CN105884129A - Treating method and device of organic wastewater - Google Patents
Treating method and device of organic wastewater Download PDFInfo
- Publication number
- CN105884129A CN105884129A CN201610240435.2A CN201610240435A CN105884129A CN 105884129 A CN105884129 A CN 105884129A CN 201610240435 A CN201610240435 A CN 201610240435A CN 105884129 A CN105884129 A CN 105884129A
- Authority
- CN
- China
- Prior art keywords
- oxidation
- organic wastewater
- reverse osmosis
- membrane
- cod
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 94
- 239000002351 wastewater Substances 0.000 title claims abstract description 63
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 93
- 239000012528 membrane Substances 0.000 claims abstract description 91
- 238000011282 treatment Methods 0.000 claims abstract description 85
- 230000003647 oxidation Effects 0.000 claims abstract description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 68
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 59
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 22
- 230000008569 process Effects 0.000 claims description 77
- 239000007788 liquid Substances 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 239000000126 substance Substances 0.000 claims description 25
- 239000011148 porous material Substances 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000005189 flocculation Methods 0.000 claims description 12
- 230000016615 flocculation Effects 0.000 claims description 12
- 206010021143 Hypoxia Diseases 0.000 claims description 10
- 238000003672 processing method Methods 0.000 claims description 10
- -1 heteroaryl compound Chemical class 0.000 claims description 7
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 6
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 claims description 6
- 238000006056 electrooxidation reaction Methods 0.000 claims description 5
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims description 5
- 230000004044 response Effects 0.000 claims description 4
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 3
- 150000001336 alkenes Chemical class 0.000 claims description 3
- 150000004982 aromatic amines Chemical class 0.000 claims description 3
- 150000001491 aromatic compounds Chemical class 0.000 claims description 3
- 239000004305 biphenyl Substances 0.000 claims description 3
- 235000010290 biphenyl Nutrition 0.000 claims description 3
- HBGGXOJOCNVPFY-UHFFFAOYSA-N diisononyl phthalate Chemical compound CC(C)CCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCC(C)C HBGGXOJOCNVPFY-UHFFFAOYSA-N 0.000 claims description 3
- 229920000742 Cotton Polymers 0.000 claims description 2
- 230000005518 electrochemistry Effects 0.000 claims 1
- 230000004907 flux Effects 0.000 abstract description 22
- 238000004042 decolorization Methods 0.000 abstract 1
- 238000001914 filtration Methods 0.000 description 35
- 239000000047 product Substances 0.000 description 33
- 239000010802 sludge Substances 0.000 description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 17
- 229910052760 oxygen Inorganic materials 0.000 description 17
- 239000001301 oxygen Substances 0.000 description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 230000035484 reaction time Effects 0.000 description 14
- 238000004062 sedimentation Methods 0.000 description 13
- 239000000463 material Substances 0.000 description 9
- 239000000919 ceramic Substances 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 8
- 238000001556 precipitation Methods 0.000 description 8
- 206010002660 Anoxia Diseases 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 230000026676 system process Effects 0.000 description 7
- 230000000844 anti-bacterial effect Effects 0.000 description 6
- 239000004760 aramid Substances 0.000 description 6
- 229920003235 aromatic polyamide Polymers 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000008394 flocculating agent Substances 0.000 description 6
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 6
- 235000014666 liquid concentrate Nutrition 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- 238000000909 electrodialysis Methods 0.000 description 5
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- 229920000642 polymer Polymers 0.000 description 4
- 239000006228 supernatant Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- 239000000701 coagulant Substances 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 238000009738 saturating Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000012028 Fenton's reagent Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229920002647 polyamide Polymers 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 230000009182 swimming Effects 0.000 description 2
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 description 1
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N Acrylic acid Chemical class OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 239000004695 Polyether sulfone Substances 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 238000002835 absorbance Methods 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 125000003342 alkenyl group Chemical group 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 150000001409 amidines Chemical class 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 229940088710 antibiotic agent Drugs 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 229920005601 base polymer Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- 125000000623 heterocyclic group Chemical group 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 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 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229950000845 politef Drugs 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920003229 poly(methyl methacrylate) Polymers 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229920006393 polyether sulfone Polymers 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
- 239000004926 polymethyl methacrylate Substances 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
- C02F2101/327—Polyaromatic Hydrocarbons [PAH's]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/36—Organic compounds containing halogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a treating method and device of organic wastewater and belongs to the technical field of water treatment. The treating method comprises steps as follows: step 1, the organic wastewater is subjected to biochemical treatment; step 2, effluent after biochemical treatment is subjected to oxidation and/or ultrafiltration treatment; step 3, water produced in the step 2 is treated through reverse osmosis. The organic wastewater treated with the treating method can meet the emission standard, reverse osmosis membrane effluent is high in rejection rate and color removal rate, and the flux is stable.
Description
Technical field
The present invention relates to the processing method and processing device of a kind of organic wastewater, belong to water-treatment technology field.
Background technology
The usual complicated component of organic wastewater, organic pollutant category is many, concentration is high, COD value is high and undulatory property big, particularly
The BOD5/COD value of some waste water differs greatly, and colourity is deep, and toxicity is big, solid suspension SS concentration high, seriously polluted,
Difficult.
Some treatment of Organic Wastewater main process use " pretreatment+anaerobic treatment+Aerobic Process for Treatment " at present, the dirt after process
Water also remains the heterocycle of a certain amount of difficult for biological degradation, polycyclic aromatic hydrocarbon compounds.Therefore need to increase advanced treatment process and carry out shape
Becoming high temperature, the reaction condition of high pressure, improve the quantity that free radical is formed simultaneously, reaching further mineralising Organic substance is carbon dioxide
With the purpose of inorganic ions, thus reach the emission request of national regulation.
When above-mentioned Technologies for Organic Wastewater Treatment is individually used for Sewage advanced treatment or the combination of existing wastewater processing technology,
Waste water after process all can not reach emission request, and a combination thereof is also difficult in adapt to complex chemical composition especially heterocyclic compound
The pharmacy waste water that thing is big, it is therefore necessary to the process technique for intractable organic wastewater makees further research and probe.
Summary of the invention
It is an object of the invention to: the processing method and processing device of a kind of organic wastewater that can solve high COD high chroma is provided.
Technical scheme is:
The processing method of a kind of organic wastewater, comprises the steps:
1st step, organic wastewater is carried out biochemical treatment；
2nd step, carry out the water outlet of biochemical treatment aoxidizing and/or ultra-filtration filters processes；
3rd step, the product water in the 2nd step is processed with reverse osmosis again.
The COD of described organic wastewater is between 100～20000mg/L, and colour is between 5～200.
Described organic wastewater contains obstinate COD composition that at least one is following: polycyclic aromatic hydrocarbon, heteroaryl compound, chlorination
Aromatic compounds, nitro-aromatics, aromatic amine, atomatic olefins, aromatic ester, biphenyl or organic cyanide.
Described biochemical treatment refers to A2O method.
After described biochemical treatment step, carry out solid-liquid separation process to producing water.
Described oxidation step be selected from photochemical oxidation, CWO, sonochemical oxidation, ozone high grade oxidation,
One or any several combination in electrochemical oxidation, Fenton oxidation.
The Average Pore Size of UF Membrane used in described ultrafiltration step can be 5nm～50nm, or is molecular cut off
It it is the film of 1000～200000Da.
In the step of described ultrafiltration, temperature is between 5～70 DEG C；Pressure is between 0.05～1Mpa；Crossflow velocity exists
Between 0.5～10m/s.
In the 2nd described step, refer to first use oxidation processes, then use hyperfiltration treatment.
In the 2nd described step, in producing water, need to add flocculant after the oxidising treat-ment carry out flocculation treatment.
The reverse osmosis concentrated liquid obtained in the 3rd described step returns again to process in the 2nd step, preferably by reverse osmosis concentrated
Contracting liquid is sequentially sent to oxidation, flocculation, ultrafiltration step process again after carrying out electrodialysis desalination.
The processing means of a kind of organic wastewater, includes biochemical treatment unit and reverse osmosis membrane, described biochemical treatment list
Unit is connected with reverse osmosis membrane by oxidation treatment device and/or ultrafilter membrane.
Described biochemical treatment unit passes sequentially through oxidation treatment device and is connected with reverse osmosis membrane with ultrafilter membrane.
Can also be connected on pipeline between oxidation treatment device with ultrafilter membrane and have flocculation tank, all right on flocculation tank
The adding apparatus of flocculant is installed.
The structure of biochemical treatment unit includes the anaerobic reation pool-hypoxia response pond-aerobic reaction pond being sequentially connected with.
Oxidation treatment device can use photochemical oxidation reactor, CWO reactor, sonochemical oxidation anti-
Answer one or several the group in device, ozone oxidation reaction device, electrochemical oxidation reactions device or Fenton oxidation reactor
Close.
The molecular cut off scope of ultrafilter membrane 3 can be can be 5nm in 1000～200000Da or its average pore size
～50nm.
The concentration side of reverse osmosis membrane is connected with the water inlet of oxidation treatment device.Preferably first pass through electrodialysis system, then
It is connected with the water inlet of oxidation treatment device.
Beneficial effect
The present invention process organic wastewater can make waste water reach can discharge standard, the rejection of reverse osmosis membrane water outlet simultaneously is high, color
Value clearance is high, flux stabilized.
Accompanying drawing explanation
Fig. 1 is the installation drawing used in one embodiment of the present of invention.
Wherein, 1, biochemical treatment unit；2, oxidation treatment device；3, ultrafilter membrane；4, reverse osmosis membrane；5, flocculation tank.
Detailed description of the invention
Below by detailed description of the invention, the present invention is described in further detail.But those skilled in the art will manage
Solving, the following example is merely to illustrate the present invention, and should not be taken as limiting the scope of the invention.Unreceipted concrete skill in embodiment
Art or condition person, according to the technology described by the document in this area or condition (such as with reference to Xu Nan equality write " inoranic membrane divides
From technology and application ", Chemical Industry Press, 2003) or carry out according to product description.Agents useful for same or instrument are not noted
Bright production firm person, be can by city available from conventional products.
Approximation language used herein can be used for modifying the statement of any quantity in entire disclosure and claims, and it can
Permit being changed under conditions of its relevant basic function changes being not resulted in.Therefore, such as term " about " repair
The value of decorations is not limited to specified exact value.In at least some cases, approximation language can be with the instrument for measuring this value
Precision corresponding.Unless indicated otherwise in context or statement, otherwise range limit can be combined and/or exchange, and
And this scope is confirmed as and includes all subranges contained herein.Except operation embodiment in or elsewhere
In indicate outside, the numeral of the amount of all expression compositions used in specification and claims, reaction condition etc. or
Express the modification that shall be construed as in all cases by word " about ".
The value expressed using range format should be interpreted as in a flexible way not only including clearly listing as scope
The numerical value of limit value, but also include containing all single numerical value within the range or subinterval, just as each numerical value and Zi Qu
Between be expressly recited out.Such as, the concentration range of " about 0.1% to about 5% " should be understood to not only to include clearly to list
The concentration of about 0.1% to about 5%, also includes the single concentration (e.g., 1%, 2%, 3% and 4%) in the range of indication and subinterval (example
As, 0.1% to 0.5%, 1% to 2.2%, 3.3% to 4.4%).
It should be understood that it can be direct with other elements when an element is mentioned and " is connected " with another element
It is connected or is indirectly connected to other elements, and between them, being inserted with element.Unless there are the most contrary explanation, otherwise term
" include " and " having " is interpreted as stating and comprises listed element, and non-excluded arbitrarily other elements.
Word used herein " includes ", " comprising ", " having " or its any other variant are intended to non-exclusionism
Including.Such as, including listing the technique of key element, method, article or standby being not necessarily limited by those key elements, but can be included other
It is not expressly set out or belongs to the key element that this technique, method, article or equipment are intrinsic." removal " in this specification, not only
Including removing the situation of target substance completely, also include that part removes the situation of (reducing the amount of this material).In this specification
" purify ", including removing arbitrary or specific impurity.
Waste water handled by the present invention can be any organic wastewater, wherein contains higher COD and colourity, has here
The source of machine waste water includes but not limited to: electronic industry waste water, pharmacy waste water, chemical plant's waste water, bakery and confectionery waste water etc..This
A little waste water are generally of high COD and the high feature of colourity, such as COD between 100～20000mg/L, colour 5～200 it
Between, and particularly containing many difficult for biological degradation, the composition of difficult biochemical treatment in some waste water, the method for the present invention is particularly
It is applicable to the obstinate COD composition following containing at least one: polycyclic aromatic hydrocarbon, heteroaryl compound, chlorinating aromatic compounds, nitro are fragrant
Compounds of group, aromatic amine, atomatic olefins, aromatic ester, biphenyl and organic cyanide.
Former water is processed by the technique in the present invention initially with the mode of biochemical treatment, can get rid of in waste water
The composition that a part can be bacterially decomposed.Here biological treatment is to reduce chemical oxygen demand by the biologically digesting of antibacterial
Amount (COD) and BOD (BOD) process a kind for the treatment of process of waste water.Generally, it can be divided into anaerobic processes and aeration
Process.In most cases, two kinds of processes are all applied.Biological treatment is to carry out in pond or bioreactor.In the present invention,
Biological treatment is used as the pretreatment before other operations, can be decomposed by a part of Organic substance.Preferably, in the present invention
The biological treatment used is A2O method (or referred to as A-A/O, anaerobic-anoxic-oxic).
Wherein, as the anaerobe processing means carried out a biological disposal upon of anaerobic waste water ground, as long as have
The decomposition efficiency excellence of machine thing, it is possible to use the biological reaction tank of known anaerobe processing mode.Anaerobic is raw
Thing processing means can be to carry out acid reaction of formation and 1 slot type of methane reaction of formation in same groove, it is also possible to time in difference
2 slot types of each reaction are carried out in groove.Each reactive tank can be to be the mode of swimming (alr mode), Sludge Bed mode (the heavy side of sludge filtering
Formula) etc. any-mode, furthermore it is also possible to be carrier addition type, pelletize mud type.Spy is there is no as anaerobe processing means
Not limiting, be preferably provided with acid and generate groove and the reactive tank of UASB (upflow anaerobic sludge blanket process) mode, its reason is can be high
Load running.As the oxybiotic organism processing means for anaerobe is carried out a biological disposal upon with processing water aerobism,
As long as organic decomposition efficiency excellence, it is possible to use the biological reaction tank of known oxybiotic organism processing mode.
It is for instance possible to use in groove, keep the mode of swimming of activated sludge with suspended state, to make activated sludge be attached to carrier enterprising
The biomembrane mode etc. that row keeps.It addition, fixed-bed type, fluidized bed type, expansion bed etc. can be used in biomembrane mode
Arbitrary microorganism bed mode, and carrier can use activated carbon, various plastic carrier, sponge carrier etc. any one.Carrier
Preferably sponge carrier, when being sponge carrier, can maintain microorganism in high concentration.Sponge material is not particularly limited, preferably
Ester system polyurethane.The input amount of carrier is also not particularly limited, and the generally carrier with the tankage relative to biological reaction tank is apparent
Capacity is calculated as 10～about 50%, particularly preferably 30～about 50%.Decompose as under aerobism state microbes
Organic oxybiotic organism reactive tank, it is possible to use be provided with for providing the diffuser of oxygen (air), aerator etc. in groove
Oxygen provides the aeration tank of device.Oxybiotic organism reactive tank can be 1 slot type, it is also possible to be multi-groove type, furthermore it is also possible to be
1 slot type, partition walls is set in groove.
After after biochemical treatment, by the way of conventional solid-liquid separation, the solids produced in water can be carried out
Removing (filter, sedimentation tank etc.), the most again product water is carried out oxidation processes or hyperfiltration treatment, the effect of oxidation can be decomposed
Falling the COD not being bacterially decomposed and the colourity of a part, and a part of COD also can be removed by ultrafiltration, they can realize carrying
The effect of the effluent quality of high reverse osmosis flux and raising reverse osmosis.Here oxidation processes selected from photochemical oxidation, be catalyzed wet
One or any several group in formula oxidation, sonochemical oxidation, ozone high grade oxidation, electrochemical oxidation, Fenton oxidation
Close.Water after oxidation processes is re-fed in ultrafilter membrane filtering.
After biochemical treatment, produce and water also has some antibacterials, undegradable Organic substance, colloid etc., when needs use ultrafiltration
When film processes, the phenomenon that antibacterial assembles at ultrafiltration membrane surface, grows can be there is, easily cause asking of microorganism pollution
Topic.In one embodiment, being the process simultaneously using oxidation and ultrafiltration, the product water that oxidation processes obtains enters back at ultrafiltration
Reason, logical snperoxiaized effect, the activity of antibacterial therein can be destroyed, it is to avoid the untenable problem of Pollution of Ultrafiltration Membrane, flux,
In Oxidation, destroy the structure of microbial film with the Oxidation of oxygen atom, to realize bactericidal action.
Hyperfiltration treatment described here, mainly uses ceramic super-filtering film, Average Pore Size of UF Membrane can be 5nm～
50nm, or be the film of 1000～200000Da for molecular cut off, here, owing to the aperture of ultrafilter membrane is too small and be difficult to electricity consumption
Sub-microscopes etc. measure the aperture on film surface, so it is big to replace average pore size to be used as aperture by the value of referred to as molecular cut off
Little index.About molecular cut off, as described in the textbook of this area: " will with molecular weight solute as transverse axis,
Prevention rate is the longitudinal axis, and the curve drawing data is referred to as molecular cut off curve.And by prevention rate be 90% point
Son amount is referred to as the molecular cut off of film ", molecular cut off is as the index of the film properties representing ultrafilter membrane, for people in the art
Member is known.Its filter element shape includes, Flat Membrane, tubular film, multi-channel type film, spiral membrane, hollow-fibre membrane etc., all modules
Form.As these micro-filtration membrane or the material of ultrafilter membrane, as long as being capable of granule, the suspension removing in above-mentioned alkanolamine solution
The such the object of the invention of the composition such as thing, colloid, is not particularly limited, and can enumerate: cellulose, cellulose esters, polysulfones,
Polyether sulfone, polrvinyl chloride, chloropropene, polyolefin, polyvinyl alcohol, polymethyl methacrylate, Kynoar, politef
Deng organic material, or the inorganic material such as metal or pottery such as rustless steel.The present invention use ultrafilter membrane raffinate is carried out
When filtering to remove Organic substance therein, " dead-end filtration " pattern can be used, but preferably with " cross flow filter " pattern.
The fluid separation process of " cross flow filter " form: material liquid is flow at high speed in membrane tube, containing small molecule component under pressure-driven
Penetrating fluid along direction normal thereto outwards through film, the muddy pollutant containing macromolecular components are rejected by, so that fluid
Reach separation, concentration, the purpose of purification.Thus it is guaranteed that certain cross-flow amount is the essential condition that film can normally continuously run；
When cross-flow amount is relatively low, the content of the internal impurity of film device can increase sharply, and fouling membrane speed is accelerated, and flux declines very fast；When
When cross-flow amount is higher, energy consumption can increase again, is unfavorable for energy-saving consumption-reducing.
In order to improve reduction COD and the effect of colour further, it is also possible to carried out flocculation treatment before water is produced in ultrafiltration.
For flocculant, can enumerate: high polymer coagulant, inorganic flocculating agent.As high polymer coagulant, wad a quilt with cotton as macromolecule
Solidifying agent, can list cation system, anion system, both sexes system etc., include, for example out amidine based flocculating agent, acrylamide flocculation
Agent, acrylic acid series flocculant etc.；High polymer coagulant addition in waste water preferably 10～1000ppm.As inorganic flocculation
Agent, include, for example out the ferrum system flocculant aids such as bodied ferric sulfate (concentration of iron is 5～15%), iron chloride；The aluminum such as aluminum sulfate, PAC
It it is flocculant aid etc.；Inorganic flocculating agent addition in waste water preferably 100～5000ppm.Can according to organic kind,
Characteristic, treatment situation etc. carry out suitable selection.When being condensed processing, it is added as needed on the nothing that pH regulator will be used
Machine flocculating agent adjusts to preferred pH.That is, as pH condition, for example, during ferrum system flocculating agent, it is made to react at below pH5.5
Effectively；During for aluminum system flocculating agent, it is made to adjust after reacting to pH6.0 effective above, the most preferably according to need at below pH5.0
The alkali such as the acid such as hydrochloric acid to be added, sulphuric acid or sodium hydroxide carry out pH adjustment.
After the process of oxidation or ultrafilter membrane, re-use reverse osmosis and carry out advanced treating, wherein remain for removing
COD and colour, if directly the product water after oxidation processes is carried out reverse-osmosis treated, find reverse osmosis can not fully by
Remaining COD therein and colour are removed, and cause reverse osmosis water outlet water quality bad, and easily occur that reverse osmosis membrane pollutes, leads to
The problem that amount declines.After hyperfiltration treatment, a part of COD and colour can be got rid of, additionally can improve reverse osmosis
The water quality of water outlet, and solve the problem that reverse osmosis membrane pollutes, flux is low.
As the material of reverse osmosis membrane, generally use cellulose acetate base polymer, polyamide, polyester, polyimides, second
The macromolecular materials such as alkenyl polymer.It addition, construct as it, at least side at film is had to have compacted zone, from this compacted zone
Internal to film or opposite side surface has the anisotropic membrane of the minute aperture in the aperture slowly becoming big and at this anisotropic membrane
Compacted zone on there is the composite membrane etc. of the thinnest active layer formed by other materials.Wherein, as the shape of reverse osmosis membrane
Formula, has macaroni yarn, flat film etc..Generally, it is preferred to the thickness of macaroni yarn peace film is 10 μm～1mm, the external diameter of macaroni yarn is 50 μm
～4mm.It addition, as flat film, preferably anisotropic membrane, as composite membrane preferably by substrate support such as fabric, fabric, non-woven fabrics
But film., the method for the present invention can not to be used with relying on the material of reverse osmosis membrane, membrane structure or form, for
Any one situation is the most effective.
For the concentrated solution of reverse osmosis, wherein containing more salt, its content of organics is high, and colour is high, can be by it
After being back to second pond, then sequentially pass through oxidation and/or hyperfiltration treatment.In one embodiment, the electricity in reverse osmosis concentrated liquid
Conductance 10～30ms/cm, COD is between 500～1000；In an other embodiment, electrodialysis system pair can be passed through
Reverse osmosis concentrated liquid is re-fed into second pond processing unit after carrying out desalination, can improve the filtration flux of ultrafiltration.
Based on above-mentioned method, the device that the present invention can use is as shown in Figure 1.Outlet at biochemical treatment unit 1
It is connected with reverse osmosis membrane 4 by oxidation treatment device 2 and/or ultrafilter membrane 3.The effect of biochemical treatment unit 1 is to enter waste water
Row biochemical degradation processes, the structure of biochemical treatment unit 1 can include anaerobic reation pool-hypoxia response pond of being sequentially connected with-
Aerobic reaction pond, water inlet and water outlet at reaction tank can also connect the solid-liquid separation such as preliminary sedimentation tank and second pond dress respectively
Put.Biochemical treatment unit 1 can be connected with reverse osmosis membrane 4 with ultrafilter membrane 3 by oxidation treatment device 2 respectively, it is also possible to depends on
Secondary it is connected with reverse osmosis membrane 4 again with ultrafilter membrane 4 by oxidation treatment device 2.Oxidation treatment device 2 and ultrafilter membrane 3 can
Processing the product water of biochemical treatment unit 1 respectively, the effect of reverse osmosis membrane 4 is that the product water to aforementioned means carries out the degree of depth
Except COD and colour process.
Flocculation tank 5 is had, at flocculation tank it addition, can also be connected on pipeline between oxidation treatment device 2 with ultrafilter membrane 3
The adding apparatus of flocculant it is also equipped with on 5.In another embodiment, can be further by reverse osmosis membrane 4
Concentrated solution side is connected with second pond；Can also be by the concentrated solution side of reverse osmosis membrane 4 by connecting with ultrafilter membrane again after electrodialysis plant
Connect.
It addition, oxidation treatment device 2 can use photochemical oxidation reactor, CWO reactor, sonochemistry
One in oxidation reactor, ozone oxidation reaction device, electrochemical oxidation reactions device or Fenton oxidation reactor or several
The combination planted；And the molecular cut off scope of ultrafilter membrane 3 can be can be in 1000～200000Da or its average pore size
5nm～50nm.
COD is according to China's Industry specification (Chinese Industry Code) HJ/T399-2007 " COD-quickly disappear
The water-quality determination of solution-spectrophotography " measured by COD chromium method.
Colourity is to represent faint yellow to yellow because of dissolve caused by the material being present in or be present in water with colloidal state
The degree of brown, utilizes ultraviolet-uisible spectrophotometer (UV-3100) to measure the absorbance near 390nm, by the mark of titer
Directrix curve calculates.
The fundamental property of the synthetically produced waste water of chemical intermediate processed in following example: CODCr: 1500～1600mg/L,
PH is 10～12, salinity 2～3%, BOD5/CODCrBetween 0.05 to 0.15, waste water generation amount is 50m3/ d, main in waste water
Polycyclic aromatic hydrocarbon to be contained, heteroaryl compound.
Embodiment 1
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed in entrance ceramic super-filtering film carrying out at filtration
Reason, film average pore size is 50nm, filters under different crossflow velocities, filtration temperature 35 DEG C, transmembrane pressure 0.4Mpa, film
Surface current speed 3m/s, feed liquid concentrates 8 times, and after process 100L feed liquid, the average flux of ultrafilter membrane is 43 L/m2H, ultrafilter membrane water outlet
Entering in reverse osmosis membrane and carry out filtration treatment, reverse osmosis membrane is aromatic polyamide screw type RO film, feed temperature 35 DEG C, pressure
Power 2.0Mpa, processes the average flux of feed liquid reverse osmosis of 100L at 0.4m3/m2About/d, the product water COD after process is 16.3
Mg/L, colourity is 2.
Embodiment 2
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses O3/H2O2Collaborative
Oxidation processes.Concrete reaction condition is: pH value former alkaline under the conditions of, O3And H2O2Concentration be respectively 118mg/L and
15mg/L, oxidization time is 30min, reaction temperature 30 DEG C.Product water COD after process is 145mg/L, and colourity is 51.
Oxidation is produced in water entrance ceramic super-filtering film and is carried out filtration treatment, and film average pore size is 50nm, filtration temperature 35 DEG C, across
Mould difference 0.4Mpa, crossflow velocity 3m/s, feed liquid concentrates 8 times, and after process 100L feed liquid, the average flux of ultrafilter membrane is 68 L/
m2H, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment, and reverse osmosis membrane is aromatic polyamide screw type RO
Film, feed temperature 35 DEG C, pressure 2.0Mpa, process the average flux of feed liquid reverse osmosis of 100L at 0.5m3/m2About/d, processes
After product water COD be 11.3 mg/L, colourity is 2.
Ultra-filtration process is processed by the way of employing aoxidizes by embodiment 2, antibacterial can be alleviated on film surface
Pollute, improve the flux of ultrafiltration, also further increasing the reverse osmosis rejection for COD.
Embodiment 3
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses O3/H2O2Collaborative
Oxidation processes.Concrete reaction condition is: pH value former alkaline under the conditions of, O3And H2O2Concentration be respectively 118mg/L and
15mg/L, oxidization time is 30min, reaction temperature 30 DEG C.Product water COD after process is 145mg/L, and colourity is 51.
The liquid caustic soda adding 30 wt% concentration in water water outlet is produced in oxidation, regulates pH to 8.8, and the PAM adding 5 ppm helps solidifying
Agent, waste water enters sedimentation tank and starts precipitation.After precipitation a period of time, the supernatant is pumped in ceramic super-filtering film and carry out at filtration
Reason, film average pore size is 50nm, filtration temperature 35 DEG C, transmembrane pressure 0.4Mpa, crossflow velocity 3m/s, and feed liquid concentrates 8 times, processes
After 100L feed liquid, the average flux of ultrafilter membrane is 77 L/m2H, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment,
Reverse osmosis membrane is aromatic polyamide screw type RO film, feed temperature 35 DEG C, pressure 2.0Mpa, processes the feed liquid reverse osmosis of 100L
Saturating average flux is at 0.6m3/m2About/d, the product water COD after process is 7.4 mg/L, and colourity is 1.
After water outlet for oxidation step is flocculated in embodiment 3, improve the flux of ultrafilter membrane, the most further
Improve the reverse osmosis rejection for COD.
Embodiment 4
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 3.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 40%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.2 mg/L, reaction time 4h.Product water COD after process is
230mg/L, colourity is 84.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses Fenton reagent
Carry out oxidation processes.Concrete reaction condition is: Fe in Fenton reagent2+And H2O2Concentration is respectively 120mg/L and 25mg/L,
System pH is 3, and reaction temperature is 46 DEG C, and the response time is 40min.Product water COD after process is 134mg/L, and colourity is
46。
Oxidation is produced in water entrance ceramic super-filtering film and is carried out filtration treatment, and film average pore size is 50nm, filtration temperature 35 DEG C, across
Mould difference 0.4Mpa, carries out filtration treatment under different crossflow velocities, and feed liquid concentrates 8 times, processes ultrafilter membrane after 100L feed liquid
Average flux be 68 L/m2H, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment, and reverse osmosis membrane is aromatic series
Polyamide screw type RO film, feed temperature 35 DEG C, pressure 2.0Mpa.
Embodiment 5
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses O3/H2O2Collaborative
Oxidation processes.Concrete reaction condition is: pH value former alkaline under the conditions of, O3And H2O2Concentration be respectively 118mg/L and
15mg/L, oxidization time is 30min, reaction temperature 30 DEG C.Product water COD after process is 145mg/L, and colourity is 51.
The liquid caustic soda adding 30 wt% concentration in water water outlet is produced in oxidation, regulates pH to 8.5, and the PAM adding 10 ppm helps solidifying
Agent, waste water enters sedimentation tank and starts precipitation.After precipitation a period of time, the supernatant is pumped in ceramic super-filtering film and carry out at filtration
Reason, uses the ultrafilter membrane of different film average pore sizes, filtration temperature 35 DEG C, transmembrane pressure 0.4Mpa, crossflow velocity 3m/s, feed liquid
Concentrating 8 times, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment, and reverse osmosis membrane is aromatic polyamide screw type RO
Film, feed temperature 35 DEG C, pressure 2.0Mpa.
Embodiment 6
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses O3/H2O2Collaborative
Oxidation processes.Concrete reaction condition is: pH value former alkaline under the conditions of, O3And H2O2Concentration be respectively 118mg/L and
15mg/L, oxidization time is 30min, reaction temperature 30 DEG C.Product water COD after process is 145mg/L, and colourity is 51.
The liquid caustic soda adding 30 wt% concentration in water water outlet is produced in oxidation, regulates pH to 8.8, and the PAM adding 5 ppm helps solidifying
Agent, waste water enters sedimentation tank and starts precipitation.After precipitation a period of time, the supernatant is pumped in ceramic super-filtering film and carry out at filtration
Reason, film average pore size is 50nm, filtration temperature 35 DEG C, transmembrane pressure 0.4Mpa, crossflow velocity 3m/s, and feed liquid concentrates 8 times, processes
After 100L feed liquid, the average flux of ultrafilter membrane is 77 L/m2H, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment,
Reverse osmosis membrane is aromatic polyamide screw type RO film, feed temperature 35 DEG C, pressure 2.0Mpa, processes the feed liquid reverse osmosis of 100L
Saturating average flux is at 0.6m3/m2About/d, the product water COD after process is 7.4 mg/L, and colourity is 1.
In reverse osmosis concentrated liquid, COD is at about 547mg/L, and electrical conductivity is at 14ms/cm, after returning it in second pond,
Re-use same O3/H2O2Synergistic oxidation processes and follow-up helps wadding, hyperfiltration treatment.Ultra-filtration water water quality is COD 32mg/
L, after process 5L feed liquid, the average flux of ultrafilter membrane is 53 L/m2·h。
Embodiment 7
By synthetically produced for chemical industry chemical intermediate waste water after preliminary sedimentation tank processes, then carry out aerobic-anoxia-aerobic biochemical system
Process.Aerobic biochemical pool runs in following condition: inflow temperature 30～32 DEG C, contact-oxidation pool end dissolved oxygen 2.5 mg/L,
Sludge concentration 3000mg/L, sludge settling ratio 30%, mixed-liquor return 150%, reaction time 10h；Anaerobic biological pond under
Condition of stating is run: inflow temperature 30～32 DEG C, dissolved oxygen 0.1 mg/L, reaction time 4h.Product water COD after process is
240mg/L, colourity is 89.
The product water processed, again after second pond solid-liquid separation, is re-fed into oxidation treatment device, uses O3/H2O2Collaborative
Oxidation processes.Concrete reaction condition is: pH value former alkaline under the conditions of, O3And H2O2Concentration be respectively 118mg/L and
15mg/L, oxidization time is 30min, reaction temperature 30 DEG C.Product water COD after process is 145mg/L, and colourity is 51.
The liquid caustic soda adding 30 wt% concentration in water water outlet is produced in oxidation, regulates pH to 8.8, and the PAM adding 5 ppm helps solidifying
Agent, waste water enters sedimentation tank and starts precipitation.After precipitation a period of time, the supernatant is pumped in ceramic super-filtering film and carry out at filtration
Reason, film average pore size is 50nm, filtration temperature 35 DEG C, transmembrane pressure 0.4Mpa, crossflow velocity 3m/s, and feed liquid concentrates 8 times, processes
After 100L feed liquid, the average flux of ultrafilter membrane is 77 L/m2H, ultrafilter membrane water outlet enters in reverse osmosis membrane and carries out filtration treatment,
Reverse osmosis membrane is aromatic polyamide screw type RO film, feed temperature 35 DEG C, pressure 2.0Mpa, processes the feed liquid reverse osmosis of 100L
Saturating average flux is at 0.6m3/m2About/d, the product water COD after process is 7.4 mg/L, and colourity is 1.
In reverse osmosis concentrated liquid, COD is at about 547mg/L, and electrical conductivity, at 14ms/cm, passes it through electrodialysis plant and carries out
After being back in second pond after partially desalted, re-use same O3/H2O2Synergistic oxidation processes and follow-up helps wadding, ultrafiltration
Process.Ultra-filtration water water quality is COD 27mg/L, and after process 5L feed liquid, the average flux of ultrafilter membrane is 65L/m2·h。
Claims (10)
1. the processing method of an organic wastewater, it is characterised in that comprise the steps: the 1st step, organic wastewater is carried out biochemistry
Process；2nd step, carry out the water outlet of biochemical treatment aoxidizing and/or ultra-filtration filters processes；3rd step, to the product water in the 2nd step again
Process with reverse osmosis.
The processing method of organic wastewater the most according to claim 1, it is characterised in that: the COD of described organic wastewater exists
Between 100～20000mg/L, colour is between 5～200；Described organic wastewater contains at least one following obstinate COD and becomes
Point: polycyclic aromatic hydrocarbon, heteroaryl compound, chlorinating aromatic compounds, nitro-aromatics, aromatic amine, atomatic olefins, aromatic ester,
Biphenyl or organic cyanide.
The processing method of organic wastewater the most according to claim 1, it is characterised in that: described biochemical treatment refers to A2O
Method；After described biochemical treatment step, carry out solid-liquid separation process to producing water.
The processing method of organic wastewater the most according to claim 1, it is characterised in that: described oxidation step is selected from light
One in chemical oxidation, CWO, sonochemical oxidation, ozone high grade oxidation, electrochemical oxidation, Fenton oxidation or
The combination that person is the most several.
The processing method of organic wastewater the most according to claim 1, it is characterised in that: described ultrafiltration step uses
Average Pore Size of UF Membrane can be 5nm～50nm, or is the film of 1000～200000Da for molecular cut off；Described ultrafiltration
Step in, temperature is between 5～70 DEG C；Pressure is between 0.05～1Mpa；Crossflow velocity is between 0.5～10m/s.
The processing method of organic wastewater the most according to claim 1, it is characterised in that: in the 2nd described step, refer to first use
Oxidation processes, then use hyperfiltration treatment；In the 2nd described step, in producing water, need to add flocculant after the oxidising treat-ment wad a quilt with cotton
Solidifying process.
7. the processing means of an organic wastewater, it is characterised in that include biochemical treatment unit (1) and reverse osmosis membrane (4), institute
The biochemical treatment unit (1) stated is connected with reverse osmosis membrane (4) by oxidation treatment device (2) and/or ultrafilter membrane (3).
The processing means of organic wastewater the most according to claim 7, it is characterised in that: described biochemical treatment unit (1)
Pass sequentially through oxidation treatment device (2) to be connected with reverse osmosis membrane (4) with ultrafilter membrane (3)；In oxidation treatment device (2) and ultrafiltration
Can also connect on pipeline between film (3) and have flocculation tank (5), flocculation tank (5) is also equipped with the addition of flocculant
Device；The structure of biochemical treatment unit (1) includes the anaerobic reation pool-hypoxia response pond-aerobic reaction pond being sequentially connected with.
The processing means of organic wastewater the most according to claim 7, it is characterised in that: oxidation treatment device (2) can be adopted
By light chemical oxidation reaction device, CWO reactor, sonochemical oxidation reactor, ozone oxidation reaction device, electrochemistry
One or several combination in oxidation reactor or Fenton oxidation reactor.
The processing means of organic wastewater the most according to claim 7, it is characterised in that: the molecular cut off of ultrafilter membrane (3)
Scope can be can be 5nm～50nm in 1000～200000Da or its average pore size.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610240435.2A CN105884129A (en) | 2016-04-18 | 2016-04-18 | Treating method and device of organic wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610240435.2A CN105884129A (en) | 2016-04-18 | 2016-04-18 | Treating method and device of organic wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105884129A true CN105884129A (en) | 2016-08-24 |
Family
ID=56705088
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610240435.2A Pending CN105884129A (en) | 2016-04-18 | 2016-04-18 | Treating method and device of organic wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105884129A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110563223A (en) * | 2018-07-06 | 2019-12-13 | 中石化石油工程技术服务有限公司 | process method for treating difficultly degraded COD (chemical oxygen demand) in produced water of high-sulfur-content gas field |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201817357U (en) * | 2010-06-21 | 2011-05-04 | 吴静璇 | Full-reuse treatment device for coking wastewater through Fenton oxidation and double-membrane process |
| CN102329051A (en) * | 2011-09-02 | 2012-01-25 | 陈勇 | Rubbish percolate treatment method and device by taking advanced oxidation and comprehensive membrane treatment as cores |
| CN102358651A (en) * | 2011-09-23 | 2012-02-22 | 郑州大学 | Advanced treatment process for fermented pharmaceutical waste water |
| WO2012083673A1 (en) * | 2010-12-24 | 2012-06-28 | 波鹰(厦门)科技有限公司 | Printing and dyeing wastewater treatment and reuse apparatus and method therefor |
| CN104030517A (en) * | 2013-03-06 | 2014-09-10 | 上海凯鑫分离技术有限公司 | Advanced treatment recovery technology of coking wastewater |
| CN105439395A (en) * | 2016-01-04 | 2016-03-30 | 大唐国际化工技术研究院有限公司 | Zero-discharge treatment method of salt-containing organic wastewater |
-
2016
- 2016-04-18 CN CN201610240435.2A patent/CN105884129A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201817357U (en) * | 2010-06-21 | 2011-05-04 | 吴静璇 | Full-reuse treatment device for coking wastewater through Fenton oxidation and double-membrane process |
| WO2012083673A1 (en) * | 2010-12-24 | 2012-06-28 | 波鹰(厦门)科技有限公司 | Printing and dyeing wastewater treatment and reuse apparatus and method therefor |
| CN102329051A (en) * | 2011-09-02 | 2012-01-25 | 陈勇 | Rubbish percolate treatment method and device by taking advanced oxidation and comprehensive membrane treatment as cores |
| CN102358651A (en) * | 2011-09-23 | 2012-02-22 | 郑州大学 | Advanced treatment process for fermented pharmaceutical waste water |
| CN104030517A (en) * | 2013-03-06 | 2014-09-10 | 上海凯鑫分离技术有限公司 | Advanced treatment recovery technology of coking wastewater |
| CN105439395A (en) * | 2016-01-04 | 2016-03-30 | 大唐国际化工技术研究院有限公司 | Zero-discharge treatment method of salt-containing organic wastewater |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110563223A (en) * | 2018-07-06 | 2019-12-13 | 中石化石油工程技术服务有限公司 | process method for treating difficultly degraded COD (chemical oxygen demand) in produced water of high-sulfur-content gas field |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102786183B (en) | Method for processing garbage leachate | |
| Qin et al. | Enhanced MBR by internal micro-electrolysis for degradation of anthraquinone dye wastewater | |
| CN102344227B (en) | Hairwork waste water cyclic utilization device and treatment method thereof | |
| CN104098228B (en) | A kind of organic amine wastewater treatment method | |
| CN103288309B (en) | Coal gasification wastewater zero-emission treatment method, and application thereof | |
| CN105800870A (en) | Treatment method and device for pharmaceutical wastewater | |
| CN102786182B (en) | Device for processing landfill leachate | |
| CN107253798B (en) | Advanced treatment and reuse combined process for steel industrial wastewater | |
| CN101434437B (en) | Processing method for wastewater from cephalosporin synthesis pharmaceutical production | |
| CN103265133B (en) | Recycling method of papermaking advanced treatment wastewater based on chemical decalcification | |
| CN103253838B (en) | Recycling device used for papermaking advanced treatment wastewater and based on chemical decalcification | |
| Deemter et al. | Advances in membrane separation of urban wastewater effluents for (pre) concentration of microcontaminants and nutrient recovery: a mini review | |
| CN105565581B (en) | Coal ethylene wastewater integrated conduct method | |
| Priyanka et al. | Hybrid membrane technology: an alternative to industrial wastewater treatment | |
| CN110156249A (en) | A kind of pretreated integrated approach of high-concentration printing and dyeing wastewater based on tubular membrane | |
| CN105565582A (en) | Method for treatment on sewage produced through preparation of hydrogen from coal | |
| CN207726919U (en) | A kind of Multistage Membranes composite processing system of landfill leachate | |
| Tian et al. | Hybrid process of BAC and sMBR for treating polluted raw water | |
| CN202610073U (en) | Processing apparatus of garbage percolating liquid | |
| Xu et al. | Fenton-Anoxic–Oxic/MBR process as a promising process for avermectin fermentation wastewater reclamation | |
| KR101710554B1 (en) | Method and Apparatus for treating Effluent of Sewage Treatment Plant | |
| CN220335004U (en) | Lithium iron phosphate production wastewater treatment system | |
| CN205917117U (en) | Organic waste water's processing apparatus | |
| CN112960861A (en) | Biological denitrification treatment process for stainless steel pickling wastewater | |
| CN106430846A (en) | Efficient treatment integrated process for recalcitrant wastewater with low organic matter content |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160824 |
|
| RJ01 | Rejection of invention patent application after publication |