CN114105415A - Pretreatment method and system for brewing yellow water - Google Patents
Pretreatment method and system for brewing yellow water Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 238000002203 pretreatment Methods 0.000 title claims description 14
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 151
- 230000003647 oxidation Effects 0.000 claims abstract description 145
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 129
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims abstract description 99
- 239000010802 sludge Substances 0.000 claims abstract description 98
- 239000002351 wastewater Substances 0.000 claims abstract description 85
- 230000002195 synergetic effect Effects 0.000 claims abstract description 82
- 235000014101 wine Nutrition 0.000 claims abstract description 29
- 239000000945 filler Substances 0.000 claims abstract description 27
- 230000003197 catalytic effect Effects 0.000 claims abstract description 26
- 238000005273 aeration Methods 0.000 claims abstract description 23
- 238000011049 filling Methods 0.000 claims abstract description 8
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- 238000000926 separation method Methods 0.000 claims description 140
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- 239000007788 liquid Substances 0.000 claims description 115
- 239000006228 supernatant Substances 0.000 claims description 90
- 238000005189 flocculation Methods 0.000 claims description 11
- 230000016615 flocculation Effects 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 9
- 238000006385 ozonation reaction Methods 0.000 claims description 8
- 238000000265 homogenisation Methods 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 3
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- 239000000203 mixture Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 38
- 239000003344 environmental pollutant Substances 0.000 abstract description 10
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- 238000012545 processing Methods 0.000 abstract description 5
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- 229910052698 phosphorus Inorganic materials 0.000 description 15
- 239000011574 phosphorus Substances 0.000 description 15
- 238000005868 electrolysis reaction Methods 0.000 description 13
- 238000004065 wastewater treatment Methods 0.000 description 11
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- 239000000126 substance Substances 0.000 description 7
- 230000015556 catabolic process Effects 0.000 description 6
- 238000006731 degradation reaction Methods 0.000 description 6
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- 239000000292 calcium oxide Substances 0.000 description 5
- 238000011161 development Methods 0.000 description 5
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- 238000001514 detection method Methods 0.000 description 4
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- 238000011514 vinification Methods 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
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- 239000012028 Fenton's reagent Substances 0.000 description 2
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- 125000003118 aryl group Chemical group 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- MKJXYGKVIBWPFZ-UHFFFAOYSA-L calcium lactate Chemical compound [Ca+2].CC(O)C([O-])=O.CC(O)C([O-])=O MKJXYGKVIBWPFZ-UHFFFAOYSA-L 0.000 description 2
- 229960002401 calcium lactate Drugs 0.000 description 2
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 235000019606 astringent taste Nutrition 0.000 description 1
- 230000000975 bioactive effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
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- 238000010438 heat treatment Methods 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000011218 seed culture Methods 0.000 description 1
- 235000019614 sour taste Nutrition 0.000 description 1
- 235000015096 spirit Nutrition 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000001648 tannin Substances 0.000 description 1
- 229920001864 tannin Polymers 0.000 description 1
- 235000018553 tannin Nutrition 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 235000020097 white wine Nutrition 0.000 description 1
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- 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
- C02F1/52—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
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/18—PO4-P
-
- 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
Abstract
The invention discloses a method and a system for pretreating yellow wine brewing water, wherein the method comprises the following steps: (1) carrying out iron-carbon/ozone synergistic oxidation treatment; (2) anaerobic biochemical treatment; (3) carrying out catalytic oxidation advanced treatment by ozone; in the step 1, the operation of the iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to be acidic into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment of wastewater. This application can carry out the preliminary treatment to this kind of making wine yellow water, and yellow water after the preliminary treatment can satisfy the requirement of intaking of the current processing system of brewing factory, and waste water after this application preliminary treatment can get into the current processing system of brewing factory and carry out biochemical treatment, then discharge up to standard. The method can effectively solve the problems, remarkably reduce the generation amount of sludge, reduce the treatment cost of the secondary pollutants in the yellow water, and has remarkable progress significance.
Description
Technical Field
The application relates to the technical field of wastewater treatment, in particular to a method and a system for pretreating brewing yellow water. The application makes the refractory organic matters in the yellow water fully degraded through the pretreatment of the brewing yellow water, so as to meet the treatment requirement of a subsequent biochemical system of a winery, has the characteristics of short process flow, less sludge production and low treatment cost, can effectively reduce the treatment cost of the winery yellow water, and has remarkable economic value and practical value.
Background
The yellow water is a byproduct at the bottom of a pit in the traditional strong aromatic Chinese spirits fermentation process, is a yellow brown viscous liquid, and has sour and astringent taste. The yellow water contains not only alcohols, acids, aldehydes, esters, etc., but also beneficial microorganisms domesticated in a specific environment in a cellar for a long time, sugar substances, nitrogen-containing compounds, etc., and a small amount of tannin, pigment, fragrance-producing precursor substances, etc.
At present, the domestic methods for brewing yellow water by using white spirit mainly comprise the following steps: 1) precipitating, filtering, decolorizing yellow water, and directly flavoring; 2) mixing yellow water, wine lees, Daqu powder and edible alcohol in proportion, and steaming to extract fragrance; 3) (ii) a Esterifying yellow water by biological enzyme esterification technology, converting organic acid and other components into mixed liquor of ester and other white wine flavor components, and distilling the prepared esterified liquor in series for flavor extraction and cellaring to improve the content of flavor substances in the base wine; 4) and (5) using the yellow water for maintaining the pit.
The yellow water has a recycling value, but due to the problems of economic cost and technical defects, the yellow water cannot be fully recycled, and the yellow water which is not recycled still needs to be subjected to advanced treatment, so that the pollution problem of the yellow water is thoroughly solved. Yellow water contains abundant organic acid, reducing sugar, yeast autolysate and the like, so that the COD of the yellow water is as high as tens of thousands or even hundreds of thousands.
The winery is usually built with a biochemical treatment system for treating low-concentration wastewater for wine making in the winery. If the yellow water and the brewing low-concentration wastewater are directly sent into a biochemical treatment system, the demand of the brewing low-concentration wastewater is greatly increased, so that the wastewater treatment cost is too high, and by adopting the mode, the refractory organic matters in the yellow water cannot be effectively degraded, and the normal operation of the biochemical system can be influenced.
At present, few patent documents are disclosed for the treatment of yellow water. For example, the chinese patent application CN98121895.4 discloses a method for extracting calcium lactate from brewery wastewater, which comprises adding 5-15% yellow water into the brewery wastewater, mixing uniformly, fermenting for 3-5 days at 40-55 ℃; adding lime water for neutralization and sedimentation, and then filtering; heating and concentrating the clear liquid, stirring and crystallizing to obtain calcium lactate.
Chinese patent application CN201210169681.5 discloses a process for biologically degrading yellow water in a liquor factory, which takes aspergillus oryzae as an initial strain to carry out test tube amplification culture, liquid shake culture, primary seed culture and yellow water degradation, the degraded wastewater is centrifuged to obtain aspergillus oryzae mycelia, and the filtrate is subjected to molecular interception to obtain various bioactive molecules.
How to reduce the treatment cost of the yellow water is always the key point of research of people, and the method has important significance for the sustainable development of the strong aromatic white spirit. Therefore, the application provides a method and a system for pretreating brewing yellow water.
Disclosure of Invention
The yellow water has the characteristics of high acid, high chemical oxygen demand, high ammonia nitrogen and high total phosphorus. If the yellow water is directly discharged into a sewage treatment station and treated with other low-concentration wine-making wastewater, the treatment difficulty of the wastewater can be greatly increased, and the resource waste is caused. Therefore, the yellow water must be pretreated separately to the acceptable limit of the conventional wastewater treatment process and then treated together with other wastewater in the wine industry.
The invention of the present application aims to: the method and the system for pretreating the yellow water for brewing wine are provided aiming at the characteristics that the yellow water has high acid, high chemical oxygen demand, high ammonia nitrogen and high total phosphorus, and if the untreated yellow water and other low-concentration wastewater for brewing wine are treated together, the treatment difficulty of the wastewater is greatly increased, and the problem of resource waste is caused. This application can carry out the preliminary treatment to this kind of making wine yellow water, and yellow water after the preliminary treatment can satisfy the requirement of intaking of the current processing system of brewing factory, and waste water after this application preliminary treatment can get into the current processing system of brewing factory and carry out biochemical treatment, then discharge up to standard. The method can effectively solve the problems, remarkably reduce the generation amount of sludge, reduce the treatment cost of the secondary pollutants in the yellow water, and has remarkable progress significance. The method has the advantages of reasonable process and short treatment flow, can greatly reduce the integral treatment cost of the yellow water, has obvious economic value and application value, and is worthy of large-scale popularization and application.
In order to achieve the purpose, the following technical scheme is adopted in the application:
a pretreatment method of brewing yellow water comprises the following steps:
(1) iron-carbon/ozone co-oxidation treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to be acidic; then carrying out iron-carbon/ozone synergistic oxidation treatment for 3-6 h, and adjusting the pH value to be alkalescent to obtain a first mixed solution; centrifuging the first mixed solution to obtain a first supernatant;
in the step 1, the operation of the iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to be acidic into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment on wastewater;
(2) anaerobic biochemical treatment
Mixing the brewing low-concentration wastewater with the first supernatant obtained in the step (1) according to a set proportion, and diluting the first supernatant through the brewing low-concentration wastewater to obtain a second mixed solution; feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4-6 days to obtain a third mixed solution;
carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant;
(3) catalytic oxidation advanced treatment by ozone
Adjusting the pH value of the third supernatant to be alkalescent to obtain a fourth mixed solution; treating the fourth mixed solution for 6-10 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution;
and carrying out mud-water separation on the fifth mixed solution to obtain a fifth supernatant, and finishing the pretreatment operation of the yellow water.
In the step 1, after the yellow water to be treated is sent into a pre-adjusting tank for homogenizing and uniform treatment, the pH value is adjusted to 3-4; after the iron-carbon/ozone synergistic oxidation treatment is carried out for 3 hours, the pH value is adjusted to 8-9, and a first mixed solution is obtained; centrifuging the first mixed solution to obtain a first supernatant;
in the step 1, the operation of the iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to 3-4 into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment of wastewater.
And respectively feeding the first precipitated sludge generated by the centrifugal separation of the first mixed liquid, the third precipitated sludge generated by the centrifugal separation of the third mixed liquid and the fifth precipitated sludge generated by the mud-water separation of the fifth mixed liquid into a sludge collection tank for collection.
In the step 1, sulfuric acid is adopted to adjust the pH value to 3-4, and the rotation speed of centrifugal separation is 1000-5000 rad/min.
And in the step 2, performing centrifugal separation on the third mixed solution to respectively obtain a third supernatant and third precipitated sludge.
And in the step 3, adjusting the pH value of the third supernatant to 8-9 by using quicklime.
And in the step 3, adding an ozone catalyst into the fourth mixed solution, and introducing ozone for ozone catalytic oxidation treatment for 6 hours to obtain a fifth mixed solution.
The ozone catalyst is one or more of ferrous iron and ferric iron.
And in the step 3, performing sludge-water separation on the fifth mixed solution by adopting one or more of flocculation precipitation and filter pressing, and respectively obtaining a fifth supernatant and fifth precipitated sludge.
And in the step 3, sequentially adding PAC and PAM into the fifth mixed solution, and precipitating for 2h to respectively obtain a fifth supernatant and fifth precipitated sludge.
And in the step 3, sending the fifth supernatant into a biochemical treatment system for biochemical treatment.
In the step 3, after the pH value of the third supernatant is adjusted to 8-9, a fourth mixed solution is obtained; and treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution.
A wine yellow water pretreatment system, comprising:
the pre-adjusting tank is used for carrying out homogenizing and quantity-equalizing treatment on the fed yellow water to be treated;
the first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4;
the iron-carbon/ozone synergistic oxidation treatment unit is connected with the first pH value adjusting tank and is used for carrying out iron-carbon/ozone synergistic oxidation treatment on the yellow water with the pH value adjusted to 3-4;
the second pH value adjusting tank is connected with the iron carbon/ozone synergistic oxidation treatment unit and is used for adjusting the pH value of the liquid obtained by iron carbon/ozone synergistic oxidation treatment back to 8-9 to obtain a first mixed liquid;
the first centrifuge is connected with the second pH value adjusting tank and is used for carrying out centrifugal separation on the first mixed solution to respectively obtain a first supernatant and first precipitated sludge;
the anaerobic unit is connected with the first centrifugal machine, and after the first supernatant produced by the first centrifugal machine and the brewing low-concentration wastewater are mixed in the anaerobic unit according to a set proportion, anaerobic biochemical treatment can be carried out to obtain a third mixed solution;
the third solid-liquid separation tank is connected with the anaerobic unit, and the third mixed solution is subjected to solid-liquid separation in the third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively;
the fourth pH value adjusting tank is connected with the third solid-liquid separation tank, and third supernatant obtained by separation in the third solid-liquid separation tank can be sent into the fourth pH value adjusting tank to adjust the pH value to 8-9, so that fourth mixed liquid is obtained;
the fourth ozone oxidation tank is connected with the fourth pH value adjusting tank, and the fourth mixed solution can be subjected to catalytic ozonation treatment in the fourth ozone oxidation tank to obtain a fifth mixed solution;
the fifth solid-liquid separation tank is connected with the fourth ozone oxidation tank, and the fifth mixed liquid can be subjected to mud-water separation in the fifth solid-liquid separation tank to obtain a fifth supernatant and fifth precipitated sludge respectively;
the sludge collection tank is respectively connected with the first centrifugal machine, the third solid-liquid separation tank and the fifth solid-liquid separation tank, and first precipitated sludge generated by the first centrifugal machine, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected;
the iron-carbon/ozone synergistic oxidation treatment unit comprises a synergistic oxidation pond, iron-carbon fillers and an ozone aeration device, wherein the iron-carbon fillers are arranged in the synergistic oxidation pond, an ozone generation port of the ozone aeration device is arranged below the iron-carbon fillers, and ozone generated by the ozone aeration device can replace air and the iron-carbon fillers to carry out iron-carbon/ozone synergistic treatment on wastewater.
The fifth solid-liquid separation tank is a flocculation sedimentation tank.
In order to solve the problems, the application provides a method and a system for pretreating wine-making yellow water. The pretreatment method comprises the following steps: iron carbon/ozone synergistic oxidation treatment, anaerobic biochemical treatment and ozone catalytic oxidation advanced treatment.
Further, the inventors explain the working process of the present application as follows.
In the application, firstly, high-concentration refractory yellow water to be treated is sent into a pre-regulating tank for homogenizing and uniform treatment, so that the hydraulic power and pollutant load of a subsequent treatment system are reduced, and the running stability of the system is improved; more specifically, the pre-adjusting tank utilizes the adjusting tank with a certain storage volume to temporarily store the incoming water, so that the influence of the quality and quantity fluctuation of the incoming water on the system is avoided. And (4) after homogenizing and quantity-balancing adjustment is carried out on the wastewater, adjusting the pH value to 3-4. And then carrying out iron-carbon/ozone synergistic oxidation treatment on the wastewater with the pH value adjusted to 3-4 for 3h (in the process, the wastewater with the pH value adjusted to acidity is added into an iron-carbon micro-electrolysis reaction device, ozone is utilized for aeration for 3h to remove COD in the wastewater), and then adjusting the pH value to 8-9 to obtain a first mixed solution. And centrifuging the first mixed solution to obtain a first supernatant.
And (2) mixing the brewing low-concentration wastewater with the first supernatant obtained in the step (1) according to a set proportion, and diluting the first supernatant through the brewing low-concentration wastewater to obtain a second mixed solution. The process adds the brewing low-concentration wastewater with a set proportion, so that the purpose of reducing the sewage concentration can be achieved, the biodegradability of the sewage can be improved, and the subsequent anaerobic biochemical treatment efficiency can be improved. And (4) feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4 days to obtain a third mixed solution. And carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant. The step can effectively remove COD, ammonia nitrogen and TP in the wastewater; and (4) performing solid-liquid separation on the anaerobic effluent by using a centrifugal machine at the rotating speed of 3000rad/min, and sending the first supernatant obtained by centrifugal separation to the next step.
And finally, adjusting the pH value of the third supernatant to be alkalescent to obtain a fourth mixed solution. And treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution. This application adopts ozone catalytic oxidation technology to handle the third supernatant at last, further gets rid of pollutants such as remaining COD in the waste water, realizes reducing waste water COD, ammonia nitrogen and TP's purpose. The wastewater pretreated by the method can meet the pretreatment requirement and can be treated together with other low-concentration brewing wastewater. The method can not comprise a sludge treatment system, and the sludge is discharged to other wine-making wastewater sludge treatment systems to be treated together, so that the investment and the operation cost are reduced.
The pretreatment method of the invention is adopted to pretreat the yellow wine brewing water, and can effectively solve the problem that the wastewater has high COD and TP and is difficult to be treated together with other low-concentration wine brewing wastewater. Finally, the wastewater pretreated by the method can be sent to the existing treatment system of the brewhouse for biochemical treatment, and finally reaches the discharge standard, thereby meeting the requirements of sustainable development.
In summary, due to the adoption of the technical scheme, the invention has the beneficial effects that:
(1) the advanced oxidation method is the most effective method for treating high-concentration refractory organic wastewater at present, but has relatively high treatment cost and is mainly suitable for the following working conditions: pretreating high-concentration and small-water-volume degradation-resistant organic wastewater; advanced treatment of low-concentration organic wastewater difficult to biodegrade; the anaerobic oxidation method is the most economic method for treating high-concentration degradable organic wastewater which is acknowledged at present, but the effect of removing the organic pollutants which are difficult to degrade is not obvious; therefore, according to earlier experimental results and similar engineering experiences, the iron-carbon oxidation process and the ozone oxidation process are combined synergistically for the first time, so that the operation cost is greatly reduced on the premise of meeting the requirement of treating high-concentration refractory organic wastewater, and the treatment effect of 1+1 & gt 2 is achieved;
(2) according to the method, the advanced oxidation, anaerobic treatment and advanced oxidation advanced treatment are adopted, so that pollutants such as COD (chemical oxygen demand), ammonia nitrogen, total phosphorus and the like in the wastewater are effectively removed, and a guarantee is provided for mixed treatment with other brewing wastewater; on one hand, the method utilizes an advanced oxidation means to oxidize refractory macromolecular substances in the wastewater into micromolecular substances, so that the stable and efficient operation of an anaerobic system is ensured; on the other hand, high-concentration organic matters in the wastewater are removed by metabolism by an anaerobic biological treatment process; finally, further removing COD in the wastewater by using an advanced oxidation means;
(3) the method adopts 'multi-stage gradient' treatment on COD in the brewing wastewater, ensures the stability and safety of the operation of the whole process system, and fully ensures that effluent meets the requirement of pretreated effluent;
(4) by adopting the method, the high-concentration and difficult-to-degrade yellow water can be pretreated, the low-concentration wastewater treatment system can receive water quality, and the minimization of treatment cost is realized while the effective treatment of wastewater is realized;
(5) the application can effectively reduce COD, ammonia nitrogen and total phosphorus in the wastewater, increase environmental benefits, solve the problem of pollutant discharge such as brewing yellow water COD, can also provide reference for the treatment of other similar high-concentration refractory organic wastewater, and meet the requirements of sustainable development.
Drawings
FIG. 1 is a process flow diagram of the present invention.
The labels in the figure are: 1. the system comprises a pre-adjusting tank, 2, a first pH value adjusting tank, 3, an iron-carbon/ozone synergistic oxidation treatment unit, 4, a second pH value adjusting tank, 5, a first centrifugal machine, 6, an anaerobic unit, 7, a third solid-liquid separation tank, 8, a fourth pH value adjusting tank, 9, a fourth ozone oxidation tank, 10, a fifth solid-liquid separation tank, 11 and a sludge collecting tank.
Detailed Description
All of the features disclosed in this specification, or all of the steps in any method or process so disclosed, may be combined in any combination, except combinations of features and/or steps that are mutually exclusive.
The following description of the embodiments of the present invention is provided to facilitate the understanding of the present invention by those skilled in the art, but it should be understood that the present invention is not limited to the scope of the embodiments, and it will be apparent to those skilled in the art that various changes may be made without departing from the spirit and scope of the invention as defined and defined in the appended claims, and all matters produced by the invention using the inventive concept are protected.
Example 1
The embodiment provides a pretreatment system for yellow wine water, which comprises a pre-adjusting tank, an iron carbon/ozone synergistic oxidation assembly, an anaerobic assembly and a deep treatment assembly. The pre-adjusting tank is used for carrying out homogeneous and uniform treatment on the fed yellow water to be treated, so that the hydraulic power and impact load of a subsequent treatment system are effectively reduced, and the normal and stable operation of the system is ensured.
The iron carbon/ozone cooperative oxidation assembly comprises a first pH value adjusting tank, an iron carbon/ozone cooperative oxidation treatment unit, a second pH value adjusting tank and a first centrifuge. The first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4; the iron-carbon/ozone synergistic oxidation treatment unit comprises a synergistic oxidation pond, iron-carbon fillers and an ozone aeration device, wherein the iron-carbon fillers are arranged in the synergistic oxidation pond, an ozone generation port of the ozone aeration device is arranged below the iron-carbon fillers, and ozone generated by the ozone aeration device can replace air and the iron-carbon fillers to carry out iron-carbon/ozone synergistic treatment on wastewater; the first pH value adjusting tank is connected with the synergistic oxidation tank and is used for carrying out iron-carbon/ozone synergistic oxidation treatment on the yellow water with the pH value adjusted to 3-4; the cooperative oxidation tank is connected with the second pH value adjusting tank and is used for adjusting the pH value of the liquid obtained by iron-carbon/ozone cooperative oxidation treatment to 8-9 and obtaining a first mixed liquid; and the first centrifugal machine is connected with the second pH value adjusting tank and is used for carrying out centrifugal separation on the first mixed liquor to respectively obtain first supernatant and first precipitated sludge. Adopt aforementioned structure, carry out handles such as pH regulation, iron carbon/ozone collaborative oxidation, pH recall, solid-liquid separation to making wine yellow water in proper order, can degrade macromolecule refractory organic matter in the yellow water into micromolecular organic matter, improve waste water biodegradability, provide the advantage for follow-up anaerobism unit, ensure the abundant effective degradation of pollutant.
The anaerobic component comprises an anaerobic unit and a third solid-liquid separation tank; the anaerobic unit is connected with the first centrifugal machine, and the third solid-liquid separation tank is connected with the anaerobic unit. In this embodiment, after the first supernatant produced by the first centrifuge and the low-concentration brewing wastewater are mixed in the anaerobic unit according to a volume ratio of 1:10, anaerobic biochemical treatment can be performed, and a third mixed solution is obtained. And performing solid-liquid separation on the third mixed solution by using a third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively. By adopting the step, most degradable organic pollutants in the wastewater are removed.
The advanced treatment component comprises a fourth pH value adjusting tank, a fourth ozone oxidation tank and a fifth solid-liquid separation tank. The fourth pH value adjusting tank is connected with the third solid-liquid separation tank, the fourth ozone oxidation tank is connected with the fourth pH value adjusting tank, and the fifth solid-liquid separation tank is connected with the fourth ozone oxidation tank. Sending a third supernatant obtained by separation in the third solid-liquid separation tank into a fourth pH value adjusting tank, adjusting the pH value to 8-9, and obtaining a fourth mixed solution; carrying out catalytic ozonation treatment on the fourth mixed solution in a fourth ozonation tank to obtain a fifth mixed solution; and carrying out sludge-water separation on the fifth mixed solution in a fifth solid-liquid separation tank to respectively obtain a fifth supernatant and fifth precipitated sludge. In this embodiment, the fifth solid-liquid separation tank is a flocculation sedimentation tank. In the advanced treatment component, the third supernatant is sequentially subjected to pH value adjustment, ozone catalytic oxidation and flocculation precipitation, high-concentration COD in the wastewater is further removed, and the effluent is ensured to meet the requirement of the inlet water quality of a low-concentration wastewater treatment system.
Meanwhile, the system also comprises a sludge collecting tank. The first centrifugal machine, the third solid-liquid separation tank and the fifth solid-liquid separation tank are respectively connected with the sludge collection tank, and first precipitated sludge generated by the first centrifugal machine, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected.
The operation of the system is as follows.
(1) Iron-carbon/ozone co-oxidation treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to 3-4; and then carrying out iron-carbon/ozone synergistic oxidation treatment for 3 hours, and adjusting the pH value to 8-9 to obtain a first mixed solution. And after the first mixed solution is subjected to centrifugal separation, the rotating speed of the centrifugal separation is 3000rad/min, and a first supernatant is obtained.
In step 1, the operation of iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to 3-4 into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment of wastewater.
(2) Anaerobic biochemical treatment
And (3) mixing the first supernatant obtained in the step (1) with the brewing low-concentration wastewater according to the volume ratio of 1:10 to obtain a second mixed solution. And (4) feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4 days to obtain a third mixed solution. And carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant.
(3) Catalytic oxidation advanced treatment by ozone
And adjusting the pH value of the third supernatant to 8-9 by using quick lime to obtain a fourth mixed solution. And treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution. And sequentially adding PAC and PAM into the fifth mixed solution, and precipitating for 2h to respectively obtain a fifth supernatant and fifth precipitated sludge, thereby finishing the pretreatment operation of the yellow water. And sending the fifth supernatant into a biochemical treatment system for biochemical treatment.
Meanwhile, first precipitated sludge generated by centrifugal separation of the first mixed solution, third precipitated sludge generated by centrifugal separation of the third mixed solution and fifth precipitated sludge generated by mud-water separation of the fifth mixed solution are respectively sent into a sludge collection tank to be collected.
Through detection, the system inlet water COD is 228000 mg/L, the ammonia nitrogen is 3021 mg/L, and the total phosphorus is 3565 mg/L; after the iron-carbon/ozone synergistic oxidation component is adopted for treatment, the effluent COD is 115200 mg/L, the ammonia nitrogen is 2451 mg/L, the total phosphorus is 455 mg/L, and the removal rates are 49.5% of COD, 18.9% of ammonia nitrogen and 87.2% of total phosphorus respectively.
After the treatment of the embodiment, the COD of the final effluent is 1100mg/L, and the ammonia nitrogen is 290 mg/L, thereby meeting the water inlet requirement of a low-concentration brewing wastewater treatment station.
Example 2
The wine brewing yellow water pretreatment system comprises a pre-conditioning pool, an iron-carbon micro-electrolysis component, an anaerobic component and a deep treatment component. The pre-adjusting tank is used for carrying out homogeneous and uniform treatment on the fed yellow water to be treated, so that the hydraulic power and impact load of a subsequent treatment system are effectively reduced, and the normal and stable operation of the system is ensured.
The iron-carbon micro-electrolysis assembly comprises a first pH value adjusting pool, an iron-carbon micro-electrolysis unit, a second pH value adjusting pool and a first centrifuge. The first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4; the iron-carbon micro-electrolysis unit comprises a synergistic oxidation tank, iron-carbon filler and an air aeration device, wherein the iron-carbon filler is arranged in the synergistic oxidation tank, and a gas outlet of the air aeration device is arranged below the iron-carbon filler; the first pH value adjusting tank is connected with the cooperative oxidation tank and is used for carrying out iron-carbon micro-electrolysis oxidation treatment on the yellow water with the pH value adjusted to 3-4; the cooperative oxidation tank is connected with the second pH value adjusting tank and is used for adjusting the pH value of the liquid obtained by iron-carbon micro-electrolysis treatment to 8-9 and obtaining a first mixed liquid; and the first centrifugal machine is connected with the second pH value adjusting tank and is used for carrying out centrifugal separation on the first mixed liquor to respectively obtain first supernatant and first precipitated sludge. By adopting the structure, the wine yellow water is sequentially subjected to pH adjustment, iron-carbon micro-electrolysis, pH adjustment, solid-liquid separation and the like.
The anaerobic component comprises an anaerobic unit and a third solid-liquid separation tank; the anaerobic unit is connected with the first centrifugal machine, and the third solid-liquid separation tank is connected with the anaerobic unit. In this embodiment, after the first supernatant produced by the first centrifuge and the low-concentration brewing wastewater are mixed in the anaerobic unit according to a volume ratio of 1:10, anaerobic biochemical treatment can be performed, and a third mixed solution is obtained. And performing solid-liquid separation on the third mixed solution by using a third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively. By adopting the step, most degradable organic pollutants in the wastewater are removed.
The advanced treatment component comprises a fourth pH value adjusting tank, a fourth ozone oxidation tank and a fifth solid-liquid separation tank. The fourth pH value adjusting tank is connected with the third solid-liquid separation tank, the fourth ozone oxidation tank is connected with the fourth pH value adjusting tank, and the fifth solid-liquid separation tank is connected with the fourth ozone oxidation tank. Sending a third supernatant obtained by separation in the third solid-liquid separation tank into a fourth pH value adjusting tank, adjusting the pH value to 8-9, and obtaining a fourth mixed solution; carrying out catalytic ozonation treatment on the fourth mixed solution in a fourth ozonation tank to obtain a fifth mixed solution; and carrying out sludge-water separation on the fifth mixed solution in a fifth solid-liquid separation tank to respectively obtain a fifth supernatant and fifth precipitated sludge. In this embodiment, the fifth solid-liquid separation tank is a flocculation sedimentation tank. In the advanced treatment component, the third supernatant is sequentially subjected to pH value adjustment, ozone catalytic oxidation and flocculation precipitation, high-concentration COD in the wastewater is further removed, and the effluent is ensured to meet the requirement of the inlet water quality of a low-concentration wastewater treatment system.
Meanwhile, the system also comprises a sludge collecting tank. The first centrifugal machine, the third solid-liquid separation tank and the fifth solid-liquid separation tank are respectively connected with the sludge collection tank, and first precipitated sludge generated by the first centrifugal machine, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected.
The operation of the system is as follows.
(1) Iron-carbon micro-electrolysis treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to 3-4; and then carrying out iron-carbon micro-electrolysis treatment for 3 hours, and adjusting the pH value to 8-9 to obtain a first mixed solution. And after the first mixed solution is subjected to centrifugal separation, the rotating speed of the centrifugal separation is 3000rad/min, and a first supernatant is obtained.
In step 1, the iron-carbon micro-electrolysis treatment is performed as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to 3-4 into the synergistic oxidation tank, and introducing air into the synergistic oxidation tank for aeration to realize iron-carbon micro-electrolysis wastewater treatment.
(2) Anaerobic biochemical treatment
And (3) mixing the first supernatant obtained in the step (1) with the brewing low-concentration wastewater according to the volume ratio of 1:10 to obtain a second mixed solution. And (4) feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4 days to obtain a third mixed solution. And carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant.
(3) Catalytic oxidation advanced treatment by ozone
And adjusting the pH value of the third supernatant to 8-9 by using quick lime to obtain a fourth mixed solution. And treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution. And sequentially adding PAC and PAM into the fifth mixed solution, and precipitating for 2h to respectively obtain a fifth supernatant and fifth precipitated sludge, thereby finishing the pretreatment operation of the yellow water. And sending the fifth supernatant into a biochemical treatment system for biochemical treatment.
Meanwhile, first precipitated sludge generated by centrifugal separation of the first mixed solution, third precipitated sludge generated by centrifugal separation of the third mixed solution and fifth precipitated sludge generated by mud-water separation of the fifth mixed solution are respectively sent into a sludge collection tank to be collected.
In this example, the quality of the feed water of the yellow water to be treated was the same as in example 1.
Detection shows that after iron-carbon micro-electrolysis treatment, the effluent COD is 154600 mg/L, the ammonia nitrogen is 2580mg/L, and the total phosphorus is 483 mg/L, and the removal rates are 32.2% of the COD, 14.6% of the ammonia nitrogen and 86.4% of the total phosphorus respectively. Adopt this embodiment to handle yellow water, waste water ammonia nitrogen and total phosphorus get rid of the effect difference not big, and the COD clearance reduces than embodiment 1, but when the COD of intaking is lower, can adopt "indisputable carbon microelectrolysis + anaerobism + ozone" processing technology, and the effluent can satisfy low concentration making wine waste water quality of water standard of intaking.
Example 3
The wine brewing yellow water pretreatment system comprises a pre-conditioning tank, a Fenton oxidation assembly, an anaerobic assembly and a deep treatment assembly. The pre-adjusting tank is used for carrying out homogeneous and uniform treatment on the fed yellow water to be treated, so that the hydraulic power and impact load of a subsequent treatment system are effectively reduced, and the normal and stable operation of the system is ensured.
The Fenton oxidation assembly comprises a first pH value adjusting tank, a Fenton reaction tank, a second pH value adjusting tank and a first filter press. The first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4; the first pH value adjusting tank is connected with the Fenton reaction tank and is used for carrying out Fenton oxidation treatment on the yellow water with the pH value adjusted to 3-4; the Fenton reaction tank is connected with the second pH value adjusting tank and is used for adjusting the pH value of the liquid obtained by Fenton oxidation treatment to 8-9 and obtaining a first mixed liquid; and the first filter press is connected with the second pH value adjusting tank and used for carrying out filter pressing treatment on the first mixed liquor to respectively obtain first supernatant and first precipitated sludge. Adopt aforementioned structure, carry out handles such as pH regulation, fenton oxidation, pH recall, solid-liquid separation to making wine yellow water in proper order, degrade macromolecule difficult degradation organic matter in the waste water into micromolecule organic matter, improve waste water biodegradability, provide the advantage for follow-up anaerobism unit, ensure the abundant effective degradation of pollutant.
The anaerobic component comprises an anaerobic unit and a third solid-liquid separation tank; the anaerobic unit is connected with the first filter press, and the third solid-liquid separation tank is connected with the anaerobic unit. In this embodiment, after the first supernatant produced by the first filter press and the low-concentration wastewater for brewing are mixed in the anaerobic unit according to the volume ratio of 1:10, anaerobic biochemical treatment can be performed, and a third mixed solution is obtained. And performing solid-liquid separation on the third mixed solution by using a third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively. By adopting the step, most degradable organic pollutants in the wastewater are removed.
The advanced treatment component comprises a fourth pH value adjusting tank, a fourth ozone oxidation tank and a fifth solid-liquid separation tank. The fourth pH value adjusting tank is connected with the third solid-liquid separation tank, the fourth ozone oxidation tank is connected with the fourth pH value adjusting tank, and the fifth solid-liquid separation tank is connected with the fourth ozone oxidation tank. Sending a third supernatant obtained by separation in the third solid-liquid separation tank into a fourth pH value adjusting tank, adjusting the pH value to 8-9, and obtaining a fourth mixed solution; carrying out catalytic ozonation treatment on the fourth mixed solution in a fourth ozonation tank to obtain a fifth mixed solution; and carrying out sludge-water separation on the fifth mixed solution in a fifth solid-liquid separation tank to respectively obtain a fifth supernatant and fifth precipitated sludge. In this embodiment, the fifth solid-liquid separation tank is a flocculation sedimentation tank. In the advanced treatment component, the third supernatant is sequentially subjected to pH value adjustment, ozone catalytic oxidation and flocculation precipitation, high-concentration COD in the wastewater is further removed, and the effluent is ensured to meet the requirement of the inlet water quality of a low-concentration wastewater treatment system.
Meanwhile, the system also comprises a sludge collecting tank. The first filter press, the third solid-liquid separation tank and the fifth solid-liquid separation tank are respectively connected with the sludge collection tank, and first precipitated sludge generated by the first filter press, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected.
The operation of the system is as follows.
(1) Fenton oxidation treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to 3-4; and after the Fenton oxidation treatment is carried out for 3 hours, the pH value is adjusted to 8-9, and a first mixed solution is obtained. And after the first mixed solution is subjected to centrifugal separation, the rotating speed of the centrifugal separation is 3000rad/min, and a first supernatant is obtained.
(2) Anaerobic biochemical treatment
And (3) mixing the first supernatant obtained in the step (1) with the brewing low-concentration wastewater according to the volume ratio of 1:10 to obtain a second mixed solution. And (4) feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4 days to obtain a third mixed solution. And carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant.
(3) Catalytic oxidation advanced treatment by ozone
And adjusting the pH value of the third supernatant to 8-9 by using quick lime to obtain a fourth mixed solution. And treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution. And sequentially adding PAC and PAM into the fifth mixed solution, and precipitating for 2h to respectively obtain a fifth supernatant and fifth precipitated sludge, thereby finishing the pretreatment operation of the yellow water. And sending the fifth supernatant into a biochemical treatment system for biochemical treatment.
Meanwhile, first precipitated sludge generated by centrifugal separation of the first mixed solution, third precipitated sludge generated by centrifugal separation of the third mixed solution and fifth precipitated sludge generated by mud-water separation of the fifth mixed solution are respectively sent into a sludge collection tank to be collected.
In this example, the quality of the feed water of the yellow water to be treated was the same as in example 1.
Detection shows that after Fenton oxidation treatment, the effluent COD is 127100 mg/L, the ammonia nitrogen is 2480mg/L, the total phosphorus is 490mg/L, and the removal rates are 44.2% of the COD, 17.9% of the ammonia nitrogen and 86.2% of the total phosphorus respectively. By adopting the embodiment to treat the yellow water, the removal effects of COD, ammonia nitrogen and total phosphorus in the wastewater are not much different from those in embodiment 1, but the dosage and the sludge amount in the Fenton oxidation reaction are huge, the treatment cost is high, and secondary pollution is possibly generated due to improper management. Because the concentration of the influent pollutants is too high, the corresponding Fenton reagent dosage is huge, a large amount of byproduct sludge is generated while the wastewater is removed, and the design concept of sustainable development is violated.
Example 4
The embodiment provides a pretreatment system for yellow wine water, which comprises a pre-adjusting tank, an iron carbon/ozone synergistic oxidation assembly, an anaerobic assembly and a deep treatment assembly. The pre-adjusting tank is used for carrying out homogeneous and uniform treatment on the fed yellow water to be treated, so that the hydraulic power and impact load of a subsequent treatment system are effectively reduced, and the normal and stable operation of the system is ensured.
The iron carbon/ozone cooperative oxidation assembly comprises a first pH value adjusting tank, an iron carbon/ozone cooperative oxidation treatment unit, a second pH value adjusting tank and a first centrifuge. The first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4; the iron-carbon/ozone synergistic oxidation treatment unit comprises a synergistic oxidation pond, iron-carbon fillers and an ozone aeration device, wherein the iron-carbon fillers are arranged in the synergistic oxidation pond, an ozone generation port of the ozone aeration device is arranged below the iron-carbon fillers, and ozone generated by the ozone aeration device can replace air and the iron-carbon fillers to carry out iron-carbon/ozone synergistic treatment on wastewater; the first pH value adjusting tank is connected with the synergistic oxidation tank and is used for carrying out iron-carbon/ozone synergistic oxidation treatment on the yellow water with the pH value adjusted to 3-4; the cooperative oxidation tank is connected with the second pH value adjusting tank and is used for adjusting the pH value of the liquid obtained by iron-carbon/ozone cooperative oxidation treatment to 8-9 and obtaining a first mixed liquid; and the first centrifugal machine is connected with the second pH value adjusting tank and is used for carrying out centrifugal separation on the first mixed liquor to respectively obtain first supernatant and first precipitated sludge. Adopt aforementioned structure, carry out handles such as pH regulation, iron carbon/ozone collaborative oxidation, pH recall, solid-liquid separation to making wine yellow water in proper order, can degrade macromolecule refractory organic matter in the yellow water into micromolecular organic matter, improve waste water biodegradability, provide the advantage for follow-up anaerobism unit, ensure the abundant effective degradation of pollutant.
The anaerobic component comprises an anaerobic unit and a third solid-liquid separation tank; the anaerobic unit is connected with the first centrifugal machine, and the third solid-liquid separation tank is connected with the anaerobic unit. In this embodiment, after the first supernatant produced by the first centrifuge and the low-concentration brewing wastewater are mixed in the anaerobic unit according to a volume ratio of 1:10, anaerobic biochemical treatment can be performed, and a third mixed solution is obtained. And performing solid-liquid separation on the third mixed solution by using a third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively. By adopting the step, most degradable organic pollutants in the wastewater are removed.
The advanced treatment component comprises a fourth pH value adjusting tank, a Fenton oxidation tank, a fifth pH value adjusting tank and a fifth solid-liquid separation tank. The fourth pH value adjusting tank is connected with the third solid-liquid separation tank, the Fenton oxidation tank is connected with the fourth pH value adjusting tank, the fifth pH value adjusting tank is connected with the Fenton oxidation tank, and the fifth solid-liquid separation tank is connected with the fifth pH value adjusting tank. Sending a third supernatant obtained by separation in the third solid-liquid separation tank into a fourth pH value adjusting tank, adjusting the pH value to 8-9, and obtaining a fourth mixed solution; performing Fenton oxidation treatment on the fourth mixed solution in a Fenton oxidation pond to obtain a fifth mixed solution; the fifth mixed solution is subjected to pH adjustment through a fifth pH value adjusting tank to obtain an adjusted intermediate solution; and (5) adjusting the intermediate solution back to perform mud-water separation in a fifth solid-liquid separation tank to obtain a fifth supernatant and fifth precipitated sludge respectively. In this embodiment, the fifth solid-liquid separation tank is a flocculation sedimentation tank. In the advanced treatment assembly, the third supernatant is sequentially subjected to pH value adjustment, Fenton oxidation, pH readjustment and flocculation precipitation, high-concentration COD in the wastewater is further removed, and the effluent is ensured to meet the requirement of the inlet water quality of a low-concentration wastewater treatment system.
Meanwhile, the system also comprises a sludge collecting tank. The first centrifugal machine, the third solid-liquid separation tank and the fifth solid-liquid separation tank are respectively connected with the sludge collection tank, and first precipitated sludge generated by the first centrifugal machine, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected.
The operation of the system is as follows.
(1) Iron-carbon/ozone co-oxidation treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to 3-4; and then carrying out iron-carbon/ozone synergistic oxidation treatment for 3 hours, and adjusting the pH value to 8-9 to obtain a first mixed solution. And after the first mixed solution is subjected to centrifugal separation, the rotating speed of the centrifugal separation is 3000rad/min, and a first supernatant is obtained.
In step 1, the operation of iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to 3-4 into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment of wastewater.
(2) Anaerobic biochemical treatment
And (3) mixing the first supernatant obtained in the step (1) with the brewing low-concentration wastewater according to the volume ratio of 1:10 to obtain a second mixed solution. And (4) feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4 days to obtain a third mixed solution. And carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant.
(3) Deep oxidation treatment
And adjusting the pH value of the third supernatant to 8-9 by using quick lime to obtain a fourth mixed solution. And treating the fourth mixed solution for 6 hours by Fenton oxidation to obtain a fifth mixed solution. And the fifth mixed solution is subjected to pH readjustment through a fifth pH value adjusting tank to obtain a readjusted intermediate solution. And sequentially adding PAC and PAM into the adjusted intermediate solution, and precipitating for 2h to respectively obtain a fifth supernatant and fifth precipitated sludge, thereby finishing the pretreatment operation of the yellow water. And sending the fifth supernatant into a biochemical treatment system for biochemical treatment.
Meanwhile, first precipitated sludge generated by centrifugal separation of the first mixed solution, third precipitated sludge generated by centrifugal separation of the third mixed solution and fifth precipitated sludge generated by mud-water separation of the fifth mixed solution are respectively sent into a sludge collection tank to be collected.
In this example, the quality of the feed water of the yellow water to be treated was the same as in example 1.
After detection, after treatment by the iron-carbon/ozone synergistic oxidation assembly, effluent COD 115200 mg/L, ammonia nitrogen 2451 mg/L and total phosphorus 455 mg/L are obtained, and the removal rates are 49.5% of COD, 18.9% of ammonia nitrogen and 87.2% of total phosphorus respectively.
After the treatment of the embodiment, the final effluent COD is 2357mg/L, and the ammonia nitrogen is 307 mg/L, so that the water inlet requirement of a low-concentration brewing wastewater treatment station is met. However, the dosage and the sludge amount of the Fenton oxidation reaction are large, the treatment cost is high, and secondary pollution can be caused by improper management. Although a large amount of COD is removed by the front-end pretreatment, the COD of the inlet water of the advanced treatment unit is still higher, the corresponding dosage of Fenton reagent is huge, a large amount of byproduct sludge is generated while the waste water is removed, and the design concept of the sustainable development is violated.
The invention is not limited to the foregoing embodiments. The invention extends to any novel feature or any novel combination of features disclosed in this specification and any novel method or process steps or any novel combination of features disclosed.
Claims (10)
1. The pretreatment method of the brewing yellow water is characterized by comprising the following steps:
(1) iron-carbon/ozone co-oxidation treatment
Sending the yellow water to be treated into a pre-adjusting tank for homogenizing and uniform treatment, and adjusting the pH value to be acidic; then carrying out iron-carbon/ozone synergistic oxidation treatment for 3-6 h, and adjusting the pH value to be alkalescent to obtain a first mixed solution; centrifuging the first mixed solution to obtain a first supernatant;
in the step 1, the operation of the iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to be acidic into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment on wastewater;
(2) anaerobic biochemical treatment
Mixing the brewing low-concentration wastewater with the first supernatant obtained in the step (1) according to a set proportion, and diluting the first supernatant through the brewing low-concentration wastewater to obtain a second mixed solution; feeding the second mixed solution into an anaerobic unit for anaerobic biochemical treatment, and treating for 4-6 days to obtain a third mixed solution;
carrying out solid-liquid separation on the third mixed solution to obtain a third supernatant;
(3) catalytic oxidation advanced treatment by ozone
Adjusting the pH value of the third supernatant to be alkalescent to obtain a fourth mixed solution; treating the fourth mixed solution for 6-10 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution;
and carrying out mud-water separation on the fifth mixed solution to obtain a fifth supernatant, and finishing the pretreatment operation of the yellow water.
2. The pretreatment method of the yellow wine brewing water according to claim 1, wherein in the step 1, the yellow water to be treated is sent into a pre-adjusting tank for homogenizing and uniform treatment, and then the pH value is adjusted to 3-4; after the iron-carbon/ozone synergistic oxidation treatment is carried out for 3 hours, the pH value is adjusted to 8-9, and a first mixed solution is obtained; centrifuging the first mixed solution to obtain a first supernatant;
in the step 1, the operation of the iron-carbon/ozone synergistic oxidation treatment is as follows: firstly, filling iron-carbon filler in the synergistic oxidation tank, then sending yellow water with the pH value adjusted to 3-4 into the synergistic oxidation tank, and introducing ozone into the synergistic oxidation tank for aeration to realize iron-carbon/ozone synergistic treatment of wastewater.
3. The pretreatment method of yellow wine brewing water as claimed in claim 1, wherein the first precipitated sludge produced by centrifuging the first mixed solution, the third precipitated sludge produced by centrifuging the third mixed solution, and the fifth precipitated sludge produced by separating the fifth mixed solution from the water are respectively sent to a sludge collection tank for collection.
4. The pretreatment method of yellow wine brewing water according to claim 1, wherein in the step 2, the third mixed solution is subjected to centrifugal separation to obtain a third supernatant and a third precipitated sludge respectively.
5. The pretreatment method of yellow wine brewing water according to claim 1, wherein in the step 3, an ozone catalyst is added into the fourth mixed solution, and ozone is introduced for catalytic oxidation treatment for 6 hours to obtain a fifth mixed solution.
6. The pretreatment method of yellow wine brewing water according to claim 1, wherein in the step 3, one or more of flocculation precipitation and filter pressing are adopted to separate the fifth mixed solution from sludge and water, and a fifth supernatant and a fifth precipitated sludge are obtained respectively.
7. The pretreatment method of yellow wine brewing water according to claim 6, wherein in the step 3, PAC and PAM are sequentially added into the fifth mixed solution, and the mixture is precipitated for 2 hours to obtain a fifth supernatant and a fifth precipitated sludge respectively.
8. The pretreatment method of yellow wine brewing water according to claim 1, wherein in the step 3, the fifth supernatant is sent to a biochemical treatment system for biochemical treatment.
9. The pretreatment method of yellow wine brewing water according to claim 1, wherein in the step 3, a fourth mixed solution is obtained after the pH value of the third supernatant is adjusted to 8-9; and treating the fourth mixed solution for 6 hours by adopting ozone catalytic oxidation to obtain a fifth mixed solution.
10. The utility model provides a making wine yellow water pretreatment systems which characterized in that includes:
the pre-adjusting tank is used for carrying out homogenizing and quantity-equalizing treatment on the fed yellow water to be treated;
the first pH value adjusting tank is connected with the pre-adjusting tank and is used for adjusting the pH value of the yellow water after the homogenization and uniform amount treatment to 3-4;
the iron-carbon/ozone synergistic oxidation treatment unit is connected with the first pH value adjusting tank and is used for carrying out iron-carbon/ozone synergistic oxidation treatment on the yellow water with the pH value adjusted to 3-4;
the second pH value adjusting tank is connected with the iron carbon/ozone synergistic oxidation treatment unit and is used for adjusting the pH value of the liquid obtained by iron carbon/ozone synergistic oxidation treatment back to 8-9 to obtain a first mixed liquid;
the first centrifuge is connected with the second pH value adjusting tank and is used for carrying out centrifugal separation on the first mixed solution to respectively obtain a first supernatant and first precipitated sludge;
the anaerobic unit is connected with the first centrifugal machine, and after the first supernatant produced by the first centrifugal machine and the brewing low-concentration wastewater are mixed in the anaerobic unit according to a set proportion, anaerobic biochemical treatment can be carried out to obtain a third mixed solution;
the third solid-liquid separation tank is connected with the anaerobic unit, and the third mixed solution is subjected to solid-liquid separation in the third solid-liquid separation tank to obtain a third supernatant and third precipitated sludge respectively;
the fourth pH value adjusting tank is connected with the third solid-liquid separation tank, and third supernatant obtained by separation in the third solid-liquid separation tank can be sent into the fourth pH value adjusting tank to adjust the pH value to 8-9, so that fourth mixed liquid is obtained;
the fourth ozone oxidation tank is connected with the fourth pH value adjusting tank, and the fourth mixed solution can be subjected to catalytic ozonation treatment in the fourth ozone oxidation tank to obtain a fifth mixed solution;
the fifth solid-liquid separation tank is connected with the fourth ozone oxidation tank, and the fifth mixed liquid can be subjected to mud-water separation in the fifth solid-liquid separation tank to obtain a fifth supernatant and fifth precipitated sludge respectively;
the sludge collection tank is respectively connected with the first centrifugal machine, the third solid-liquid separation tank and the fifth solid-liquid separation tank, and first precipitated sludge generated by the first centrifugal machine, third precipitated sludge generated by the third solid-liquid separation tank and fifth precipitated sludge generated by the fifth solid-liquid separation tank can be respectively sent into the sludge collection tank to be collected;
the iron-carbon/ozone synergistic oxidation treatment unit comprises a synergistic oxidation pond, iron-carbon fillers and an ozone aeration device, wherein the iron-carbon fillers are arranged in the synergistic oxidation pond, an ozone generation port of the ozone aeration device is arranged below the iron-carbon fillers, and ozone generated by the ozone aeration device can replace air and the iron-carbon fillers to carry out iron-carbon/ozone synergistic treatment on wastewater.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102464422A (en) * | 2011-10-26 | 2012-05-23 | 山东新时代药业有限公司 | Method for pretreating industrial waste water |
| CN103304094A (en) * | 2013-05-23 | 2013-09-18 | 宇星科技发展(深圳)有限公司 | High-concentration degradation-resistant organic wastewater treatment process |
| CN104773930A (en) * | 2015-04-30 | 2015-07-15 | 中国华电工程(集团)有限公司 | Semi-coke waste water treatment system and technology |
| CN105417793A (en) * | 2015-11-24 | 2016-03-23 | 苏州博创环保科技有限公司 | Treatment method for organic wastewater |
| CN207227082U (en) * | 2017-07-20 | 2018-04-13 | 中建华安（北京）建设工程有限公司 | A kind of micro-nano oxidation sewage-treatment plant of iron-carbon micro-electrolysis ozone |
| CN108033520A (en) * | 2017-12-11 | 2018-05-15 | 江苏森博环保科技发展有限公司 | A kind of rail carbon micro-electrolytic processes of logical ozone for wastewater treatment |
| CN113620541A (en) * | 2021-09-08 | 2021-11-09 | 贵州大学 | System and method for cooperatively treating brewing wastewater and low-carbon domestic sewage |
-
2021
- 2021-12-01 CN CN202111452040.6A patent/CN114105415A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102464422A (en) * | 2011-10-26 | 2012-05-23 | 山东新时代药业有限公司 | Method for pretreating industrial waste water |
| CN103304094A (en) * | 2013-05-23 | 2013-09-18 | 宇星科技发展(深圳)有限公司 | High-concentration degradation-resistant organic wastewater treatment process |
| CN104773930A (en) * | 2015-04-30 | 2015-07-15 | 中国华电工程(集团)有限公司 | Semi-coke waste water treatment system and technology |
| CN105417793A (en) * | 2015-11-24 | 2016-03-23 | 苏州博创环保科技有限公司 | Treatment method for organic wastewater |
| CN207227082U (en) * | 2017-07-20 | 2018-04-13 | 中建华安（北京）建设工程有限公司 | A kind of micro-nano oxidation sewage-treatment plant of iron-carbon micro-electrolysis ozone |
| CN108033520A (en) * | 2017-12-11 | 2018-05-15 | 江苏森博环保科技发展有限公司 | A kind of rail carbon micro-electrolytic processes of logical ozone for wastewater treatment |
| CN113620541A (en) * | 2021-09-08 | 2021-11-09 | 贵州大学 | System and method for cooperatively treating brewing wastewater and low-carbon domestic sewage |
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