 1/10-1/6 adds ferrous sulfate according to Fe2+/H2O2, oxidation 1-6 hour, adds alkali and regulates PH to neutral after oxidation, water outlet enters settling tank precipitation.
4. treatment process according to claim 2, is characterized in that described advanced oxidation comprises:
Anoxybiotic-aerobic biologic reactor is gone out to water ph value and be adjusted to 7-10, according to 100-400mg/L, add O3, use low pressure ultraviolet ray to irradiate simultaneously, reaction 1-4 hour.
5. according to the treatment process described in claim 3 or 4, it is characterized in that described step C also comprises, anoxic denitrification technique residence time HRT >=24 hour, aerobe reactor load 0.1-0.2kgCOD/kgMLSS.d, sludge concentration MLSS >=4000mg/L, dissolved oxygen is controlled at 2-4mg/L, hydraulic detention time HRT >=24 hour, second pond mud is back to anoxic pond by 50-80%, denitrification internal reflux ratio 200-400%.
6. treatment process according to claim 4, is characterized in that in described treatment step F, waste water pH value in BAF is 6-8, dissolved oxygen 2-5mg/L, retention time of sewage >=6h.
7. treatment process according to claim 4, is characterized in that described organic amine is: N methyldiethanol amine, DMF, N-N,N-DIMETHYLACETAMIDE, trolamine.
8. treatment process according to claim 4, is characterized in that in described treatment step B: can adopt USAB or ABR anaerobic treatment process, and anaerobism temperature 30-40 ℃, anaerobism volumetric loading 3-6kgCOD/m3.d, waste water PH is controlled between 7-8.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201410351298.0A CN104098228B (en) | 2014-07-22 | 2014-07-22 | A kind of organic amine wastewater treatment process |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201410351298.0A CN104098228B (en) | 2014-07-22 | 2014-07-22 | A kind of organic amine wastewater treatment process |
Publications (2)
Publication Number | Publication Date |
---|---|
CN104098228A true CN104098228A (en) | 2014-10-15 |
CN104098228B CN104098228B (en) | 2015-11-04 |
Family
ID=51666824
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN201410351298.0A Expired - Fee Related CN104098228B (en) | 2014-07-22 | 2014-07-22 | A kind of organic amine wastewater treatment process |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN104098228B (en) |
Cited By (22)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104276696A (en) * | 2014-10-16 | 2015-01-14 | 南京国能环保工程有限公司 | Pretreatment method of high-concentration organic wastewater containing DMAC (dimethylacetamide) |
CN104773787A (en) * | 2015-03-24 | 2015-07-15 | 大连理工齐旺达化工科技有限公司 | Method for reducing chemical oxygen demand of zeolite molecular sieve production wastewater |
CN104773786A (en) * | 2015-03-24 | 2015-07-15 | 大连理工齐旺达化工科技有限公司 | Method for reducing total organic carbon content of zeolite molecular sieve production wastewater |
CN104803547A (en) * | 2015-03-25 | 2015-07-29 | 江苏博大环保股份有限公司 | Method for treating COW-DM sewage with high chemical stability and biodegradation difficulty |
CN104828941A (en) * | 2014-11-17 | 2015-08-12 | 环境保护部华南环境科学研究所 | A2O-BAF combined process and A2O-BAF combined device |
CN105541017A (en) * | 2015-12-30 | 2016-05-04 | 北京清大国华环境股份有限公司 | Method and device for realizing zero emission of strong brine |
CN105692971A (en) * | 2016-03-18 | 2016-06-22 | 沈阳飞机工业(集团)有限公司 | Method for treating aluminum alloy chemical milling cleaning liquid through electro-Fenton oxidization |
CN105819625A (en) * | 2016-05-09 | 2016-08-03 | 中国科学院生态环境研究中心 | Tanning synthetic wastewater treatment system and treatment method |
CN106830571A (en) * | 2017-04-05 | 2017-06-13 | 绍兴柯桥江滨水处理有限公司 | The processing system and processing method of a kind of antibiotic fermentation waste water |
CN107162335A (en) * | 2017-06-21 | 2017-09-15 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for handling chitin pharmaceutical wastewater |
CN108892321A (en) * | 2018-07-27 | 2018-11-27 | 江苏南大华兴环保科技股份公司 | A kind of method of biological electrochemical coupling technique processing pyridine farm chemical waste water |
CN108947139A (en) * | 2018-08-13 | 2018-12-07 | 九江天赐高新材料有限公司 | A kind of processing method of the high ammonia-nitrogen wastewater containing organic amine |
CN109293176A (en) * | 2018-12-13 | 2019-02-01 | 湖南大辰环保科技有限公司 | DMF low-pressure distillation recycling column overhead wastewater treatment method and system in film production |
CN109502879A (en) * | 2018-03-05 | 2019-03-22 | 辽宁石油化工大学 | A kind of high-concentration hardly-degradable industrial wastewater treatment system and processing method |
CN109928541A (en) * | 2019-03-21 | 2019-06-25 | 中科海创环境科技(大连)有限公司 | A kind of triethylamine wastewater treatment method |
CN110407408A (en) * | 2019-07-22 | 2019-11-05 | 东莞市逸轩环保科技有限公司 | Oil-polluted water treatment process |
CN110498562A (en) * | 2019-08-08 | 2019-11-26 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
CN110723802A (en) * | 2019-10-09 | 2020-01-24 | 合肥停弦渡生物科技有限公司 | Improved HiPO based on pre-oxidantxDeep oxidation treatment method |
CN110759610A (en) * | 2019-12-24 | 2020-02-07 | 山东万圣博化工有限公司 | Adhesive industrial wastewater treatment method |
CN113582338A (en) * | 2021-06-29 | 2021-11-02 | 山东联盟化工股份有限公司 | Treatment method of high-concentration ethylenediamine wastewater |
CN113772893A (en) * | 2021-09-27 | 2021-12-10 | 上海沁泰环境科技有限公司 | Treatment process of alcohol amine organic nitrogen wastewater |
CN113955824A (en) * | 2021-11-24 | 2022-01-21 | 中国华能集团清洁能源技术研究院有限公司 | Method for treating wastewater containing carbon dioxide capture absorbent by photo-Fenton oxidation process |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102849893A (en) * | 2012-08-06 | 2013-01-02 | 南京凯盛国际工程有限公司 | Treatment method of high-concentration nondegradable organic wastewater |
-
2014
- 2014-07-22 CN CN201410351298.0A patent/CN104098228B/en not_active Expired - Fee Related
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102849893A (en) * | 2012-08-06 | 2013-01-02 | 南京凯盛国际工程有限公司 | Treatment method of high-concentration nondegradable organic wastewater |
Cited By (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104276696A (en) * | 2014-10-16 | 2015-01-14 | 南京国能环保工程有限公司 | Pretreatment method of high-concentration organic wastewater containing DMAC (dimethylacetamide) |
CN104828941A (en) * | 2014-11-17 | 2015-08-12 | 环境保护部华南环境科学研究所 | A2O-BAF combined process and A2O-BAF combined device |
CN104773787A (en) * | 2015-03-24 | 2015-07-15 | 大连理工齐旺达化工科技有限公司 | Method for reducing chemical oxygen demand of zeolite molecular sieve production wastewater |
CN104773786A (en) * | 2015-03-24 | 2015-07-15 | 大连理工齐旺达化工科技有限公司 | Method for reducing total organic carbon content of zeolite molecular sieve production wastewater |
CN104803547A (en) * | 2015-03-25 | 2015-07-29 | 江苏博大环保股份有限公司 | Method for treating COW-DM sewage with high chemical stability and biodegradation difficulty |
CN105541017A (en) * | 2015-12-30 | 2016-05-04 | 北京清大国华环境股份有限公司 | Method and device for realizing zero emission of strong brine |
CN105541017B (en) * | 2015-12-30 | 2023-06-30 | 清大国华环境集团股份有限公司 | Method and device for zero emission of strong brine |
CN105692971A (en) * | 2016-03-18 | 2016-06-22 | 沈阳飞机工业(集团)有限公司 | Method for treating aluminum alloy chemical milling cleaning liquid through electro-Fenton oxidization |
CN105819625A (en) * | 2016-05-09 | 2016-08-03 | 中国科学院生态环境研究中心 | Tanning synthetic wastewater treatment system and treatment method |
CN106830571B (en) * | 2017-04-05 | 2019-11-29 | 绍兴柯桥江滨水处理有限公司 | A kind of processing system and processing method of antibiotic fermentation waste water |
CN106830571A (en) * | 2017-04-05 | 2017-06-13 | 绍兴柯桥江滨水处理有限公司 | The processing system and processing method of a kind of antibiotic fermentation waste water |
CN107162335A (en) * | 2017-06-21 | 2017-09-15 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for handling chitin pharmaceutical wastewater |
CN109502879A (en) * | 2018-03-05 | 2019-03-22 | 辽宁石油化工大学 | A kind of high-concentration hardly-degradable industrial wastewater treatment system and processing method |
CN108892321A (en) * | 2018-07-27 | 2018-11-27 | 江苏南大华兴环保科技股份公司 | A kind of method of biological electrochemical coupling technique processing pyridine farm chemical waste water |
CN108892321B (en) * | 2018-07-27 | 2021-04-23 | 江苏南大华兴环保科技股份公司 | Method for treating pyridine pesticide wastewater by biological-electrochemical coupling technology |
CN108947139A (en) * | 2018-08-13 | 2018-12-07 | 九江天赐高新材料有限公司 | A kind of processing method of the high ammonia-nitrogen wastewater containing organic amine |
CN109293176A (en) * | 2018-12-13 | 2019-02-01 | 湖南大辰环保科技有限公司 | DMF low-pressure distillation recycling column overhead wastewater treatment method and system in film production |
CN109928541A (en) * | 2019-03-21 | 2019-06-25 | 中科海创环境科技(大连)有限公司 | A kind of triethylamine wastewater treatment method |
CN110407408A (en) * | 2019-07-22 | 2019-11-05 | 东莞市逸轩环保科技有限公司 | Oil-polluted water treatment process |
CN110498562A (en) * | 2019-08-08 | 2019-11-26 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
CN110498562B (en) * | 2019-08-08 | 2022-05-13 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
CN110723802A (en) * | 2019-10-09 | 2020-01-24 | 合肥停弦渡生物科技有限公司 | Improved HiPO based on pre-oxidantxDeep oxidation treatment method |
CN110759610A (en) * | 2019-12-24 | 2020-02-07 | 山东万圣博化工有限公司 | Adhesive industrial wastewater treatment method |
CN113582338A (en) * | 2021-06-29 | 2021-11-02 | 山东联盟化工股份有限公司 | Treatment method of high-concentration ethylenediamine wastewater |
CN113772893A (en) * | 2021-09-27 | 2021-12-10 | 上海沁泰环境科技有限公司 | Treatment process of alcohol amine organic nitrogen wastewater |
CN113955824A (en) * | 2021-11-24 | 2022-01-21 | 中国华能集团清洁能源技术研究院有限公司 | Method for treating wastewater containing carbon dioxide capture absorbent by photo-Fenton oxidation process |
Also Published As
Publication number | Publication date |
---|---|
CN104098228B (en) | 2015-11-04 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN104098228B (en) | A kind of organic amine wastewater treatment process | |
CN102452770A (en) | Biochemical treatment/advanced oxidation treatment coupled sewage treatment technique | |
CN105693029A (en) | Landfill leachate treatment process | |
CN101659484B (en) | Catalytic oxidation method capable of recycling waste residues | |
CN101570368A (en) | Method for processing waste water by fenton oxidation | |
CN106830536A (en) | A kind of advanced treatment process of ferment antibiotics waste water | |
CN101693569A (en) | Device for catalyzing and oxidating ozone effectively | |
CN101514070B (en) | Disposal technique of nitrobenzene-containing sewage | |
CN101767859A (en) | Waste water treatment method combining Fenton oxidization and microwave catalysis phase | |
CN102616979B (en) | Treatment method for surface treatment liquid wastewater of metal processing | |
CN203833777U (en) | Treatment device for ozone oxidation treatment leachate nanofiltration concentrated solution | |
CN102786179A (en) | Method for treatment and comprehensive utilization of high-concentration organic wastewater | |
CN105712564A (en) | Equipment for processing waste water through glyphosate production | |
CN103073154B (en) | Treatment process of refractory pharmaceutical park tail water | |
CN207726919U (en) | A kind of Multistage Membranes composite processing system of landfill leachate | |
CN113443796A (en) | Ultraviolet catalytic oxidation wastewater treatment process | |
Yusif et al. | A review of tannery effluent treatment | |
CN102674621A (en) | Method for treating high-concentration morpholine wastewater | |
Pieczykolan et al. | Comparison of landfill leachate treatment efficiency using the advanced oxidation processes | |
CN104496130B (en) | A kind of method of processing difficult degradation Fine Chemistry Wastewater | |
CN105254116A (en) | Chemical waste water processing method | |
CN115259573A (en) | Treatment method of high-sulfate organic wastewater in petroleum refining industry | |
CN105776779A (en) | Comprehensive pesticide wastewater treatment method | |
CN111170433A (en) | Coagulant for water-based ink wastewater and water-based ink wastewater treatment method | |
CN205687733U (en) | A kind of refractory organic industrial sewage advanced treatment system |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C06 | Publication | ||
PB01 | Publication | ||
C10 | Entry into substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
C14 | Grant of patent or utility model | ||
GR01 | Patent grant | ||
CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151104 |
|
CF01 | Termination of patent right due to non-payment of annual fee |