CN102249498A - Biochemical treatment method for waste water from small and medium-sized starch factories - Google Patents
Biochemical treatment method for waste water from small and medium-sized starch factories Download PDFInfo
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Abstract
The invention discloses a biochemical treatment method for waste water from small and medium-sized starch factories. The biochemical treatment method comprises the following steps of: stirring an organic flocculating agent and an inorganic flocculating agent in waste water, so that flocculate is formed in mixed solution; performing air floating separation on the mixed solution formed by stirring by using an air floating tank to separate suspended matters from the waste water; filtering separated effluent and dehydrating to obtain starch protein and filter liquor; guiding the filter liquor into an internal circulation (IC) reactor to perform biochemical treatment, and guiding liquid which is subjected to the biochemical treatment into a membrane biological reactor (MBR) for separating; and drying and recycling sludge obtained by separation, and discharging or recycling obtained subnatant which meets the national sewage discharge standard directly. By the biochemical treatment method, a large amount of starch waste water can be treated effectively and the starch protein and methane can be recovered in the waste treatment process, so that resources are utilized to a maximum degree to create obvious economic and environmental benefit.
Description
Technical field
The present invention relates to a kind of wastewater treatment method, particularly relate to a kind of biochemical processing method of middle-size and small-size wastewater of starch factory.
Background technology
Starch is a kind of important industrial raw material, except that edible and processed food, is applied to industries such as weaving, papermaking, medicine, fermentation, casting, gluing, chemical industry, machinery and drilling well widely.But in the starch course of processing, can produce the acid organic waste water of a large amount of high densitys, contain carbohydrate, protein and organic acids etc. such as a large amount of remaining starch, glucose, fructose, maltose in the organic waste water, easily corrupt smelly, chemical oxygen demand COD content is everlasting between 1000～30000mg/L; In addition, total nitrogen and phosphate concn height in the starch wastewater are to pollute one of the most serious waste water in the foodstuffs industry.
At present, China produces more than 300 ten thousand tons of starch per year, and according to existing complete processing, 1 ton of starch of average every production produces 10～20m
3Waste water, the nontoxicity of starch wastewater own, its pollutent mainly are the organism that carbohydrate, protein, fat etc. generate naturally, easily corrupt fermentation, make the water quality blackout smelly, enter the dissolved oxygen in the rivers meeting consume water, promote the breeding of algae and waterplant, when the starch wastewater amount is big, river meeting severe depletion of oxygen, generation anaerobism corruption is distributed stench, makes therefore death by suffocation of hydrocoles such as its fish, shrimp, shellfish.Therefore, starch wastewater is treated as the very severe problem that present China Starch Production producer faces.
At present, the existing method of handling at starch wastewater both at home and abroad mainly contains physico-chemical process and biological process.
1, physico-chemical process: mainly comprise flocculent precipitation and the combined technical method of forming by flocculation and absorption.Though the physico-chemical process investment is little, the working cost height, and also water outlet is difficult to reach emission standard.
2, biological process: mainly comprise aerobe method, anaerobic biological process and photosynthetic bacterium method etc., bioremediation is because have advantages such as cost is low, energy consumption is little, surplus sludge volume is few, thereby obtained the attention of environmental engineering circle.
Aspect the processing starch wastewater, main prior art is as follows:
1999, the China relevant technologies personnel of agricultural machinery research institute food machinery institute have proposed to brief talk middle-size and small-size yam starch factory sewage disposal scheme, this article has simply been introduced the present situation of China's starch industry, set forth present technology level and the discharge of wastewater situation of potato starch factory, proposed employing anaerobic-aerobic biochemical processing method, introduced producing technical scheme and the technical process that 5000 tons of yam starch factory discharge of wastewater carry out sewage disposal per year.This starch wastewater treatment process technology is outmoded, and the waste water after the processing may cause secondary pollution; And still contain the lot of valuable resource in the waste water after handling, the discharging of waste water has caused the waste of precious resources.
In addition, have now in the wastewater processing technology and corn starch wastewater is used to feed pigs, feeds chicken etc. through the throw out of barrier post precipitation, waste water entered oxidation pond spontaneous fermentation 1～2 day, enter the Herba Eichhorniae pond then and purify 7 days, enter the fine duckweed pond again and purify 7 days, reach agricultural irrigation water quality standard, this part water is used to irrigate rice field, fruit tree and vegetables etc., realizes the utilization again of resource by this process.This treatment process is with low content of technology, in the waste water still some resource be wasted.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of biochemical processing method of middle-size and small-size wastewater of starch factory.Can effectively handle a large amount of starch wastewaters by the inventive method, its resource is farthest utilized, thereby obtain remarkable economic efficiency and environmental benefit.
In order to address the above problem, the technical solution used in the present invention is:
The invention provides a kind of biochemical processing method of middle-size and small-size wastewater of starch factory, described biochemical processing method may further comprise the steps:
A, at first in starch wastewater, add the organic polymer coargulator polyacrylamide solution and the inorganic flocculating agent polymerize aluminum chloride aqueous solution, mix then, obtain mixed solution, be formed with stable floc sedimentation in the mixed solution; The add-on of described polyacrylamide solution accounts for 2～4% of starch wastewater gross weight, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1～2% of starch wastewater gross weight;
B, the mixed solution importing air flotation pool that step a is mixed carry out dissolved air flotation, through after the dissolved air flotation, isolate the suspended substance floc sedimentation that floats in the mixed solution, obtaining water outlet is protein liquid, to separate the water outlet that obtains through air flotation pool is that protein liquid adopts plate-and-frame filter press to carry out filter-press dehydration, obtain starch albumen and filtered liquid after the dehydration, gained starch albumen is made protein fodder through the pipe bundle drier drying;
C, filtered liquid that will obtain behind the step b filter-press dehydration import in the IC anaerobic reactor and carry out biochemical treatment, the filtered liquid that is about to obtain is entered first reaction zone of reactor by the bottom of IC anaerobic reactor, the filtered liquid that imports is diluted in water inlet by reactor, organism in its filtered liquid is fully reacted to be degraded, produce a large amount of biogas simultaneously, the biogas part of generation is collected by the triphase separator of IC anaerobic reactor lower floor; A part of in addition biogas carries that mud enters second reaction zone in filtered liquid and the filtered liquid secretly, filtered liquid enters in the gas-liquid separator that is provided with in second reaction zone under the effect of carrying secretly of biogas, by gas-liquid separation, biogas breaks away from filtered liquid and effluxes collection, and residue filtered liquid and mud enter the bottom of first reaction zone by return line under action of gravity;
D, the filtered liquid that enters first reaction zone bottom after step c handled through the IC anaerobic reactor and mud import in the MBR membrane bioreactor and separate, the time that stops in the MBR membrane bioreactor is 4～6h, and the content of control dissolved oxygen DO composition is 2～4 mg/L in the sepn process; Carry out drying through the mud that obtains after the separation of MBR membrane bioreactor and utilize again, the following clear liquid that obtains after the separation is discharging or recycle directly.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, the mass percentage concentration of polyacrylamide solution described in the step a is 0.05～0.1%; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 5～10%.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, described in the step b with gained starch albumen when the pipe bundle drier drying is made protein fodder, drying conditions is that normal pressure, drying temperature are that 40～50 ℃, time of drying are 4～6h.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, isolate the suspended substance floc sedimentation that floats in the mixed solution described in the step b, isolate ss suspended solid and chemical oxygen demand COD in the starch wastewater behind the suspended substance
CrThe clearance of the two reaches respectively 〉=and 80% and 〉=30%.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, it is the tower reactor of 4～8:1 that the anaerobic reactor of IC described in the step c adopts aspect ratio; Described IC anaerobic reactor is to move under normal temperature condition, and volumetric loading is 17.0～22.0 kg COD
Cr/ (m
3D), settling region surface load 0.6 m
3/ (m
2H), reaction zone hydraulic detention time 5～7 h.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, what the membrane bioreactor of MBR described in the steps d adopted is polypropylene hollow fiber membrane, and the aperture of film is 0.1～0.45 μ m.
According to the biochemical processing method of above-mentioned middle-size and small-size wastewater of starch factory, steps d is through ss suspended solid and biochemical oxygen demand (BOD) BOD in the clear liquid under the gained of MBR membrane bioreactor separation back
5Clearance reach respectively 〉=90% and 〉=85%.
Positive beneficial effect of the present invention:
1, at first in starch wastewater, adds organic floculant and inorganic flocculating agent in the treatment process of the present invention, add inorganic flocculating agent and can produce electrical neutralizing effect, wadding grain in the waste water is easy near being condensed into bigger wadding grain, adding organic floculant can make between the wadding grain by the more stable big floc sedimentation of adsorption bridging effect formation, help dissolved air flotation like this, thereby can effectively isolate ss suspended solid and chemical oxygen demand COD in the waste water
CrThe present invention unites use organic floculant and inorganic flocculating agent, and not only flocculating effect is good, and can reduce the consumption of flocculation agent greatly.
2, the waste water that will add flocculation agent in the treatment process of the present invention mixes, utilize air flotation pool to separate, carry out filter dehydration through the water outlet that obtains after the dissolved air flotation, can obtain protein fodder after the filtration, ss suspended solid and chemical oxygen demand COD in the filtrate filtered
CrClearance reach respectively more than 80% and more than 30%.According to measuring and calculating, can extract protein fodder 5kg at this stage every cubic metre of waste water, according to 1150 yuan of/ton calculating, every cubic metre of waste water can bring benefits 5.75 yuan; Can extract protein fodder 5kg according to every cubic metre of waste water and calculate, can extract 3969 tons of protein fodders every year.The present invention carries out in the IC anaerobic reactor in the biochemical treatment process, and every cubic metre of waste water can reclaim 1.90m
3Biogas.Therefore,, not only effectively handled a large amount of starch wastewaters, also obtained extra economic benefit simultaneously by the present invention.Therefore, the present invention has remarkable economic efficiency and social benefit.
3, after starch wastewater is handled through the inventive method, the ss suspended solid in the starch wastewater, chemical oxygen demand COD
CrWith biochemical oxygen demand (BOD) BOD
5Reduce to 86 mg/L, 127 mg/L and 22.5 mg/L respectively by original content 6862mg/L, 14467 mg/L and 8672 mg/L, promptly descend clear liquid can reach integrated wastewater discharge standard (GB8978-1996, first discharge standard) fully through the water outlet that obtains after the last MBR membrane bioreactor separation.Therefore,, not only efficiently solve the starch wastewater pollution problems, and in wastewater treatment process, also extracted protein fodder and obtained biogas, additionally obtained economic benefit through treatment process of the present invention.So no matter the present invention aspect economic benefit or aspect social environment benefit, has significant effect.
4, after the present invention passes through to add flocculation agent, dissolved air flotation, the processing of IC anaerobic biological and MBR Membrane Bioreactor for Wastewater Treatment with starch wastewater; can make the final effluent quality of starch wastewater of high density be better than the GB8978-1996 first discharge standard; final water outlet can be back to factory's wash-down water, flushing supply, greening water, landscape water; not only reached the purpose of protection environment; saved conventional water resources simultaneously; good ecological benefits have been obtained; and reduced fresh water, reduced the enterprise water use cost.Thereby the present invention has remarkable economic efficiency.
Four, embodiment:
Following examples only in order to further specify the present invention, do not limit content of the present invention.
Embodiment 1:
The biochemical processing method of a kind of middle-size and small-size wastewater of starch factory of the present invention, the detailed step of described biochemical processing method is as follows:
A, at first in starch wastewater, add the organic polymer coargulator polyacrylamide solution and the inorganic flocculating agent polymerize aluminum chloride aqueous solution, mix then, obtain mixed solution, be formed with stable floc sedimentation in the mixed solution; The mass percentage concentration of described polyacrylamide solution is 0.08%, and the add-on of polyacrylamide solution accounts for 3% of starch wastewater gross weight; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 8%, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1.5% of starch wastewater gross weight;
B, the mixed solution that step a is mixed import air flotation pool and carry out dissolved air flotation, through after the dissolved air flotation, isolate the suspended substance floc sedimentation that floats in the mixed solution and (isolate ss suspended solid and chemical oxygen demand COD in the starch wastewater behind the suspended substance
CrThe clearance of the two reaches respectively 〉=and 80% and 〉=30%), obtaining water outlet is protein liquid; To separate the water outlet that obtains through air flotation pool is that protein liquid adopts plate-and-frame filter press to carry out filter-press dehydration, obtains starch albumen and filtered liquid after the dehydration, and gained starch albumen is made protein fodder through the pipe bundle drier drying; Drying conditions is that normal pressure, drying temperature are that 40 ℃, time of drying are 6h when pipe bundle drier is dry;
C, filtered liquid that will obtain behind the step b filter-press dehydration import in the IC anaerobic reactor and carry out biochemical treatment, the filtered liquid that is about to obtain is entered first reaction zone of reactor by the bottom of IC anaerobic reactor, the filtered liquid that imports is diluted in water inlet by reactor, organism in its filtered liquid is fully reacted to be degraded, produce a large amount of biogas simultaneously, the biogas part of generation is collected by the triphase separator of IC anaerobic reactor lower floor; A part of in addition biogas carries that mud enters second reaction zone in filtered liquid and the filtered liquid secretly, filtered liquid enters in the gas-liquid separator that is provided with in second reaction zone under the effect of carrying secretly of biogas, by gas-liquid separation, biogas breaks away from filtered liquid and effluxes collection, and residue filtered liquid and mud enter the bottom of first reaction zone by return line under action of gravity;
It is the tower reactor of 4～8:1 that described IC anaerobic reactor adopts aspect ratio; Described IC anaerobic reactor is to move under normal temperature condition, and volumetric loading is 17.0～22.0 kg COD
Cr/ (m
3D), settling region surface load 0.6 m
3/ (m
2H), reaction zone hydraulic detention time 5～7 h;
D, the filtered liquid that enters first reaction zone bottom after step c handled through the IC anaerobic reactor and mud import in the MBR membrane bioreactor and separate that (what described MBR membrane bioreactor adopted is polypropylene hollow fiber membrane, the aperture of film is 0.1～0.45 μ m), the time that stops in the MBR membrane bioreactor is 4～6h, and the content of control dissolved oxygen DO composition is 2～4 mg/L in the sepn process; Carry out drying through the mud that obtains after the separation of MBR membrane bioreactor and utilize again, the following clear liquid that obtains after the separation is discharging or recycle directly; Through ss suspended solid and biochemical oxygen demand (BOD) BOD in the clear liquid under the gained of MBR membrane bioreactor separation back
5Clearance reach respectively 〉=90% and 〉=85%.
Embodiment 2: substantially the same manner as Example 1, difference is:
Among the step a: the mass percentage concentration of described polyacrylamide solution is 0.05%, and the add-on of polyacrylamide solution accounts for 4% of starch wastewater gross weight; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 10%, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1.0% of starch wastewater gross weight;
Among the step b: drying conditions is that normal pressure, drying temperature are that 50 ℃, time of drying are 4h when pipe bundle drier is dry.
Embodiment 3: substantially the same manner as Example 1, difference is:
Among the step a: the mass percentage concentration of described polyacrylamide solution is 0.1%, and the add-on of polyacrylamide solution accounts for 2% of starch wastewater gross weight; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 5%, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 2% of starch wastewater gross weight;
Among the step b: drying conditions is that normal pressure, drying temperature are that 45 ℃, time of drying are 5h when pipe bundle drier is dry.
Embodiment 4: substantially the same manner as Example 1, difference is:
Among the step a: the mass percentage concentration of described polyacrylamide solution is 0.065%, and the add-on of polyacrylamide solution accounts for 3.5% of starch wastewater gross weight; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 9%, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1.2% of starch wastewater gross weight.
Embodiment 5: substantially the same manner as Example 1, difference is:
Among the step a: the mass percentage concentration of described polyacrylamide solution is 0.09%, and the add-on of polyacrylamide solution accounts for 2.5% of starch wastewater gross weight; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 6%, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1.8% of starch wastewater gross weight.
Claims (7)
1. the biochemical processing method of a middle-size and small-size wastewater of starch factory is characterized in that, described biochemical processing method may further comprise the steps:
A, at first in starch wastewater, add the organic polymer coargulator polyacrylamide solution and the inorganic flocculating agent polymerize aluminum chloride aqueous solution, mix then, obtain mixed solution, be formed with stable floc sedimentation in the mixed solution; The add-on of described polyacrylamide solution accounts for 2～4% of starch wastewater gross weight, and the add-on of the polymerize aluminum chloride aqueous solution accounts for 1～2% of starch wastewater gross weight;
B, the mixed solution importing air flotation pool that step a is mixed carry out dissolved air flotation, through after the dissolved air flotation, isolate the suspended substance floc sedimentation that floats in the mixed solution, obtaining water outlet is protein liquid, to separate the water outlet that obtains through air flotation pool is that protein liquid adopts plate-and-frame filter press to carry out filter-press dehydration, obtain starch albumen and filtered liquid after the dehydration, gained starch albumen is made protein fodder through the pipe bundle drier drying;
C, filtered liquid that will obtain behind the step b filter-press dehydration import in the IC anaerobic reactor and carry out biochemical treatment, the filtered liquid that is about to obtain is entered first reaction zone of reactor by the bottom of IC anaerobic reactor, the filtered liquid that imports is diluted in water inlet by reactor, organism in its filtered liquid is fully reacted to be degraded, produce a large amount of biogas simultaneously, the biogas part of generation is collected by the triphase separator of IC anaerobic reactor lower floor; A part of in addition biogas carries that mud enters second reaction zone in filtered liquid and the filtered liquid secretly, filtered liquid enters in the gas-liquid separator that is provided with in second reaction zone under the effect of carrying secretly of biogas, by gas-liquid separation, biogas breaks away from filtered liquid and effluxes collection, and residue filtered liquid and mud enter the bottom of first reaction zone by return line under action of gravity;
D, the filtered liquid that enters first reaction zone bottom after step c handled through the IC anaerobic reactor and mud import in the MBR membrane bioreactor and separate, the time that stops in the MBR membrane bioreactor is 4～6h, and the content of control dissolved oxygen DO composition is 2～4 mg/L in the sepn process; Carry out drying through the mud that obtains after the separation of MBR membrane bioreactor and utilize again, the following clear liquid that obtains after the separation is discharging or recycle directly.
2. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1, it is characterized in that: the mass percentage concentration of polyacrylamide solution described in the step a is 0.05～0.1%; The mass percentage concentration of the described polymerize aluminum chloride aqueous solution is 5～10%.
3. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1, it is characterized in that: described in the step b with gained starch albumen when the pipe bundle drier drying is made protein fodder, drying conditions is that normal pressure, drying temperature are that 40～50 ℃, time of drying are 4～6h.
4. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1 is characterized in that: isolate the suspended substance floc sedimentation that floats in the mixed solution described in the step b, isolate ss suspended solid and chemical oxygen demand COD in the starch wastewater behind the suspended substance
CrThe clearance of the two reaches respectively 〉=and 80% and 〉=30%.
5. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1 is characterized in that: it is the tower reactor of 4～8:1 that the anaerobic reactor of IC described in the step c adopts aspect ratio; Described IC anaerobic reactor is to move under normal temperature condition, and volumetric loading is 17.0～22.0 kg COD
Cr/ (m
3D), settling region surface load 0.6 m
3/ (m
2H), reaction zone hydraulic detention time 5～7 h.
6. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1 is characterized in that: what the membrane bioreactor of MBR described in the steps d adopted is polypropylene hollow fiber membrane, and the aperture of film is 0.1～0.45 μ m.
7. the biochemical processing method of middle-size and small-size wastewater of starch factory according to claim 1 is characterized in that: steps d is separated under the gained of back ss suspended solid and biochemical oxygen demand (BOD) BOD in the clear liquid through the MBR membrane bioreactor
5Clearance reach respectively 〉=90% and 〉=85%.
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Cited By (13)
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| CN104118964A (en) * | 2014-06-19 | 2014-10-29 | 山东西王糖业有限公司 | Method for separating active protein in sewage treatment process |
| CN104478989A (en) * | 2014-12-20 | 2015-04-01 | 山东绅联生物科技有限公司 | Method for recovering protein from heparin sodium extraction waste liquid |
| CN104609646A (en) * | 2014-12-24 | 2015-05-13 | 三达膜环境技术股份有限公司 | Treatment method of Chinese caterpillar fungus powder wastewater |
| CN105366783A (en) * | 2015-12-08 | 2016-03-02 | 甘肃省建材科研设计院 | Purification treatment method of potato starch wastewater |
| CN105461162A (en) * | 2015-11-24 | 2016-04-06 | 广西罗城科潮基业科技发展有限公司 | Starch wastewater treatment method |
| CN106746225A (en) * | 2016-12-28 | 2017-05-31 | 宁夏北国环保节能有限公司 | Device and method for recovering potato starch production wastewater |
| CN107050937A (en) * | 2017-04-13 | 2017-08-18 | 池州西恩新材料科技有限公司 | A kind of processing system and processing method in coal chemical industry Heisui River |
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| CN108423828A (en) * | 2018-05-15 | 2018-08-21 | 中国科学院兰州化学物理研究所 | A kind of potato starch processing waste water qualified discharge processing system |
| CN108689489A (en) * | 2018-05-15 | 2018-10-23 | 中国科学院兰州化学物理研究所 | A kind of potato starch processing waste water qualified discharge treatment process |
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| CN109956615A (en) * | 2017-12-25 | 2019-07-02 | 安徽洁之源环保科技有限公司 | Packaging printing sewage treatment process |
| CN108423828A (en) * | 2018-05-15 | 2018-08-21 | 中国科学院兰州化学物理研究所 | A kind of potato starch processing waste water qualified discharge processing system |
| CN108689489A (en) * | 2018-05-15 | 2018-10-23 | 中国科学院兰州化学物理研究所 | A kind of potato starch processing waste water qualified discharge treatment process |
| CN111233261A (en) * | 2020-01-20 | 2020-06-05 | 轻工业环境保护研究所 | Treatment technology of potato starch production wastewater |
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