CN109320029A - Liquor production wastewater processing method and system - Google Patents
Liquor production wastewater processing method and system Download PDFInfo
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- CN109320029A CN109320029A CN201811523788.9A CN201811523788A CN109320029A CN 109320029 A CN109320029 A CN 109320029A CN 201811523788 A CN201811523788 A CN 201811523788A CN 109320029 A CN109320029 A CN 109320029A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 109
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 30
- 238000003672 processing method Methods 0.000 title claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000000126 substance Substances 0.000 claims abstract description 29
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 28
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 24
- 239000011574 phosphorus Substances 0.000 claims abstract description 24
- 230000007062 hydrolysis Effects 0.000 claims abstract description 22
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 22
- 238000004062 sedimentation Methods 0.000 claims abstract description 22
- 230000001112 coagulating effect Effects 0.000 claims abstract description 18
- 239000002957 persistent organic pollutant Substances 0.000 claims abstract description 18
- 238000004042 decolorization Methods 0.000 claims abstract description 17
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 16
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims abstract description 14
- 229920002521 macromolecule Polymers 0.000 claims abstract description 13
- 239000002245 particle Substances 0.000 claims abstract description 13
- 239000002244 precipitate Substances 0.000 claims abstract description 7
- 125000004122 cyclic group Chemical group 0.000 claims abstract description 6
- 230000000593 degrading effect Effects 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 41
- 239000002131 composite material Substances 0.000 claims description 17
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims description 17
- 238000011068 loading method Methods 0.000 claims description 15
- 238000005868 electrolysis reaction Methods 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 230000003750 conditioning effect Effects 0.000 claims description 10
- 230000009189 diving Effects 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 10
- 239000010802 sludge Substances 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 238000001556 precipitation Methods 0.000 claims description 9
- 239000000701 coagulant Substances 0.000 claims description 8
- 230000020477 pH reduction Effects 0.000 claims description 8
- 230000001376 precipitating effect Effects 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 239000002893 slag Substances 0.000 claims description 5
- 206010021143 Hypoxia Diseases 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 3
- 230000007954 hypoxia Effects 0.000 claims description 3
- 239000010812 mixed waste Substances 0.000 claims description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims 2
- 229910052742 iron Inorganic materials 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 19
- 231100000719 pollutant Toxicity 0.000 abstract description 19
- 150000003384 small molecules Chemical class 0.000 abstract description 13
- 239000000356 contaminant Substances 0.000 abstract description 9
- 239000007787 solid Substances 0.000 abstract description 6
- 230000015556 catabolic process Effects 0.000 abstract description 3
- 238000006731 degradation reaction Methods 0.000 abstract description 3
- 238000002306 biochemical method Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 27
- 239000000243 solution Substances 0.000 description 7
- 239000006228 supernatant Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 230000031018 biological processes and functions Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- 238000012797 qualification Methods 0.000 description 2
- 235000020097 white wine Nutrition 0.000 description 2
- 229910017112 Fe—C Inorganic materials 0.000 description 1
- AMQJEAYHLZJPGS-UHFFFAOYSA-N N-Pentanol Chemical compound CCCCCO AMQJEAYHLZJPGS-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 238000013124 brewing process Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 239000005446 dissolved organic matter Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 208000014451 palmoplantar keratoderma and congenital alopecia 2 Diseases 0.000 description 1
- 238000000053 physical method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 235000014101 wine Nutrition 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/46104—Devices therefor; Their operating or servicing
-
- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
- C02F2103/325—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of wine products
-
- 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
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—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)
- Water Treatment By Electricity Or Magnetism (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
A kind of liquor production wastewater processing method and system, belong to technical field of waste water processing range, carry out water quality and quantity adjusting after the solid pollutant using the bulky grain in grid device removal waste water；Then the macromolecular substances and cyclic annular difficult decomposed substance removed in waste water are electrolysed after being thoroughly mixed hydrolysis；Pass through the organic pollutant in UASB reactor degrading waste water, A again2O reactor removes nitrogen, phosphorus and the organic pollutant in waste water and precipitates removal；Last ozone decolorization, coagulating sedimentation go in water removal that standard water discharge is discharged after phosphorus and tiny particles content.The present invention is first by the contaminant degradation for decomposing the hardly possible such as macromolecule contaminant and ring molecule after the bulky grain solid pollutant removal in liquor production wastewater at labile small-molecule substance, then use biochemical method by the pollutant removals such as small-molecule substance and nitrogen, phosphorus, using targeted mode multistep treatment, effectively remove the pollutant in waste water finally, standard water discharge discharge.
Description
Technical field
The present invention relates to a kind of wastewater treatment method and systems, and in particular to a kind for the treatment of method of liquor production wastewater and
System belongs to technical field of waste water processing range.
Background technique
Liquor production wastewater is originated from generated distillation bottom pot water, flushing water, fermentation vat leakage water, underground in brewing process
Wine library percolating water and fermentation vat blind drainage etc., COD, BOD and SS concentration with higher, ingredient are multiple in liquor production wastewater
It is miscellaneous, it mainly contains low-carbon alcohols (ethyl alcohol, butanol, amylalcohol etc.), fatty acid, the substances such as amino acid, is a kind of high concentration in acidity
Organic wastewater.In short, suspended matter, organic pollutant are dense relatively high in liquor production wastewater, in acidity, processing difficulty is larger,
Serious pollution can be brought to receiving environment if without processing direct emission.
Treatment method of liquor production wastewater mainly includes materialization, chemistry, biochemical processing method, for example coagulant sedimentation,
Membrane separation process, active carbon adsorption, chemical oxidization method, anaerobic biological process and aerobe method etc..Coagulant sedimentation effectively removes
Suspended matter in waste water, but a large amount of sludge is generated, and single technique is difficult to make standard water discharge, also need other techniques to cooperate；And film
The physico-chemical process such as partition method and activated carbon adsorption have preferable removal effect to SS, dissolved organic matter in waste water, but build and transport
It is very high to seek cost, and cleaning process is checked, operation difficulty is big；Chemical oxidization method can decompose complicated oxidation operation difficult to degrade
At can or degradable small organic molecule, but reagent cost is excessively high, and operating process is complicated dangerous, is unfavorable for promoting the use；Detest
Oxygen bioanalysis has many advantages, such as high load capacity, low energy consumption and the energy recovery section energy, and aerobe method processing can be greatly lowered
COD and BOD in waste water5, but phosphate removal is acted on limited.Phosphate is the sensitive pollutant of domestic many rivers at present
Index needs to develop a kind for the treatment of process that can efficiently reduce phosphorus in liquor production wastewater, nitrogen concentration.
It is entitled " a kind of distillery's high concentrated organic wastewater waste water treatment process " such as application number CN201310568525.0
Patent of invention a kind of distillery's high concentrated organic wastewater waste water treatment process and device are disclosed, belong to white wine field wastewater treatment
Technical field.The following steps are included: high-concentration waste water is preprocessed, enters comprehensive wastewater conditioning tank after pre-acidified, Anaerobic Treatment；
Low concentration wastewater is preprocessed, enters the pond CASS after filtering carries out Aerobic biological process；Treatment of Sludge.Present invention process processing effect
Fruit is stable, operating cost is lower, and process flow is simple, and occupied area is small, and investment relatively saves, and after treatment, reclamation rate reaches waste water
95% or more, really realize " zero-emission ".
For another example application number CN201310474968.3, it is entitled " at a kind of modular combination to small-sized distillery's waste water
The patent of invention of reason technical method " discloses a kind of modular combination processing technique method to small-sized distillery's waste water, is applicable in
In distillation bottom pot water and steaming grain bottom pot water waste water that processing small-sized brewery's white wine workshop generates, modular combination optimization processing is utilized
The high concentrated organic wastewater that small-sized distillery generates, specific module include materialization module, biochemical module and advanced treating module,
Middle materialization module includes filtering-adjusting-coagulation, adjusting-Fe-C micro electrolysis submodule, and biochemical module includes two-stage anaerobic sludge
Bed, SBR, hydrolysis acidification submodule, advanced treating module include activated carbon adsorption, disinfection by ultraviolet light submodule, and the present invention is not only
The effluent quality of small-sized liquor production wastewater can be improved, and convenient for management, realize automation, modularization, occupied area is small,
Operating cost is low.
Although above-mentioned file is directed to the processing technique of liquor production wastewater, but still can not effectively remove multiple in waste water
Miscellaneous pollutant, therefore, it is desired nonetheless to improve.
Summary of the invention
The present invention is directed to the problem of current liquor production wastewater processing technique, propose a kind of simple process, phosphorus,
Nitrogen high treating effect, operating cost low treatment method of liquor production wastewater and system, the pollutant in waste water is effectively gone
Except rear qualified discharge.
The present invention in order to solve the above problem used by technological means are as follows: a kind of liquor production wastewater processing method, use
Water quality and quantity adjusting is carried out after the solid pollutant of bulky grain in grid device removal waste water；Then it is thoroughly mixed electricity after hydrolyzing
Macromolecular substances and cyclic annular difficult decomposed substance in solution removal waste water；Pass through the organic contamination in UASB reactor degrading waste water again
Object, A2O reactor removes nitrogen, phosphorus and the organic pollutant in waste water and precipitates removal；Last ozone decolorization, coagulating sedimentation removal
Standard water discharge is discharged after phosphorus and tiny particles content in water.
Further, grid device is using the structure for carrying dehydration device, and the aperture of gate hole is less than 1mm, makes grid slag
Moisture content is no more than 20%.
Further, water quality and quantity adjusts water quality, the water using conditioning tank homogenizing waste water, water of the waste water in conditioning tank
The power residence time is 6-10h.
Further, it is thoroughly mixed hydrolysis and is thoroughly mixed hydrolysis acidification pool using closed, be equipped with submersible agitating in pond and fill
It sets and waste water is stirred, be thoroughly mixed waste water, waste water is not low in the hydraulic detention time being thoroughly mixed in hydrolysis acidification pool
In for 24 hours.
Further, electrolysis uses micro cell, and the composite porous layer of iron carbon is arranged in pond, and iron carbon is porous compound
Material particle size is 10-20mm, and with a thickness of 2-3m, hydraulic detention time of the waste water in the composite porous layer of iron carbon is 5-8h.
Further, UASB reactor is divided into reaction zone and settling zone, organic loading 3-9kgCOD/ (m3.d), effective water
Deep range 5-8m, up-flow speed should not be greater than 0.8m/h, settling zone hydraulic surface loading range 0.3-0.8 m3/(m2.h)。
Further, A2O reactor, which removes nitrogen, phosphorus and the organic pollutant in waste water and precipitates removal, refers to that use is detested
Mud-water separation, and the hydraulic retention of anaerobism, anoxic and aerobic each reaction zone are carried out by secondary settling tank after oxygen, anoxic and aerobic reaction
Time is respectively 1-2h, 1-3h and 5-8h；Mixed liquor flows back between aerobic reactor zone and hypoxia response area, and return current ratio of the mixed liquid is not
Less than 200%；Secondary settling tank hydraulic surface loading range is 0.8-1.5m3/(m2.h), hydraulic detention time is not less than 2h；Secondary settling tank
The residual sludge reflux between anaerobic reaction area, reflux ratio 20-100%.
Further, ozone decolorization, which refers to, generates ozone using ozone generation device, and using submersible agitating stick to mixed liquor
It is stirred, by color species oxygenolysis in mixed liquor at small-molecule substance, the hydraulic detention time in reaction is not less than
30min, O in mixed liquor before reacting3Concentration is not less than 5mg/L.
Further, coagulating sedimentation is in such a way that reaction zone and precipitating distinguish, reaction zone and settling zone volumetric ratio 1:
Inclined plate, hydraulic surface loading 1.0-2.5m is arranged in 9-15, settling zone3/(m2.h), hydraulic detention time range 1.5-2.5h；Instead
Answer area by dosing coagulant PAC and flocculant PAM to tiny particles content precipitating removal in mixed liquor, wherein the PAC added is molten
The dosage range of PAC is 1.5-3.0g/L in liquid, and the dosage range of PAM is 0.004-0.006g/L in PAM solution；Precipitating
The discharge of area's standard water discharge.
A kind of liquor production wastewater processing system, grill unit including the removal large particle being sequentially communicated, to water quality
Adjusting unit that water is adjusted is thoroughly mixed hydrolysis unit to what macromolecular substances and cyclic annular difficult decomposed substance were removed
Nitrogen, phosphorus and organic pollutant in the UASB reaction member that is removed with light electrolysis unit, to organic pollutant, removal waste water
A2O reaction member and precipitation unit, ozone decolorization unit, coagulating sedimentation unit.
Further, grill unit is equipped with dehydration device, and gate hole aperture is less than 1mm.
Further, it is thoroughly mixed in hydrolysis unit and is equipped with diving mixing device.
Further, the composite porous layer of iron carbon is provided in light electrolysis unit, the composite porous partial size of iron carbon is
10-20mm, with a thickness of 2-3m.
Further, A2O reaction member includes the reflux of anaerobic zone, anoxic zone and aerobic zone, wherein aerobic zone and anoxic zone
Connection, precipitation unit are connected to anaerobic zone reflux.
Further, ozone decolorization unit is equipped with ozone generating-device and diving mixing device.
Further, coagulating sedimentation unit includes reaction zone and settling zone, reaction zone and settling zone volumetric ratio 1:9-15, instead
Area is answered to be equipped with medicament addition device, settling zone is equipped with inclined plate.
The beneficial effects of the present invention are:
1. the present invention will first divide macromolecule contaminant and ring-type after the bulky grain solid pollutant removal in liquor production wastewater
The difficult contaminant degradation decomposed such as son at labile small-molecule substance, then using biochemical method by small-molecule substance and nitrogen,
The pollutant removals such as phosphorus effectively remove the pollutant in waste water finally, water outlet reaches using targeted mode multistep treatment
Mark discharge.
2. present invention process is simple, the removal effect of the pollutants such as phosphorus, nitrogen is obvious, and operating cost is low, is suitble to push away on a large scale
Extensively.
Detailed description of the invention
Fig. 1 is flowage structure schematic diagram of the present invention.
Specific embodiment
The following further describes the present invention with reference to the drawings.
Embodiment one
A kind of liquor production wastewater processing system, including be sequentially communicated grill unit, adjust unit, be thoroughly mixed hydrolysis unit,
Light electrolysis unit, UASB reaction member, A2O reaction member and precipitation unit, ozone decolorization unit, coagulating sedimentation unit.
Grill unit includes grid pond, and dehydration device is equipped in grid pond, and the aperture of grid gate hole is less than 1mm, waste water
Grid retains bulky grain suspended matter therein after flowing into grid pond, and dehydration device is dehydrated grid slag, makes grid slag
Moisture content is no more than 20%.
Adjusting unit includes conditioning tank, and it is 6- that grid water outlet, which enters the hydraulic detention time after conditioning tank in conditioning tank,
10h, waste water entrance is thoroughly mixed hydrolysis unit after being homogenized the water quality and quantity of waste water.
It is thoroughly mixed hydrolysis unit and is thoroughly mixed hydrolysis acidification pool to be closed, diving mixing device is provided in pond to useless
Water be sufficiently stirred being thoroughly mixed it, and hydraulic detention time of the waste water in pond is not less than for 24 hours, so that big point in waste water
The sub- abundant anaerobic hydrolysis of substance tentatively removes the macromolecular substances in waste water at small-molecule substance, makes full use of most simple
Some of the contaminants in single biological method removal waste water, reduce the pressure in subsequent processing.It, which is discharged, enters light electrolysis unit.
Light electrolysis unit includes micro cell, and the composite porous layer of iron carbon is provided in micro cell, and iron carbon is porous
Composite material particle size range is 10-20mm, thickness range 2-3m, when hydraulic retention of the waste water in the composite porous layer of iron carbon
Between range 5-8h.The macromolecular substances in waste water are fully hydrolyzed into small-molecule substance again by electrolysis, to big in waste water
Molecular substance is removed again, and iron carbon is composite porous can be by the difficult substance decomposition decomposed such as ring molecule at chain
Etc. labile substance, so that the subsequent pollutant in waste water completely removes.It, which is discharged, enters UASB reaction member.
UASB reaction member organic loading 3-9kgCOD/ (m3.d), available depth range 5-8m, up-flow speed should not be greater than
0.8m/s.Organic pollutant in waste water is carried out decomposition removal, and the biogas generated for utilizing by UASB reaction member, is useless
The pith of degradable organic pollutant in water, further improves the biodegradability of waste water.It, which is discharged, enters A2O reaction is single
Member.
A2O reaction member includes the anaerobic zone, anoxic zone and aerobic zone being sequentially communicated, and waste water is in anaerobism, anoxic and aerobic
The hydraulic detention time in area is respectively 1-2h, 1-3h, 5-8h, and aerobic zone is connected to anoxic zone reflux, and return current ratio of the mixed liquid is not small
In 200%.Precipitation unit is vertical sedimentation basin, and hydraulic surface loading range is 0.8-1.5m3/(m2.h), when hydraulic retention
Between be not less than 2h.Precipitation unit is connected to anaerobic zone reflux, and return sludge ratio range is 20-100%.It is released by anaerobic zone
Phosphorus, anoxic zone denitrogenation in waste water, aerobic zone nitrification absorb and by nitrate nitrogen be back to BOD in the removal such as anoxic zone waste water and
Nitrogen, phosphorus etc., finally carry out mud-water separation in precipitation unit, and the partial sludge of precipitation unit is back to anaerobic zone, excess sludge
The dehydration after collecting, send to have processing qualification mechanism specially dispose；Supernatant enters ozone decolorization unit.
Ozone generating-device and diving mixing device, supernatant water in ozone decolorization device are equipped in ozone decolorization unit
The power residence time is not less than 30min, O in supernatant mixed liquor before reacting3Concentration is not less than 5mg/L.Pass through diving mixing device pair
Supernatant is stirred to be mixed with ozone, and color species efficient oxidation in supernatant is resolved into small-molecule substance by ozone, is reduced
The coloration of water outlet.The water outlet of ozone decolorization unit enters coagulating sedimentation unit.
Coagulating sedimentation unit is divided into coagulating area and settling zone, and the volumetric ratio of coagulating area and settling zone is 1:9-
15, partition wall bottom is equipped with perforation tracery wall.Reagent throwing device and diving mixing device are equipped in coagulating area, throwing device is thrown
Add coagulant and flocculant so that tiny particles content in mixed liquor generates flocculation, agitating device coagulant liquid is stirred so that
Medicament is sufficiently mixed with waste water, forms flocculate.Specifically, coagulant PAC and flocculant PAM are each configured to mass fraction
For 30% and 0.2% aqueous solution, wherein PAC solution dosage range is 5-10ml/L, and PAM solution dosage range is 2-3ml/L,
Mixed liquor after coagulation enters settling zone by the perforation tracery wall of partition wall bottom.Inclined plate is arranged in settling zone, and hydraulic surface loading is
1.0-2.5m3/(m2.h), hydraulic detention time range 1.5-2.5h.It is dense that water outlet phosphorus is further decreased by coagulating sedimentation unit
Degree goes tiny particles content in water removal, and supernatant standard water discharge is discharged into receiving water body, and sludge is sent after dehydration to there is processing
Qualification mechanism specially disposes.
Above-described embodiment further relates to a kind of liquor production wastewater processing method, using big in grid device removal waste water
Water quality and quantity adjusting is carried out after the solid pollutant of grain；Then the macromolecular substances removed in waste water are electrolysed after being thoroughly mixed hydrolysis
With cyclic annular difficult decomposed substance；Pass through the organic pollutant in UASB reactor degrading waste water, A again2O reactor removes in waste water
Nitrogen, phosphorus and organic pollutant simultaneously precipitate removal；Last ozone decolorization, coagulating sedimentation go in water removal to be discharged after phosphorus and tiny particles content
Qualified discharge.
Grid device is using the structure for carrying dehydration device, and the aperture of gate hole is less than 1mm, surpasses the moisture content of grid slag not
Cross 20%.Mitigate the pressure in subsequent processing with the bulky grain pollutant in physical method removal waste water.
Water quality and quantity adjusts water quality, the water using conditioning tank homogenizing waste water, when hydraulic retention of the waste water in conditioning tank
Between be 6-10h.Make to be discharged by adjusting uniform and stable into subsequent processing unit.
Be thoroughly mixed hydrolysis and be thoroughly mixed hydrolysis acidification pool using closed, in pond equipped with diving mixing device to waste water into
Row stirring, is thoroughly mixed waste water, and waste water is in the hydraulic detention time being thoroughly mixed in hydrolysis acidification pool not less than for 24 hours.It utilizes
Part macromolecule contaminant is resolved into small-molecule substance by the characteristic of waste water itself, is reduced the cost in wastewater treatment, is also mitigated
Pressure in subsequent processing.
Electrolysis uses micro cell, and the composite porous layer of iron carbon, the composite porous partial size of iron carbon are arranged in pond
For 10-20mm, with a thickness of 2-3m, hydraulic detention time of the waste water in the composite porous layer of iron carbon is 5-8h.Pass through electrolysis
The macromolecule contaminant not hydrolyzed resolved into small-molecule substance, and difficult is decomposed by the way that iron carbon is composite porous by cyclic annular
Substance decomposition is at labile chain substance, so that the subsequent polluter in waste water completely removes.
UASB reactor is divided into reaction zone and settling zone, organic loading 3-9kgCOD/ (m3.d), available depth range 5-
8m, up-flow speed should not be greater than 0.8m/h, settling zone hydraulic surface loading range 0.3-0.8 m3/(m2.h).It is reacted by UASB
Organic pollutant in device degrading waste water.
A2Nitrogen, phosphorus and organic pollutant in O reactor removal waste water are simultaneously precipitated removal and referred to and become reconciled using anaerobism, anoxic
Pollutant, and the hydraulic detention time difference of anaerobism, anoxic and aerobic each reaction zone are removed by sedimentation in secondary sedimentation tank after oxygen reaction
For 1-2h, 1-3h and 5-8h；Mixed liquor flows back between aerobic reactor zone and hypoxia response area, and return current ratio of the mixed liquid is not less than
200%；Secondary settling tank hydraulic surface loading range is 0.8-1.5m3/(m2.h), hydraulic detention time is not less than 2h；Secondary settling tank with detest
Sludge reflux between oxygen reaction zone, reflux ratio 20-100%.Pass through A2O reactor removes nitrogen, phosphorus and the organic contamination in waste water
Object.
Ozone decolorization, which refers to, generates ozone using ozone generation device, and is stirred using submersible agitating stick to mixed liquor,
By color species oxygenolysis in mixed liquor at small-molecule substance, the hydraulic detention time in reaction is not less than 30min, before reaction
O in mixed liquor3Concentration is not less than 5mg/L.The coloration of water outlet is reduced by ozone decolorization.
Coagulating sedimentation is in such a way that reaction zone and precipitating distinguish, reaction zone and settling zone volumetric ratio 1:9-15, precipitating
Inclined plate, hydraulic surface loading 1.0-2.5m is arranged in area3/(m2.h), hydraulic detention time range 1.5-2.5h；Reaction zone passes through
Dosing coagulant PAC and flocculant PAM is to tiny particles content precipitating removal in mixed liquor, wherein PAC in the PAC solution added
Dosage range is 1.5-3.0g/L, and the dosage range of PAM is 0.004-0.006g/L in PAM solution；Settling zone water outlet reaches
Mark discharge.
From above-described embodiment as can be seen that the present invention first will be after the bulky grain solid pollutant removal in liquor production wastewater
By the difficult contaminant degradation decomposed such as macromolecule contaminant and ring molecule at labile small-molecule substance, then using biochemistry
The pollutant removals such as small-molecule substance and nitrogen, phosphorus are made the pollution in waste water using targeted mode multistep treatment by method
Object finally effectively removes, standard water discharge discharge.And present invention process is simple, the removal effect of the pollutants such as phosphorus, nitrogen is obvious, operation
It is at low cost, it is suitable for large-scale promotion.
Above embodiments are used for illustrative purposes only, rather than limitation of the present invention, the technology people in relation to technical field
Member without departing from the spirit and scope of the present invention, can also make a variety of changes or convert, therefore is all equivalent
Technical solution also should belong to protection scope of the present invention, and protection scope of the present invention should be limited by each claim.
Claims (10)
1. a kind of liquor production wastewater processing method, it is characterised in that: using consolidating for the bulky grain in grid device removal waste water
Water quality and quantity adjusting is carried out after body pollution object；Then the macromolecular substances and ring-type removed in waste water are electrolysed after being thoroughly mixed hydrolysis
Difficult decomposed substance；Pass through the organic pollutant in UASB reactor degrading waste water, A again2O reactor removes nitrogen, phosphorus in waste water
With organic pollutant and precipitate removal；Last ozone decolorization, coagulating sedimentation go in water removal standard water discharge after phosphorus and tiny particles content
Discharge.
2. liquor production wastewater processing method as described in claim 1, it is characterised in that: grid device is using included dehydration dress
The structure set, and the aperture of gate hole is less than 1mm, and the moisture content of grid slag is made to be no more than 20%；
Water quality and quantity adjusts water quality, the water using conditioning tank homogenizing waste water, and hydraulic detention time of the waste water in conditioning tank is
6-10h。
3. liquor production wastewater processing method as described in claim 1, it is characterised in that: be thoroughly mixed hydrolysis using closed
It is thoroughly mixed hydrolysis acidification pool, diving mixing device is equipped in pond and waste water is stirred, be thoroughly mixed waste water, waste water is complete
Hydraulic detention time in full mixed hydrolysis acidification pool is not less than for 24 hours.
4. liquor production wastewater processing method as described in claim 1, it is characterised in that: it is electrolysed and uses micro cell, and
Iron carbon composite porous layer is set in pond, and the composite porous partial size of iron carbon is 10-20mm, and with a thickness of 2-3m, waste water is in iron
Hydraulic detention time in the composite porous layer of carbon is 5-8h.
5. liquor production wastewater processing method as described in claim 1, it is characterised in that: UASB reactor is divided into reaction zone
And settling zone, organic loading 3-9kgCOD/ (m3.d), available depth range 5-8m, up-flow speed should not be greater than 0.8m/h, precipitates
Area hydraulic surface loading range 0.3-0.8 m3/(m2.h)。
6. liquor production wastewater processing method as described in claim 1, it is characterised in that: A2O reactor removes in waste water
Nitrogen, phosphorus and organic pollutant simultaneously precipitate removal and refer to and go to decontaminate by sedimentation in secondary sedimentation tank using after anaerobism, anoxic and aerobic reaction
Object is contaminated, and the hydraulic detention time of anaerobism, anoxic and aerobic each reaction zone is respectively 1-2h, 1-3h and 5-8h；Aerobic reactor zone
Mixed liquor flows back between hypoxia response area, and return current ratio of the mixed liquid is not less than 200%；Secondary settling tank hydraulic surface loading range is
0.8-1.5m3/(m2.h), hydraulic detention time is not less than 2h；Sludge reflux between secondary settling tank and anaerobic reaction area, reflux ratio are
20-100%。
7. liquor production wastewater processing method as described in claim 1, it is characterised in that: ozone decolorization refers to be produced using ozone
Raw device generates ozone, and is stirred using submersible agitating stick to mixed liquor, by color species oxygenolysis in mixed liquor at small
Molecular substance, the hydraulic detention time in reaction are not less than 30min, O in mixed liquor before reacting3Concentration is not less than 5mg/L；
Coagulating sedimentation is in such a way that reaction zone and precipitating distinguish, and reaction zone and settling zone volumetric ratio 1:9-15, settling zone is set
Set inclined plate, hydraulic surface loading 1.0-2.5m3/(m2.h), hydraulic detention time range 1.5-2.5h；Reaction zone is by adding
Coagulant PAC and flocculant PAM is to tiny particles content precipitating removal in mixed liquor, wherein PAC is added in the PAC solution added
Amount range is 1.5-3.0g/L, and the dosage range of PAM is 0.004-0.006g/L in PAM solution；Settling zone standard water discharge row
It puts.
8. a kind of liquor production wastewater processing system, it is characterised in that: including the grid list for the removal large particle being sequentially communicated
Member, the adjustings unit that water quality and quantity is adjusted mix completely to what macromolecular substances and cyclic annular difficult decomposed substance were removed
Close hydrolysis unit and light electrolysis unit, the UASB reaction member that organic pollutant is removed, the nitrogen in removal waste water, phosphorus and
The A of organic pollutant2O reaction member and precipitation unit, ozone decolorization unit, coagulating sedimentation unit.
9. liquor production wastewater processing system as claimed in claim 8, it is characterised in that: grill unit is equipped with dehydration device,
Gate hole aperture is less than 1mm；
It is thoroughly mixed in hydrolysis unit and is equipped with diving mixing device；
The composite porous layer of iron carbon is provided in light electrolysis unit, the composite porous partial size of iron carbon is 10-20mm, with a thickness of
2-3m；
A2O reaction member includes anaerobic zone, anoxic zone and aerobic zone, and wherein aerobic zone be connected to anoxic zone reflux, precipitation unit with
Anaerobic zone reflux connection.
10. liquor production wastewater processing system as claimed in claim 8, it is characterised in that: ozone decolorization unit is equipped with ozone
Generating device and diving mixing device；
Coagulating sedimentation unit includes reaction zone and settling zone, and reaction zone and settling zone volumetric ratio 1:9-15, reaction zone are equipped with medicament
Throwing device, settling zone are equipped with inclined plate.
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