CN101891338B - Waste water treatment method in starch and glucose production - Google Patents
Waste water treatment method in starch and glucose production Download PDFInfo
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- CN101891338B CN101891338B CN2010102204378A CN201010220437A CN101891338B CN 101891338 B CN101891338 B CN 101891338B CN 2010102204378 A CN2010102204378 A CN 2010102204378A CN 201010220437 A CN201010220437 A CN 201010220437A CN 101891338 B CN101891338 B CN 101891338B
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- 229920002472 Starch Polymers 0.000 title claims abstract description 24
- 235000019698 starch Nutrition 0.000 title claims abstract description 24
- 239000008107 starch Substances 0.000 title claims abstract description 23
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 23
- 230000009229 glucose formation Effects 0.000 title claims abstract description 17
- 239000002351 wastewater Substances 0.000 claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims abstract description 15
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims abstract description 14
- 235000005822 corn Nutrition 0.000 claims abstract description 14
- 238000006731 degradation reaction Methods 0.000 claims abstract description 13
- 230000015556 catabolic process Effects 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 230000003139 buffering effect Effects 0.000 claims abstract description 6
- 239000006228 supernatant Substances 0.000 claims description 18
- 238000004062 sedimentation Methods 0.000 claims description 16
- 240000008042 Zea mays Species 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 7
- 230000016615 flocculation Effects 0.000 claims description 7
- 230000001112 coagulating effect Effects 0.000 claims description 5
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 239000004411 aluminium Substances 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 14
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000007599 discharging Methods 0.000 abstract description 7
- 239000008103 glucose Substances 0.000 abstract description 5
- 239000010865 sewage Substances 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 230000000593 degrading effect Effects 0.000 abstract description 2
- 241000209149 Zea Species 0.000 abstract 2
- 230000008020 evaporation Effects 0.000 abstract 2
- 238000001704 evaporation Methods 0.000 abstract 2
- 230000015271 coagulation Effects 0.000 abstract 1
- 238000005345 coagulation Methods 0.000 abstract 1
- 239000008394 flocculating agent Substances 0.000 abstract 1
- 238000001914 filtration Methods 0.000 description 10
- 239000012141 concentrate Substances 0.000 description 9
- 239000010802 sludge Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000008121 dextrose Substances 0.000 description 4
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- 238000005188 flotation Methods 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 238000006396 nitration reaction Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 102000004169 proteins and genes Human genes 0.000 description 3
- 108090000623 proteins and genes Proteins 0.000 description 3
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 230000007954 hypoxia Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 235000009973 maize Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 150000002897 organic nitrogen compounds Chemical class 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 208000014451 palmoplantar keratoderma and congenital alopecia 2 Diseases 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229960004249 sodium acetate Drugs 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a wastewater treatment method in starch and glucose production, wherein the wastewater comprises corn steep liquor evaporation condensed water and process treatment wastewater, and the method comprises the following steps: a. mixing and buffering the process treated wastewater, and then performing anaerobic degradation reaction; b. mixing the wastewater after anaerobic degradation and the corn steep liquor evaporation condensate water for anoxic denitrification reaction; c. carrying out aerobic reaction on the wastewater subjected to the anoxic denitrification reaction, and removing ammonia nitrogen and further degrading; d. and adding a flocculating agent into the wastewater after the aerobic reaction for coagulation reaction, and discharging after removing suspended matters in the wastewater. The invention comprehensively utilizes the production wastewater generated in the production of starch and glucose in the wastewater treatment, treats the waste by the waste, ensures the sewage treatment effect and reduces the wastewater treatment cost.
Description
Technical field
The present invention relates to wastewater processing technology, relate in particular to the method for wastewater treatment in a kind of starch, the glucose production.
Background technology
Be to produce great amount of wastewater in the starch that carries out of raw material and the dextrose production process with the corn; Comprise corn steep liquor evaporative condensate water and art breading waste water; Wherein art breading waste water comprises the reuse water, recirculated cooling water of spent process water that operations such as fiber wash in the starch production process, flotation concentrate, albumen press filtration produce and the ion exchange system in follow-up dextrose production process etc.
Pollutent in W-Gum, the glucose wastewater is mainly dissolved organic matters such as starch, soluble proteins, carbohydrate and organic acid; Contain inorganic substance such as insoluble organism such as protein powder, maize peel and gac in addition; Be main mainly wherein with organic substance; Do not contain hazardous substance, have better biodegradability, belong to high COD, high nitrogen, high SS organic waste water.Because of organic content height in the starch glucose wastewater; If without handling directly discharging; The organism that is contained in the waste water, the dissolved oxygen in can rapid consume water after getting into water body causes water hypoxia and influences the existence of fish and other hydrocoles; Suspended substance in the waste water is prone under anaerobic decompose the generation foul smell simultaneously, worsens water quality.
To the water quality situation of W-Gum glucose wastewater, the treatment process that adopts usually at present is mainly the combined treatment technology of " anaerobism+aerobic ".Anaerobic technique adopts UASB, EGSB or IC etc. usually, and aerobic process comprises conventional activated sludge process, A/B method, A/O method, A/A/O method, SBR, CASS and contact oxidation method etc.A/O biological treatment technology maturation wherein, it is made up of anaerobic treatment unit and aerobic processing unit.Because of advantages such as A/O technology have organic matter degradation and denitrification functions efficiently, and technical process is simple, and capital cost and working cost are low, and floor space is little, become the sewage water treatment method that present most starches manufacturer generally adopts.But there is following problem in the A/O bioremediation in starch, glucose production wastewater treatment: because starch production pollutant emission ton row COD is higher at present; Outlet water organic substance is more after the anaerobic treatment; The organic loading of follow-up aerobic system is higher, is unfavorable for organic further degraded; In addition; Waste water is through anaerobic treatment, and high-enriched organics obtains degraded, and COD and BOD reduce; Meanwhile; Organic nitrogen compounds such as the protein that contains in the waste water, getting into behind the anaerobic reactor eventual degradation to be the ammonia nitrogen of high density, so high ammonia nitrogen concentration gets into follow-up aerobic treatment system and can produce many detrimentally affects:
1, the ammonia nitrogen in high density in the anaerobism water outlet gets into follow-up aerobic treatment system; Too high ammonia nitrogen loading can suppress the activity of nitrifier; Nitrated the going on foot to nitrite nitrogen one of ammonia nitrogen promptly accumulated; Be unfavorable for the nitrated removal of ammonia nitrogen on the one hand,, make the COD apparent value raise on the other hand because the 1mg/L nitrite nitrogen can show as 1.14mg/LCOD in COD mensuration process.
2, anoxic section C/N ratio is low, is unfavorable for denitrification denitrogenation, and the nitre nitrogen of high density and nitrite nitrogen remain in the water outlet of anoxic section, so that gets into the carrying out that suppresses the ammonia nitrogen nitration reaction behind the follow-up aerobic section.In addition, because the required carbon source of denitrification denitrogenation is not enough, can cause mikrobe self degraded so that carbon source to be provided, the direct result that causes like this is exactly the water outlet muddiness, and suspended substance is more, and COD rises.
If 3 nitration reactions are carried out comparatively normal, the ammonia nitrogen of high density can nitratedly be the nitre nitrogen of high density, can make that the interior pH of reaction tank is lower, and is not enough if nitration reaction is proceeded needed basicity, is unfavorable for the further fully nitrated of ammonia nitrogen.
Problems such as comprehensive above-mentioned unfavorable factor finally can cause water outlet COD and ammonia nitrogen concentration higher, and SS content is high, and colourity is dark, and pH is on the low side are difficult to reach " the People's Republic of China's integrated wastewater discharge standard " first discharge standard in (GB8978-1996).Therefore in aerobic system load operation scope,, add materials such as sodium-acetate and glucose usually carbon source is provided, finally cause cost of sewage disposal to raise if be that intensified anti-nitrated denitrogenation ability improves C/N ratio.
Summary of the invention
Technical problem to be solved by this invention is: the deficiency to prior art exists provides the starch that a kind of cost of sewage disposal is low, treatment effect is good, the method for wastewater treatment in the glucose production.
For solving the problems of the technologies described above, technical scheme of the present invention is:
Method of wastewater treatment in starch, the glucose production, said waste water comprise corn steep liquor evaporative condensate water and art breading waste water, comprise the steps:
A, said art breading waste water at first carry out the anaerobic degradation reaction after mixing and buffering.
B, the art breading waste water behind anaerobic degradation is mixed with corn steep liquor evaporative condensate water, carry out the anoxic denitrification reaction.
C, will carry out aerobic reaction, carry out ammonia nitrogen removal and further degraded through the waste water behind the anoxic denitrification reaction.
Add flocculation agent in d, the waste water behind aerobic reaction and carry out coagulating, discharge behind the suspended substance in the removal waste water.
As a kind of improvement; Said step also comprises primary sedimentation step and the secondary sedimentation step behind coagulating behind the anoxic denitrification reaction; Through precipitate and separate is supernatant and mud; Saidly get into next step wastewater treatment step, saidly discharge through the secondary sedimentation separated liquid supernatant through the primary sedimentation separated liquid supernatant.
Wherein, the said mud anoxic denitrogenation operation that refluxes back.
Wherein, the mud of the anoxic that do not reflux back denitrogenation operation carries out concentration, and press filtration is transported outward after becoming mud cake.
Dissolved oxygen＜0.5mg/L during said denitrification reaction in the waste water; C/N＞4～5; PH value=7～8; Temperature=20～35 ℃.
Dissolved oxygen >=1mg/L in waste water during said aerobic treatment; PH value=6～7; Temperature=20～35 ℃.
Said flocculation agent is a liquid aluminium polychloride, and the add-on of said flocculation agent is the 0.5～1.0wt ‰ of wastewater flow rate.
COD=8000-12000mg/L in the said art breading waste water; COD=3000-5000mg/L in the said corn steep liquor evaporative condensate water, TKN=30～40mg/L.
Said art breading waste water comprises the process water that operations such as fiber wash, flotation concentrate, albumen press filtration produce, and in follow-up dextrose production process, the reuse water of ion exchange system and recirculated cooling water etc.
Owing to adopted technique scheme, the invention has the beneficial effects as follows:
The present invention fully utilizes the factory effluent that is produced in starch, the glucose production in wastewater treatment; The corn steep liquor evaporative condensate water of the low TKN value of high COD is introduced anoxic denitrogenation operation replace additional carbon; The treatment of wastes with processes of wastes against one another has reduced cost for wastewater treatment when having guaranteed wastewater treatment efficiency.
Water-quality guideline after utilizing the present invention to the wastewater treatment that is produced in starch, the glucose production is:
COD
Cr＝75～85mg/L
BOD
5＝15～20mg/L
SS＝15～30mg/L
NH
3-N＝1.5～10mg/L
pH＝6.0～6.5
Description of drawings
Below in conjunction with accompanying drawing and embodiment the present invention is further specified.
Accompanying drawing is a process flow sheet of the present invention.
Embodiment
Shown in accompanying drawing, will comprise the process water that operations such as fiber wash, flotation concentrate, albumen press filtration produce, and in follow-up dextrose production process; The art breading waste water of the reuse water of ion exchange system and recirculated cooling water etc. is earlier after mixing and buffering; Carry out the anaerobic degradation reaction, mix with corn steep liquor evaporative condensate water then, carry out the anoxic denitrification reaction; Separate into supernatant and mud through primary sedimentation then; The sludge part anoxic denitrogenation operation that refluxes back, remaining removes to carry out mud and concentrates, and press filtration is transported outward after becoming mud cake; Supernatant gets into the aerobic reaction operation; After carrying out ammonia nitrogen removal and further degrading, add flocculation agent and carry out coagulating, the suspended substance in the removal waste water is after secondary sedimentation separates into supernatant and mud; The supernatant discharging; The sludge part anoxic denitrogenation operation that refluxes back, remaining removes to carry out mud and concentrates, and press filtration is transported outward after becoming mud cake.
Embodiment 1
A, be that the art breading waste water of 8000mg/L after mixing and buffering gets into anaerobic reactor and carries out the anaerobic degradation reaction with COD.
B, the art breading waste water behind anaerobic degradation get into the A pond, water inlet COD=1000mg/L, BOD
5=550mg/L, NH
3-N=400mg/L, dissolved oxygen=0.4mg/L, pH value=7.6; Water temperature is 30 ℃, and the corn steep liquor evaporative condensate water of introducing COD=5000mg/L, TKN=35mg/L gets into the A pond mixes, and regulates C/N=4.94; Carry out the anoxic denitrification reaction, separate into supernatant and mud through primary sedimentation then, the sludge part A pond of refluxing back; Remaining removes to carry out mud and concentrates, and press filtration is transported outward after becoming mud cake.
C, the supernatant after primary sedimentation separates get into the O pond and carry out aerobic treatment, at dissolved oxygen 2.0mg/L; PH value=6.6; During temperature=32 ℃, carry out ammonia nitrogen removal and further degraded.
D, the waste water after aerobic treatment get into coagulator; The liquid aluminium polychloride that adds wastewater flow rate 0.8wt ‰ is removed the suspended substance in the waste water, separates into supernatant and mud through secondary sedimentation then; The supernatant discharging; The sludge part A pond of refluxing back, remaining removes to carry out mud and concentrates, and press filtration becomes outward transport back discharging behind the mud cake.
Waste water COD clearance=92.4% after comprehensive treating process, ammonia nitrogen removal frank=99.4%.
The effluent quality index:
COD
Cr＝76mg/L
BOD
5＝15mg/L
SS＝19mg/L
NH
3-N＝2.4mg/L
pH＝6.5
Effluent quality meets " the People's Republic of China's integrated wastewater discharge standard " first discharge standard in (GB8978-1996).
Embodiment 2
A, be that the art breading waste water of 10000mg/L gets into anaerobic reactor and carries out the anaerobic degradation reaction after mixing and buffering with COD.
B, the art breading waste water behind anaerobic degradation get into the A pond, water inlet COD=1200mg/L, BOD
5=660mg/L, NH
3-N=550mg/L, dissolved oxygen=0.4mg/L, pH value=7.3; Water temperature is 30 ℃, and the corn steep liquor evaporative condensate water of introducing COD=4500mg/L, TKN=40mg/L gets into the A pond mixes, and regulates C/N=4.15; Carry out the anoxic denitrification reaction, separate into supernatant and mud through primary sedimentation then, the sludge part A pond of refluxing back; Remaining removes to carry out mud and concentrates, and press filtration is transported outward after becoming mud cake.
C, the supernatant after primary sedimentation separates get into the O pond and carry out aerobic treatment, at dissolved oxygen 2.5mg/L; PH value=6.4; During temperature=32 ℃, carry out ammonia nitrogen removal and further degraded.
D, the waste water after aerobic treatment get into coagulator; The liquid aluminium polychloride that adds wastewater flow rate 1.0wt ‰ is removed the suspended substance in the waste water, separates into supernatant and mud through secondary sedimentation then; The supernatant discharging; The sludge part A pond of refluxing back, remaining removes to carry out mud and concentrates, and press filtration becomes outward transport back discharging behind the mud cake.
Waste water COD clearance=93.1% after comprehensive treating process, ammonia nitrogen removal frank=98.3%.
The effluent quality index:
COD
Cr＝83mg/L
BOD
5＝19mg/L
SS＝26mg/L
NH
3-N＝9.5mg/L
pH＝6.2
Effluent quality meets " the People's Republic of China's integrated wastewater discharge standard " first discharge standard in (GB8978-1996).
Claims (8)
1. the method for wastewater treatment in starch, the glucose production, said waste water comprises corn steep liquor evaporative condensate water and art breading waste water, it is characterized in that comprising the steps:
A, said art breading waste water at first carry out the anaerobic degradation reaction after mixing and buffering;
B, the art breading waste water behind anaerobic degradation is mixed with corn steep liquor evaporative condensate water, carry out the anoxic denitrification reaction;
C, will carry out aerobic reaction, carry out ammonia nitrogen removal and further degraded through the waste water behind the anoxic denitrification reaction;
Add flocculation agent in d, the waste water behind aerobic reaction and carry out coagulating, discharge behind the suspended substance in the removal waste water.
2. the method for wastewater treatment in starch as claimed in claim 1, the glucose production; It is characterized in that: said step also comprises primary sedimentation step and the secondary sedimentation step behind coagulating behind the anoxic denitrification reaction; Through precipitate and separate is supernatant and mud; Saidly get into next step wastewater treatment step, saidly discharge through the secondary sedimentation separated liquid supernatant through the primary sedimentation separated liquid supernatant.
3. the method for wastewater treatment in starch as claimed in claim 2, the glucose production is characterized in that: the said mud anoxic denitrogenation operation that refluxes back.
4. the method for wastewater treatment in starch as claimed in claim 2, the glucose production is characterized in that: said mud carries out concentration.
5. the method for wastewater treatment in starch as claimed in claim 2, the glucose production is characterized in that: the dissolved oxygen＜0.5mg/L during said anoxic denitrification reaction in the waste water; 4＜C/N＜5; PH value=7～8; Temperature=20～35 ℃.
6. the method for wastewater treatment in starch as claimed in claim 2, the glucose production is characterized in that: dissolved oxygen >=1mg/L in waste water during said aerobic reaction; PH value=6～7; Temperature=20～35 ℃.
7. the method for wastewater treatment in starch as claimed in claim 2, the glucose production is characterized in that: said flocculation agent is a liquid aluminium polychloride, and the add-on of said flocculation agent is the 0.5～1.0wt ‰ of wastewater flow rate.
8. like the method for wastewater treatment in described any starch of claim 1 to 7, the glucose production, it is characterized in that: COD=8000-12000mg/L in the said art breading waste water; COD=3000-5000mg/L in the said corn steep liquor evaporative condensate water, TKN=30～40mg/L.
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| CN101891338B true CN101891338B (en) | 2012-05-09 |
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| CN102557357B (en) * | 2012-02-21 | 2014-04-02 | 东莞理工学院 | Treatment method and treatment system for soy sauce brewing industrial wastewater |
| CN106995256A (en) * | 2016-01-26 | 2017-08-01 | 中国环境科学研究院 | A kind of handling process of starch wastewater |
| CN107720948A (en) * | 2017-10-31 | 2018-02-23 | 沧源南华勐省糖业有限公司 | A kind of sugar production wastewater CASS activated sludge treatment methods |
| CN108569824A (en) * | 2018-04-28 | 2018-09-25 | 陕西昕宇表面工程有限公司 | A kind of starch gourmet powder waste water biochemistry intensive treatment system and technique |
| CN113321339B (en) * | 2021-05-06 | 2022-04-29 | 江南大学 | A kind of method for evaporative condensation water resource treatment and reuse to produce fuel ethanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1055161A (en) * | 1990-03-29 | 1991-10-09 | 化工部北京化工研究院 | Composite biological fluidized-bed reactor for treatment of starch wastewater |
| CN1772661A (en) * | 2005-10-15 | 2006-05-17 | 桂林工学院 | Combined biological treatment process of cassava starch production wastewater |
| CN101113047A (en) * | 2007-06-20 | 2008-01-30 | 江南大学 | A treatment method for refractory high-concentration organic wastewater |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1055161A (en) * | 1990-03-29 | 1991-10-09 | 化工部北京化工研究院 | Composite biological fluidized-bed reactor for treatment of starch wastewater |
| CN1772661A (en) * | 2005-10-15 | 2006-05-17 | 桂林工学院 | Combined biological treatment process of cassava starch production wastewater |
| CN101113047A (en) * | 2007-06-20 | 2008-01-30 | 江南大学 | A treatment method for refractory high-concentration organic wastewater |
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