CN1422818A - Process for treating waste water for fumaric acid production - Google Patents
Process for treating waste water for fumaric acid production Download PDFInfo
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- CN1422818A CN1422818A CN 01130577 CN01130577A CN1422818A CN 1422818 A CN1422818 A CN 1422818A CN 01130577 CN01130577 CN 01130577 CN 01130577 A CN01130577 A CN 01130577A CN 1422818 A CN1422818 A CN 1422818A
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- waste water
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention is a processing technique of fumaric acid production waste water. It includes in turn the steps as follows: the pretreatment on original waste water; anaerobic bio-treatment; aerobic bio-treatment; materialization treatment. It adopts the treating technique of combining anaerobic and aerobic bio-treatment and materialization method and overcomes the problem of environmental pollution.
Description
Technical field
The present invention relates to the treatment process of trade effluent, be specially the treatment process of waste water for fumaric acid production.
Background technology
Waste water for fumaric acid production is a kind of high density organic chemical waste water, and this waste water acidity is big, and pH value is 1～2, and organic content height, its CODcr are up to 80000～100000mg/l, and directly exhaust emission is very serious.In the past, once the someone want with wet oxidation process or burning method this waste water to be handled, but the cost height is serious to topsoil, does not finally also thoroughly handle.Remove this, find no this wastewater treatment method.
Summary of the invention
Technical problem to be solved by this invention is that waste water for fumaric acid production is handled, and cost is low, and the efficient height reaches effective improvement, thereby proposes a kind of treatment process.
The treatment process of waste water for fumaric acid production of the present invention is characterized in that in turn including the following steps:
Original waste water is through pre-treatment;
Anaerobic biological treatment;
Aerobe is handled;
Materialization is handled.
The present invention adopts biopurification to handle the mode that combines with materialization, makes waste water for fumaric acid production obtain administering effectively, reaches emission standard.By waste water for fumaric acid production is carried out comprehensive water quality analysis, the organism that the waste water that produces in the discovery fumaric acid production process contains has tens kinds, wherein contain compound and a spot of toxicant of being with phenyl ring, through a large amount of experimental results show that, the biodegradability of this waste water is still very high, after testing, original waste water CODcr after cooling off is reduced to 72000mg/l, at this moment BOD
5Content is 38000mg/l, BOD
5About 0.53 with the ratio of CODcr, can adopt biochemical method to handle.Consider simultaneously and contain phenyl ring based compound and poisonous substance accumulation problem in the waste water, adopt physical chemistry method to handle again after the biochemical treatment.
Original waste water is at pretreatment stage, the naturally cooling cooling, CODcr reduces to 72000mg/l, remove decrystallize and impurity after the waste water pH value that adds alkali such as adjusting waste water such as sodium hydroxide, lime be 3.5～5.5, preferred 3.5～4.0.Because waste water heterogeneity, organic concentration is very high, needs thin up, amount of water how much be to make CODcr in the waste water between 8000～12000mg/l, PH is 6～6.5, and waste water carry out heat temperature raising to 38～carry out anaerobic biological treatment after 40 ℃ or 53～55 ℃.
Anaerobic biological treatment can adopt multiple anaerobic technique method such as UASB, UASB+AF, AAFEB, EGSB or the like.Attemperator is arranged, and water distribution is even.Waste water is 5～30 days through the anaerobic biological treatment time, finishes after precipitate and carry out aerobe processing.The use that can reflux of the water outlet part of anaerobic biological treatment is used for the dilution of original waste water, and this part recirculation water is 2～10: 1 with the reflux ratio of advance waste water.
The aerobe system can adopt various ways, as active sludge, SBR, microbial film facture or the like, in lagging facility is arranged, aeration is cultivated.Temperature when aerobe is handled is 20～28 ℃, and the time is 0.5～16 day, and the water outlet dissolved oxygen is controlled at 〉=2mg/l.Carry out the materialization processing through the water outlet that aerobe is handled through post precipitation.
Materialization is handled and is comprised oxide treatment and activated carbon adsorption processing.Carry out oxide treatment through the water outlet that aerobe is handled through post precipitation adding strong oxidizer, strong oxidizer can be selected hydrogen peroxide, ozone for use, the consumption of strong oxidizer is according to how much the deciding of the organic content that contains in the waste water after biochemical treatment, and makes the content of the waste water COD cr after biochemical treatment reduce by 50～65%.Carry out charcoal absorption at last.
Beneficial effect of the present invention: the treatment process that the present invention has adopted the anaerobic and aerobic bioremediation to combine with physical chemistry method, less investment, expense is low, the efficient height, instant effect has overcome the problem of environmental pollution that adopts the burn processing method to cause.Make the high concentrated organic wastewater in the fumaric acid production obtain effective improvement, reach emission request, fundamentally solved present domestic open question still.Below be the content of CODcr in the waste water through each treatment stage, unit is mg/l:
Original waste water pre-treatment and anaerobic biological treatment aerobe are handled materialization and are handled
80000～100000 5000～8000 300～500 150
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
Embodiment
CODcr content is 100000mg/l in the original waste water, waste water COD cr content is 72000mg/l behind naturally cooling, it is 4.0 that hydro-oxidation sodium is regulated its pH value, carrying out the water yield in mixing the pond regulates, make that CODcr is 12000mg/l in the water after the adjusting, PH=6.5, mixing in the pond has heating unit, make water temperature be elevated to 30～40 ℃, enter anaerobic biological treatment then.
Anaerobic biological treatment adopts the UASB+AF method, bottom water distribution homogeneous, mud is equipped with in the inside, there is captation on structures top and the biogas collecting device is arranged, waste water stops 15 day time at anaerobic stages, and water outlet enters settling tank, and a post precipitation supernatant liquor part refluxes to enter and mixes the pond, reflux ratio is that (recirculation water: original waste water), another part flowed into the aerobe treatment system in 3: 1.CODcr is 5500mg/l in the waste water after anaerobic biological treatment.
The aerobe treatment system adopts the SBR method, in the insulation measure is arranged, make temperature be controlled at 20～28 ℃, aeration is cultivated, retention time of sewage 28 hours, its water outlet dissolved oxygen is controlled at more than the 2mg/l.The water outlet of aerobe treatment system enters the settling tank of back, the treatment stage that the water after the precipitation clarification flows into materialization.CODcr after aerobe is handled is 500mg/l.
The oxidizer hydrogen peroxide carries out oxidation in the current, and oxidization time is 4 hours, and the CODcr of water is 200mg/l after the oxidation, and last current are through active carbon layer, and CODcr is 150mg/l in the water, has reached emission standard.
Claims (7)
1, the treatment process of waste water for fumaric acid production is characterized in that in turn including the following steps:
Original waste water is through pre-treatment;
Anaerobic biological treatment;
Aerobe is handled;
Materialization is handled.
2, treatment process according to claim 1 is characterized in that original waste water at pretreatment stage, and it is 3.5～5.5 that pH value is regulated in cooling back, adds the recirculation water dilution of anaerobic biological treatment, makes CODcr in the waste water between 8000～12000mg/l.
3, treatment process according to claim 1 and 2 is characterized in that carrying out anaerobic biological treatment after waste water is warming up to 38～40 ℃ or 53～55 ℃.
4, treatment process according to claim 1 is characterized in that the anaerobic biological treatment time is 5～30 days, finishes after precipitate and carry out aerobe and handle.
5, treatment process according to claim 1, it is characterized in that refluxing through the water outlet of an anaerobic biological treatment part is used for the dilution of original waste water, with the reflux ratio of advancing waste water be 2～10: 1.
6, treatment process according to claim 1 is characterized in that the temperature when aerobe is handled is 20～28 ℃ or normal temperature, and the time is 0.5～16 day, water outlet dissolved oxygen 〉=2mg/l.
7, treatment process according to claim 1, it is characterized in that the materialization processing comprises oxide treatment and activated carbon adsorption processing, carry out oxide treatment through the water outlet that aerobe is handled through post precipitation adding strong oxidizer, make the content of the CODcr in the water after aerobe is handled reduce by 50～65% after the oxide treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011305770A CN1176033C (en) | 2001-12-03 | 2001-12-03 | Process for treating waste water for fumaric acid production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011305770A CN1176033C (en) | 2001-12-03 | 2001-12-03 | Process for treating waste water for fumaric acid production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1422818A true CN1422818A (en) | 2003-06-11 |
| CN1176033C CN1176033C (en) | 2004-11-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011305770A Expired - Fee Related CN1176033C (en) | 2001-12-03 | 2001-12-03 | Process for treating waste water for fumaric acid production |
Country Status (1)
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| CN (1) | CN1176033C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008055388A1 (en) * | 2006-11-07 | 2008-05-15 | Nanjing University | Method for the treatment of waste water from florfenicol production |
-
2001
- 2001-12-03 CN CNB011305770A patent/CN1176033C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008055388A1 (en) * | 2006-11-07 | 2008-05-15 | Nanjing University | Method for the treatment of waste water from florfenicol production |
| US7935256B2 (en) | 2006-11-07 | 2011-05-03 | Nanjing University | Method for the treatment of waste water from florfenicol production |
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| Publication number | Publication date |
|---|---|
| CN1176033C (en) | 2004-11-17 |
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