CN104529085A - Fat and oil hydrolysis waste water treatment method - Google Patents
Fat and oil hydrolysis waste water treatment method Download PDFInfo
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- CN104529085A CN104529085A CN201410853887.9A CN201410853887A CN104529085A CN 104529085 A CN104529085 A CN 104529085A CN 201410853887 A CN201410853887 A CN 201410853887A CN 104529085 A CN104529085 A CN 104529085A
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Abstract
The invention relates to a fat and oil hydrolysis waste water treatment method, in particular to a treatment method of high-concentration fat and oil hydrolysis waste water produced in a soap grain production process. The treatment method mainly includes step 1, wherein a strong-oxidization pretreatment unit is involved, and the step 1 comprises a Fenton processing step and an air-flotation treatment step; step 2, wherein an anaerobic or facultative anaerobic treatment unit is involved; and step 3, wherein an aerobic treatment unit is involved. In a preferred embodiment, step 4 is also included, wherein a sludge treatment unit is involved. According to the fat and oil hydrolysis waste water treatment method, by removing the wrapping effect of fat and oil, the biodegradability of waste water is improved, and the front-end chemical oxygen demand (COD) load is cut down; it is ensured that the water quality of the waste water entering a biological treatment unit is stable and controllable; by means of further microbiological treatment through the biological treatment unit, the chemical oxygen consumption of the waste water is reduced, and operating cost and treatment cost are lowered.
Description
Technical field
The invention belongs to technical field of waste water processing, relate to a kind of high-concentration grease hydrolyzed waste water treatment process particularly.
Background technology
Tallow Inedible Grade is utilized to produce in the process of neat soap will produce a large amount of fat hydrolysis waste water by method for hydrolysis, this chemical oxygen demand of waste water high (5000-10000mg/L), be difficult to biochemistry (B/C < 0.1)=feature, grease wherein, package action will be produced to mud or microbial film, affect processing efficiency and cause the settling property of mud to decline, and soap stock wherein easily produces a large amount of foams, affect the processing efficiency of biochemical system and the outward appearance of sewage plant.The fat hydrolysis waste water of high density directly enters biochemical system simultaneously, very easily produces to impact to sewage plant even to make whole biochemical system paralyse, and affects the normal operation of enterprise.
Summary of the invention
For the above defect of prior art, the invention provides the method for wastewater treatment that a kind of fat hydrolysis produces, by abolishing package action, the lifting waste water biodegradability of grease and cutting down the measures such as front end chemical oxygen demand load, effective solution fat hydrolysis waste water on the impact of sewage plant and impact, lifting sewage station run stability.
For reaching above-mentioned technical purpose, the present invention adopts following a kind of fat hydrolysis method for waste water: it mainly comprises the following steps:
S1: Strong oxdiative pretreatment unit: this step comprises Fenton treatment step and air supporting treatment step; S2: anaerobism or double oxygen processing unit; And S3: aerobic treatment unit.
Described Fenton treatment step can effectively reduce the chemical oxygen demand in waste water and improve the biodegradability of waste water, and air-flotation process step can remove the suspended substance produced in reaction, reduces the chemical oxygen demand of waste water further.
Further, also comprise step S4 sludge treating block: after the process of step S1 Strong oxdiative pretreatment unit, after S2 anaerobism or double oxygen processing unit processes or the mud produced after the process of S3 aerobic treatment unit insert sludge thickener, enter sludge dewatering equipment after concentrated and carry out dewatering.
Further, the waste water after described step S3 process enters settling tank, qualified discharge after removal suspended substance.
Preferably, in described Fenton treatment step, the mass ratio of oxygenant and catalyzer is 2:1 to 10:1, and oxygenant dosage is 1 ~ 4kg/m
3waste water, COD controls at 3000 ~ 10000mg/L.
Particularly, catalyzer described in described Fenton process should for having the metal of characteristic of appraising at the current rate and oxide compound thereof and salt, or the mixture of above-mentioned substance, as being selected from one or more materials in ferric sulfate, iron nitrate, iron(ic) chloride, ferrous sulfate, Z 250, ferric oxide, cupric oxide, cuprous chloride, cupric nitrate.
Preferably, described Fenton process carries out ultra violet lamp simultaneously.
In order to optimize air-flotation process condition, regulate the pH-value of waste water in step S1 before air-flotation process, pH value is adjusted to 7 ~ 8.Because will add coagulating agent before air-flotation process, for guaranteeing coagulation effect, its pH regulator is necessary, simultaneously also for meeting the pH needs of subsequent biochemical process.
Preferably, described air-flotation process is air-dissolving air-float process, and the residence time is 10-60 minute.
More specifically, described step S2 adopts acidication to hold concurrently oxygen or anaerobic biochemical treatment system, decomposes macromole organic pollutant further, guarantees follow-up aerobic unit processing efficiency.
More specifically, described step S3 adopts catalytic oxidation aerobic treatment system, can certainly adopt the processing efficiency that multiple aerobic treatment array configuration reaches best.
Preferably, the aerobic treatment unit residence time was at 10 ~ 48 hours at 12 ~ 48 hours described anaerobism or the double oxygen processing unit residence time.
Beneficial effect of the present invention:
By high-concentration grease hydrolyzed waste water treatment process of the present invention abolished grease package action, promote this wastewater biodegradability and cut down front end chemical oxygen demand load, effectively solve fat hydrolysis waste water to the impact of sewage plant and impact, the stability that lifting sewage station is run.
Accompanying drawing explanation
Fig. 1 is the flow chart illustration of high-concentration grease hydrolyzed waste water treatment process of the present invention.
Fig. 2 is the embodiment of the present invention 1 chemical oxygen demand test result after Strong oxdiative pre-treatment, also can be described as H
2o
2-FeSO
4-PAC enlarged experiment is tested.
Fig. 3 is the embodiment of the present invention 1 chemical oxygen demand test result after Strong oxdiative pre-treatment.This Fenton process without without ultra violet lamp, FeSO
4with H
2o
2mass ratio is 1:4, H
2o
2injected volume is 3Kg/m
3, polymerize aluminum chloride (PAC) is 0.1g/L, and the pH value of waste water is 4.Please note: last point of numerical curve is the data adding PAC coagulation after reaction precipitation.
Embodiment
In order to make the object, technical solutions and advantages of the present invention definitely, below the preferred embodiments of the present invention are described in detail.
As shown in Figure 1, the present invention adopts following a kind of fat hydrolysis method for waste water, and it mainly comprises following treatment step: S1: Strong oxdiative pretreatment unit; S2: anaerobism or double oxygen processing unit; And S3: aerobic treatment unit.Preferably S4 sludge treating block is also comprised as one.Wherein, step S1 comprises Fenton treatment step and air supporting treatment step.
Described Fenton treatment step can effectively reduce the chemical oxygen demand in waste water and improve the biodegradability of waste water, and air-flotation process step can adopt the modes such as air-dissolving air-float, jet air float and electrofloatation, can the suspended substance produced in reaction be removed, reduce the chemical oxygen demand of waste water further.Wherein be preferably air-dissolving air-float, the residence time is 10-60 minute, preferably 30 minutes.
The concrete operations of step S1 are as follows: high-concentration grease hydrolyzed waste water is (now the pH of waste water refers to be generally 4) after preliminary oil removal, squeeze in Fenton reactor with volume pump, simultaneously according to the chemical oxygen demand of water inlet, add appropriate oxygenant and catalyzer, react after 30-300 minute, adjust ph, to 7 ~ 8, enters air floatation machine, and air floatation machine is by removing suspended substance after air supporting.Preferably, in described Fenton treatment step, the mass ratio of oxygenant and catalyzer is 2:1 to 10:1, and oxygenant dosage is 1 ~ 4kg/m
3waste water, COD controls at 3000 ~ 10000mg/L.In order to optimize air-flotation process condition, regulate the pH-value of waste water in step S1 before air-flotation process, pH value is adjusted to 7 ~ 8.Because will add coagulating agent before air-flotation process, for guaranteeing coagulation effect, its pH regulator is necessary, simultaneously also for meeting the pH needs of subsequent biochemical process.And the floating process of the coagulating agent such as the general selective polymerization aluminum chloride of coagulating agent, bodied ferric sulfate, its consumption be 50 ~ 500mg/L preferably, described Fenton process carries out ultra violet lamp simultaneously.Ultraviolet lamp is a kind of form of catalyzer, belongs to intensive treatment or optimal conditions, can promote processing efficiency about 5%, and its treatment effect not adopting ultra violet lamp as shown in Figure 2.
Described step S2 adopts acidication to hold concurrently oxygen or anaerobic biochemical treatment system, decomposes macromole organic pollutant further, guarantees follow-up aerobic unit processing efficiency.Anaerobic reactor can adopt up-flow anaerobic sludge blanket (USAB, Up-flowAnaerobic Sludge Bed), anaerobic baffled reactor (ABR, Anaerobic BaffLted Reactor), the form such as EGSB (expanded granular sludge bed) (EGSB, Expanded Granular Sludge Bed).
Described step S3 adopts catalytic oxidation aerobic treatment system, can certainly adopt the processing efficiency that multiple aerobic treatment array configuration reaches best.The aerobic treatment systems such as catalytic oxidation, active sludge, oxidation pond can be adopted, single or the combination of multiple aerobic treatment and improved form thereof can be adopted to reach best processing efficiency in aerobic treatment.
Described step S4 sludge treating block specific practice is: after step S1 process, or after step S3 process, or the mud produced after step S4 process inserts sludge thickener, enters sludge dewatering equipment and carry out dewatering after concentrated.Waste water after step S3 process then enters settling tank, qualified discharge after removal suspended substance.
Embodiment 1
Get 160kg waste water in reactor, the COD of this waste water is about 9072mg/L, and original pH is 4), by 3kg/m
3hydrogen peroxide throwing amount, the concentration of hydrogen peroxide is 30%, and hydrogen peroxide and ferrous sulfate are 10:1 according to mass ratio, 8:1, the dosage of 6:1,4:1,2:1 adds wherein, it is about 8 that unlatching 80w ultraviolet lamp reacts adjust ph after 80 minutes, the polymerize aluminum chloride adding 200mg/L carries out coagulation, and get supernatant liquid filtering and measure chemical oxygen demand, experimental result as shown in Figure 2, wherein B/C rises to 0.3 by original 0.02, and the COD after coagulation is 3000mg/L.
Embodiment 2
By 15m
3the treatment capacity (COD is 5500-7500mg/L) of/h, water inlet arrives Fenton's reaction system, and according to surveyed chemical oxygen demand, the dosage being 4:1 in hydrogen peroxide and ferrous sulfate ratio adds medicament, and the concentration of hydrogen peroxide is 30%, and dosage is 2kg/m
3, continuum micromeehanics, the residence time of Fenton's reaction is 90 minutes, and add polymerize aluminum chloride by 100mg/L dose after reaction terminates, adjust ph is the laggard row air-flotation process of 7-8, and air-flotation process adopts air-dissolving air-float, and the residence time is 30 minutes.After air supporting, water outlet COD is 1600-2000mg/L, waste water enters anaerobism or double oxygen processing unit afterwards, the residence time is 20 hours, and aerobic treatment unit (catalytic oxidation) and sludge treating block (total residence time is 24 hours, biochemical treatment unit, i.e. anaerobism or double oxygen processing unit and aerobic treatment unit, for raw wastewater treatment system, directly intake after pre-treatment, do not carry out special domestication, sludge treating block plays preliminary object of cutting down COD load, effectively suppress the soap bubble produced simultaneously, catalytic oxidation because of its biotic level enrich, play the object of advanced treatment), actual waste water runs about 1 month continuously, water outlet is (COD is 110-150mg/L) discharge after rectangular sedimentation tank precipitation.Period gas floating and biochemical treatment produce mud concentrated by sludge thickener after, through sludge dewatering equipment processed, gained dewatered sludge outward transport deal carefully with.
Obviously, the above embodiment of the present invention is only for example of the present invention is clearly described, and is not the restriction to embodiments of the present invention.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here cannot give exhaustive to all embodiments.Every belong to technical scheme of the present invention the apparent change of extending out or variation be still in the row of protection scope of the present invention.
Claims (10)
1. a treatment process for fat hydrolysis waste water, is characterized in that: mainly comprise the following steps:
S1: Strong oxdiative pretreatment unit: this step comprises Fenton treatment step and air supporting treatment step;
S2: anaerobism or double oxygen processing unit; And
S3: aerobic treatment unit.
2. the treatment process of fat hydrolysis waste water as claimed in claim 1, it is characterized in that, also comprise step S4 sludge treating block: after the process of step S1 Strong oxdiative pretreatment unit, after S2 anaerobism or double oxygen processing unit processes or the mud produced after the process of S3 aerobic treatment unit insert sludge thickener, enter sludge dewatering equipment after concentrated and carry out dewatering.
3. the treatment process of fat hydrolysis waste water as claimed in claim 1, it is characterized in that, the waste water after described step S3 process enters settling tank, qualified discharge after removal suspended substance.
4. the treatment process of fat hydrolysis waste water as claimed in claim 1, it is characterized in that, the mass ratio adding oxygenant and catalyzer in described Fenton treatment step is 2:1 to 10:1, and oxygenant dosage is 1 ~ 4kg/m
3waste water, COD controls at 3000 ~ 10000mg/L.
5. the treatment process of fat hydrolysis waste water as claimed in claim 4, it is characterized in that, catalyzer is selected from one or more the material in ferric sulfate, iron nitrate, iron(ic) chloride, ferrous sulfate, Z 250, ferric oxide, cupric oxide, cuprous chloride, cupric nitrate.
6. the treatment process of fat hydrolysis waste water as claimed in claim 1, it is characterized in that, described Fenton process carries out ultra violet lamp simultaneously.
7. the treatment process of fat hydrolysis waste water as claimed in claim 1, is characterized in that, regulate the potential of hydrogen of waste water in step S1 before air-flotation process, pH value is adjusted to 7 ~ 8.
8. the treatment process of the fat hydrolysis waste water as described in claim 1 or 7, is characterized in that, described air-flotation process is air-dissolving air-float process, and the residence time is 10-60 minute.
9. the treatment process of fat hydrolysis waste water as claimed in claim 1, is characterized in that,
Step S2 adopts acidication to hold concurrently oxygen or anaerobic biochemical treatment system; Step S3 adopts catalytic oxidation aerobic treatment system.
10. the treatment process of the fat hydrolysis waste water as described in claim 1 or 9, is characterized in that, described anaerobism or the double oxygen processing unit residence time, the aerobic treatment unit residence time was at 10 ~ 48 hours at 12 ~ 48 hours.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106186551A (en) * | 2016-08-25 | 2016-12-07 | 常州市锦云工业废弃物处理有限公司 | A kind of multipurpose wastewater treatment equipment processing equipment |
| CN106673095A (en) * | 2017-02-21 | 2017-05-17 | 广东产品质量监督检验研究院 | Kitchen waste oil-water separation apparatus and oil-water separation method thereof |
| CN106698850A (en) * | 2017-01-19 | 2017-05-24 | 广州市海珥玛植物油脂有限公司 | Treatment device and treatment method of epoxy plasticizer waste water |
| CN108751344A (en) * | 2018-08-09 | 2018-11-06 | 孙鹏 | A kind of batch type processing system and treatment process of industrial wastewater middle and high concentration COD |
| CN109179917A (en) * | 2018-11-14 | 2019-01-11 | 湖南省银鑫油茶开发有限公司 | The wastewater treatment method of oil tea oil expression |
| CN109231722A (en) * | 2018-11-16 | 2019-01-18 | 郑州轻工业学院 | A kind of processing method being machined emulsifiable oil waste water |
| CN110697995A (en) * | 2019-10-31 | 2020-01-17 | 中冶华天工程技术有限公司 | Cellulose ethanol wastewater treatment process and system |
| CN117228904A (en) * | 2023-11-14 | 2023-12-15 | 天俱时工程科技集团有限公司 | Chemical synthesis pharmaceutical wastewater pretreatment method based on photocatalytic oxidation technology |
| WO2024040684A1 (en) * | 2022-08-24 | 2024-02-29 | 博瑞德环境集团股份有限公司 | Chemical wastewater treatment device using microbial sludge granules |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186551A (en) * | 2016-08-25 | 2016-12-07 | 常州市锦云工业废弃物处理有限公司 | A kind of multipurpose wastewater treatment equipment processing equipment |
| CN106698850A (en) * | 2017-01-19 | 2017-05-24 | 广州市海珥玛植物油脂有限公司 | Treatment device and treatment method of epoxy plasticizer waste water |
| CN106673095A (en) * | 2017-02-21 | 2017-05-17 | 广东产品质量监督检验研究院 | Kitchen waste oil-water separation apparatus and oil-water separation method thereof |
| CN108751344A (en) * | 2018-08-09 | 2018-11-06 | 孙鹏 | A kind of batch type processing system and treatment process of industrial wastewater middle and high concentration COD |
| CN109179917A (en) * | 2018-11-14 | 2019-01-11 | 湖南省银鑫油茶开发有限公司 | The wastewater treatment method of oil tea oil expression |
| CN109231722A (en) * | 2018-11-16 | 2019-01-18 | 郑州轻工业学院 | A kind of processing method being machined emulsifiable oil waste water |
| CN109231722B (en) * | 2018-11-16 | 2021-10-29 | 郑州轻工业学院 | Method for treating emulsified oil wastewater in mechanical processing |
| CN110697995A (en) * | 2019-10-31 | 2020-01-17 | 中冶华天工程技术有限公司 | Cellulose ethanol wastewater treatment process and system |
| WO2024040684A1 (en) * | 2022-08-24 | 2024-02-29 | 博瑞德环境集团股份有限公司 | Chemical wastewater treatment device using microbial sludge granules |
| CN117228904A (en) * | 2023-11-14 | 2023-12-15 | 天俱时工程科技集团有限公司 | Chemical synthesis pharmaceutical wastewater pretreatment method based on photocatalytic oxidation technology |
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