CN103771613B - Pretreatment method of cellulosic ethanol production wastewater - Google Patents
Pretreatment method of cellulosic ethanol production wastewater Download PDFInfo
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Abstract
The invention relates to a pretreatment method of cellulosic ethanol production wastewater, and the method is used in the treatment of organic wastewater, with high chroma, high content of suspended solids and high-concentration sulfate, produced in the ethanol production process by using vegetable fiber like corn straw as a raw material. The cellulosic ethanol production wastewater is subjected to a treatment flow comprising lime alkali precipitation, coagulation and clarification, and ozone oxidation process, and the treated outlet water has sulfate radical, suspended solids and chroma removed and gains improved biodegradability. The method provided by the invention can realize one-time removal of sulfate radicals, suspended solids and chroma of the organic wastewater with high chroma, high content of suspended solids and high-concentration sulfate, and improvement of the biodegradability of the wastewater, and can reduce the technical difficulty for subsequent biochemical treatment and inlet water pollution load.
Description
Technical field
The present invention relates to a kind of preprocess method of cellulose ethanol production wastewater, for being with Plant fiber such as corn straw
High chroma, high suspended matter, the process of high-concentration sulfuric acid salt organic waste water produced in raw material production ethanol process.
Background technology
With the worsening shortages of global fossil energy, the aggravation of environmental pollution, recycling economy and reduce the totality of carbon emission
Require, the exploitation of regenerative resource has become the theme in this epoch, and with Plant fiber such as corn straw, Sorghum vulgare Pers. straw stalks as original
Material production cellulose ethanol is one of important channel of regenerative resource exploitation.
Cellulose ethanol is typically with Plant fiber such as corn straw, Sorghum vulgare Pers. straw stalks as raw material, by steaming quick-fried pretreatment, fiber
The techniques such as enzyme hydrolysiss, saccharifying enzyme fermentation, ethanol rectification and dehydration obtain high purity ethanol, and mix and produce in gasoline component fuel
Alcohol product, as clean fuel for vehicle.In its production process, due to most hemicellulose in raw material（C5 is sugared）, wood
Quality can not be obtained by, the by-product such as the acetic acid of association, glycerol, lactic acid, furfural during adding so that final by ethanol
Float containing high concentration and dissolved organic matter in the mash of base product discharge.Meanwhile, it is to improve fiber in straw
Concentration of alcohol, alcohol product yield in hydrolysis efficiency, the fermentation liquid of element and reduce process energy consumption, enzyme preparation consumption and examine
Consider, steaming quick-fried pretreatment is often carried out in acid condition, i.e., after being impregnated to fibrous raw material with more than 1% sulphuric acid in advance
Carry out steaming quick-fried pretreatment, to reach effectively destruction straw in cellulose tissue structure purpose, and the sulphuric acid that the process is added
And in sequential hydrolysis, sweat and adjusting added sodium hydroxide（Piece alkali）Most deposited in the form of sulfate at last
In being ethanol distillation tower fermentation liquid, cellulose ethanol waste water is caused containing on the basis of high-enriched organics, and with height
The property of sulfate.Jing comprehensively detects and dissects that cellulose ethanol waste water is mainly derived from ethanol distillation tower fermentation liquid, its master
It is characterized as：Insoluble solid thing is high, and about 5%, the predominantly fine lignin of particle diameter, solid-liquid is not readily separated；Temperature is high, about
For 95 DEG C；Colourity is big；In acidity, pH value is 5 or so；The mg/L of COD about 130,000, predominantly dissolubility xylose, glycerol, acetic acid, wave
Send out phenol, lactic acid, lignin（Poly-ring aromatic compoundses）, furfural and various fermentation intermediate products；BOD5/ COD be 0.5~
0.55, if wherein bio-refractory thing and color development degree owner's aromatic compound；Inorganic salt content is about more than 2%, with sulphuric acid
Based on sodium, sulfate radical about 1%.Wherein, in waste water inorganic salt, sulfate radical, acetic acid, furfural, SS and lignin etc. are to standard biologic
Method process has serious inhibitory action.
For the high-concentration waste water that cellulose ethanol production process is produced, at present the main processing method for adopting is to high concentration
Waste water carries out anaerobic treatment, under anaerobic, the high-enriched organics in waste water is changed into into biogas（Methane, carbon dioxide
Gaseous mixture）Comprehensively utilized.As CN01808115.0 and US6555350 proposes to adopt up-flow anaerobic sludge blanket（UASB）
PROCESS FOR TREATMENT waste water, makes inhibitory substance carboxylic acid, furfural, furan, phenol in waste water etc. remove more than 80%, at least 5% after process
Waste water above is recycled, while producing biogas utilization by anaerobic fermentation.However, the inventive method is only applicable to place
Reason is neutral（Not acid adding）The cellulose ethanol waste water under quick-fried pre-treating process, the i.e. relatively low waste water of inorganic salt content are steamed, to acid
Property steam the process for the treatment of high-concentration saline organic wastewater under quick-fried pre-treating process because following two main causes are allowed to be not suitable for
Using.First, using it is acid steam it is quick-fried after ethanol distillation bottom of towe fermentation liquid in containing more than 2% inorganic salt, well beyond
Conventional anaerobic fermentation handling process is required（Inorganic salt is controlled below 1%）, in this situation, the life of anaerobic fermentation microbial bacteria
Long and activity is seriously suppressed, and even results in the failure of anaerobic treatment process；Secondly, the sulfate radical content in waste water is about 1
Ten thousand mg/L, well beyond the required value of anaerobic fermentation handling process（Sulfate radical is controlled in below 5000mg/L）, in this situation
Under, the sulfate radical in waste water will be reduced to the hydrogen sulfide of high concentration by anaerobe, so as to seriously suppress the first of high-enriched organics
Alkanisation sweat, causes biogas generation rate dramatic decrease, even can not produce biogas at all.For this kind of high concentration saliferous has
The method that the process of machine waste water is referred at present has two kinds, and first dilution is processed, i.e., it is diluted with hyposaline waste water, makes dirt
Dye thing concentration meets and processed after bioanalysises technological requirement.The characteristics of being produced due to cellulose ethanol（Straw consumption is big, conveying half
Footpath is little, rural area or suburb are founded the factory）Determine typically without optionally dilution water around it, therefore dilution processing method is difficult to fit
With；Additionally, even if there is dilution water is diluted process, the aromatic compound in the presence of waste water in biological treatment not yet
Can remove, and the high problem of effluent color dilution can be caused.It two is multiple-effect evaporation desalination, i.e., first waste water carried out at multiple-effect evaporation
Reason, the condensate after process carries out again anaerobic-aerobic treatment.This method is used at present corn fermentation production fuel alcohol
（Or edible ethanol）Field, although energy consumption is higher, can pass through to reclaim the high-quality feed with higher-value（DDGS）In addition
Compensation.And the key component in cellulose ethanol waste water is lignin and various organic and inorganic salts, albumen equal size is not reached
DDGS product indexs are required, it is difficult to reached high price and reclaimed（It is only capable of when general fuel utilization）, will significantly be increased using the handling process
Plus the production cost of cellulose ethanol.
Analyze based on more than, although being produced in technology, economy using the acid cellulose ethanol for steaming quick-fried pre-treating process
It is upper that there is larger advantage, but larger high-concentration sulfur-containing hydrochlorate treatment of Organic Wastewater problem is also accordingly brought, in waste water
High concentration sulphate, high chroma aromatic compound cause restriction to routine biochemistry process.
The content of the invention
The present invention is proposed a kind of for the water quality characteristicses of the acid cellulose ethanol base product mash for steaming quick-fried pretreatment route
The preprocess method of cellulose ethanol production wastewater.Method proposed by the present invention has high chroma, high suspended matter, high concentration sulfate
Organic wastewater is capable of achieving disposable decolouring, de- float, engaging sulphate and improves wastewater biodegradability effect, it is adaptable to fiber second
The pretreatment of the high concentration Organic Wastewater Containing Sulfate such as alcohol.
The preprocess method of cellulose ethanol production wastewater of the present invention includes three below processing unit：
（1）The analysis of Calx alkali process, from cellulose ethanol base product mash after cooling in pipe-line mixer with Calx
Breast is sufficiently mixed, and makes the sulfate radical in waste water that calcium sulfate precipitation reaction occur with lime cream, removes sulfate ion；
（2）Coagulation clarification process, step（1）Composite waste after process enters coagulation clarification pond, in coagulant and residue
Under the effect of lime cream flocculation aid, the calcium sulfate precipitation thing generated in water and original high concentration suspended matter are removed by clarifying；
（3）Ozone Oxidation Treatment, step（2）Waste water after process sends into ozone-oxidizing device, by ozone oxidation agent, will
Difficult for biological degradation Organic substance and color development degree thing in waste water is oxidized to the low-molecular material of biodegradability, reaches decolouring and improves useless
Water biodegradability purpose.
In the present invention, step（1）The analysis of Calx alkali control in processing the mixed liquor pH value of Calx and waste water reach 8.0~
10.0.The dosage of lime cream depends primarily on the pH controlling values of the sulfate radical equivalent concentration in waste water and waste water, and lime cream is excellent
Choosing adopts saturation lime cream.Waste water is sufficiently mixed in pipe-line mixer after being cooled to 50 DEG C with Calx, the sulphuric acid in waste water
There is chemical reaction and generate calcium sulphate crystal in radical ion, removed during subsequent coagulation clarification with Calx, blend
Water carries out coagulation clarification process.
In the present invention, step（2）Coagulation clarification process in hydraulic detention time of the waste water in coagulation clarification pond be 20~
60min.The pH value of the unit is always maintained at alkalescence, without regulation.The coagulant added in coagulation settling pool is conventional
Organic flocculant and inorganic flocculating agent, wherein organic flocculant are polyacrylamide, and dosage is 3~10mg/L；Inorganic flocculation
Agent can be using bodied ferric sulfate or ferric chloride, and dosage is 20~100mg/L.A water outlet part after coagulation clarification process
Ozone Oxidation Treatment is sent into, another part then returns step（1）Pipe-line mixer in circulate, with to hydroxide superfluous in water
Calcium is made full use of, and reduces the dosage of Calx.By the cell processing, original lignin, fermentation residue etc. in waste water
Float and step（1）Produced calcium sulfate precipitation thing can obtain deep removal, use aqueous suspension≤50mg/L, sulfur
Acid group≤500mg/L.
In the present invention, step（3）Ozone-oxidizing device using reaction tower or contact-oxidation pool, ozone oxidation agent by
Ozonator outside reason device is provided.The dosage of ozone oxidation agent be 20~50 mg/L waste water, preferably 30~40 mg/
L waste water；Ozone oxidation agent gas access concentration is 50~120 mg/L, preferably 100~120 mg/L；Waste water in reaction tower or
Hydraulic detention time in oxidation pond is 10~60min, preferably 20~30 min.Water outlet is mixed in pipeline after coagulation clarification process
Reaction tower or oxidation pond are entered by bottom after being sufficiently mixed with ozone oxidation agent in clutch, in the presence of ozone oxidation agent, is made
There is the senior oxidation reactions such as chain rupture, open loop, double bond in the macromolecule difficult for biological degradation Organic substance in waste water, change into low molecule
Organic substance, reaches the purpose for improving wastewater biodegradability and decolourizing, and the water outlet after process is arranged again by reaction tower or oxidation pond top
Entering conventional biological treatment unit carries out subsequent treatment.The waste water by ozone oxidation reaction of the unit is maintained at weak basic condition and carries out,
Keep pH value to be 8.0~10.0, be not required to adjust pH value, ozone is decomposed under alkalescence and produce the extremely strong hydroxyl of oxidisability certainly
By base, there is advanced oxidation reaction to the difficult for biological degradation thing in waste water and color development degree thing such as furfural, aromatic series etc., change into two
Carbonoxide, low molecular organic acidses etc., reach decolouring and improve BOD5The purpose of/COD.By the cell processing, the color in waste water
Degree can remove more than 90wt%, effluent color dilution≤30 degree；Water outlet BOD5/COD≥0.7；COD clearances >=40wt%.
The inventive method adopts the analysis of Calx alkali, coagulation clarification, ozone Oxidation Treatment technique, Jing to cellulose ethanol production wastewater
The water outlet high concentration suspended matter of said process process, sulfate radical, colourity obtain deep removal, and wastewater biodegradability is improved,
Follow-up routine biochemistry processing unit processes can be sent into, is born so as to mitigating the technical difficulty of subsequent biochemical process and entering water pollution
Lotus, has reached the purpose of pretreatment of High Concentration Wastewater.Method proposed by the present invention has high chroma, high suspended matter, high concentration sulfur
Hydrochlorate organic wastewater is capable of achieving disposable decolouring, de- float, engaging sulphate and improves wastewater biodegradability effect, it is adaptable to fine
The pretreatment of the high concentration Organic Wastewater Containing Sulfates such as dimension ethanol.
Description of the drawings
Fig. 1 is a kind of concrete fiber ethanol production wastewater pretreating process schematic flow sheet of the invention.
Wherein：1- pipe-line mixers；2- coagulation clarifications pond；3- ozone-oxidizing devices.
Specific embodiment
The specific embodiment of the inventive method is illustrated below in conjunction with accompanying drawing.In the present invention, wt% is quality point
Number.
As shown in Figure 1, cellulose ethanol production wastewater（From the mash of ethanol distillation bottom of towe, about 95 DEG C of temperature）Jing is cooled down
Pipe-line mixer 1 is continuously squeezed into pump to after less than 50 DEG C, being sufficiently mixed with lime cream carries out Calx alkali analysis process.By control
The addition of lime cream, adjusts the pH value of composite waste 8.0~10.0, the sulfate ion in waste water is occurred with lime cream
Chemical reaction, generates calcium sulphate crystal precipitation, and being re-fed into coagulation clarification pond 2 carries out coagulation clarification separation.Simultaneously to coagulation clarification
Continuous input inorganic flocculating agent and organic flocculant, make the high-concentration suspension such as original lignin, fermentation residue in waste water in pond 2
Calcium sulfate precipitation thing produced by thing and Calx alkali analysis process occurs in the presence of coagulant and superfluous lime cream flocculation aid
Coagulating sedimentation, float, sulfate ion in waste water etc. obtain deep removal, while COD also obtains part removal.Coagulation is clear
Water outlet after clear is in pipe-line mixer（It is unlisted in figure）In with from ozonator（It is unlisted in figure）Ozone oxidation agent
Send into ozone-oxidizing device 3 after being sufficiently mixed to process.In ozone-oxidizing device 3, in the presence of ozone oxidation agent, in waste water
Macromolecule difficult for biological degradation Organic substance and color development degree thing such as furfural, aromatic series etc. directly with ozone and its decompose produce hydroxyl
There is the senior oxidation reactions such as chain rupture, open loop, double bond oxidation in base free radical, be converted to carbon dioxide, low molecular organic acidses etc.
Biodegradability Organic substance, the biodegradability of waste water is strengthened, and is reached decolouring and is improved BOD5The purpose of/COD.Going out after process
Water enters conventional biological treatment unit and carries out subsequent treatment by reaction tower or oxidation pond top again.
Input lime cream can directly adopt saturation lime cream in Calx alkali analysis pipe-line mixer 1 of the present invention, also may be used
To be prepared with industrial quick lime, its dosage is depending on the sulfate radical equivalent concentration and pH controlling values in waste water after mixing 8.0
In the range of~10.0, such as 7~10 g/L.
The organic flocculant added in coagulation clarification pond 2 of the present invention be conventional polypropylene amide, dosage be 3~
10mg/L；Inorganic flocculating agent can be using bodied ferric sulfate or ferric chloride, and dosage is 20~100mg/L.Waste water is in coagulation
PH regulator need not be carried out in depositing reservoir 2, its hydraulic detention time is 20~60min.It is original in waste water by the cell processing
The suspended particulate substances such as lignin, fermentation residue and step（1）Calcium sulfate precipitation thing produced by the analysis of Calx alkali can obtain depth
Degree removing, can use aqueous suspension≤50 mg/L, turbidity≤10NTU, can meet follow-up ozone oxidation process to influent turbidity
With the index request of float control, ozone oxidation efficiency is set efficiently to be played.Meanwhile, using the processing unit, in water
Sulfate ion has obtained the removal of more than 95wt%, and water outlet sulfate radical≤500 mg/L can meet standard biologic method（Anaerobism,
It is aerobic etc.）The influent quality of subsequent treatment is required.
Ozone-oxidizing device of the present invention 3 is main by the group such as reaction tower or contact-oxidation pool, tail gas destruction facility
Into hydraulic detention time of the waste water in reaction tower or oxidation pond is 10~60min, preferably 20~30 min.Waste water is entering
To enter first uniformly mix with ozone oxidation agent in pipe-line mixer before ozone-oxidizing device 3, the dosage of ozone oxidation agent is 20
~50 mg/L waste water, preferably 30~40 mg/L waste water；The ozone oxidation agent gas access concentration for being added is 50~120
Mg/L, preferably 100~120 mg/L.Ozone oxidation reaction is maintained under weak basic condition pH8.0~10.0 and carries out, that is, be not required to
PH value is adjusted, ozone can so decomposed under alkalescence and is produced the extremely strong hydroxyl of oxidisability, to the biological drop of hardly possible in waste water
Solution thing and colourity oxidation efficiency are higher, reach higher decolouring and improve BOD5The purpose of/COD.As colourity can be removed
More than 90wt%, effluent color dilution≤30 degree, water outlet BOD5/ COD >=0.7, COD clearances >=40wt%.Because the water outlet after process is hanged
Float, sulfate radical, colourity, biodegradability etc. significantly improve, and can reduce the technical difficulty of follow-up routine biochemistry process and enter
Water pollution load.
The high chroma, high suspended matter, the treating high-concentration saline organic wastewater that produce are produced to cellulose ethanol using the inventive method
Using Calx alkali analysis-coagulation clarification-ozone Oxidation Treatment flow process, water outlet after process reaches deep removal sulfate radical, float, color
Spend and improve biodegradability purpose.Method proposed by the present invention has high chroma, high suspended matter, high-concentration sulfuric acid salt organic waste water
It is capable of achieving disposably de- float, colourity, sulfate radical and improves wastewater biodegradability, the skill that follow-up routine biochemistry is processed can be mitigated
Art difficulty and water inlet pollutional load.
The inventive method and effect are further illustrated below by embodiment.
Embodiment 1
At cellulose ethanol process units waste water of the processing method of the present invention to domestic certain medium-sized test scale
Reason.Waste water is the acid cellulose ethanol base product mash for steaming quick-fried preprocess method, and waste water is mainly characterized by：SS（Float）
50000 mg/L、COD（Chromium method, similarly hereinafter）129050 mg/L、BOD568600 mg/L, the mg/L of sulfate radical 9290, colourity
12000 degree, pH 4.7, BOD5/ COD is 0.53.
Pretreatment is carried out to above-mentioned waste water using the Calx alkali analysis-coagulation clarification-ozone oxidation group technology of the present invention, is given up
Water process scale is 100 L/h, and the major experimental device of each processing unit is constituted, service condition and treatment effect are shown in Table 1.
The main processing units of the embodiment 1 of table 1 are constituted and treatment effect
| Processing unit title | Processing meanss scale and main composition | Main service condition and control parameter | Process water outlet or effect |
| Calx alkali is analysed | Pipe-line mixer, material PVC. | Wastewater flow 100L/h；Add saturation lime cream 7.5g/L；Mixed liquor pH value 8.5. | |
| Coagulation clarification pond | PVC materials, volume 100L, built-in stirring Device is stirred to flocculant. | Wastewater flow 100L/h；Add bodied ferric sulfate 30mg/L, polyacrylamide 5mg/L；Mixed liquor pH value 8.5.Waste water hydraulic detention time 40min. | Water outlet sulfate radical 475mg/L, SS 48mg/L, turbidity are not more than 10, COD 95g/ L、BOD5For 58g/L, 11600 degree of colourity, BOD5/ COD is 0.61, pH 8.6. |
| Ozone-oxidizing device | PVC material baffling reaction tanks, effectively appearance Product 50L, external ozonator. | Wastewater flow 100L/h；Ozone dosage 30mg/L, ozone pond entrance concentration 120 mg/L；Waste water hydraulic detention time 20min；Mixed liquor pH value 8.2. | Water outlet sulfate radical 475mg/L, SS 48mg/L, COD 75g/L, BOD5For 57.5g/L, 30 degree of colourity, BOD5/ COD is 0.76, pH 8.2. |
After method of the present invention process, sulfate radical≤500 mg/L, SS in cellulose ethanol waste water≤50 mg/L,
Colourity≤30 degree, BOD5/ COD >=0.7, COD clearances >=40wt%, can meet the inflow requirement into routine biochemistry process,
And make inlet COD loading reduce more than 40wt%.
Embodiment 2
Using the processing meanss of embodiment 1, waste water same as Example 1 is processed, change the operation bar of each processing unit
The water treatment effect that part is obtained is shown in Table 2.
The main processing units of the embodiment 2 of table 2 are constituted and treatment effect
| Processing unit title | Processing meanss scale and main composition | Main service condition and control parameter | Process water outlet or effect |
| Calx alkali is analysed | Pipe-line mixer, material PVC. | Wastewater flow 100L/h；Add saturation lime cream 9.5g/L；Mixed liquor pH value 9.5. | |
| Coagulation clarification pond | PVC materials, volume 100L, built-in stirring Device is stirred to flocculant. | Wastewater flow 100L/h；Add ferric chloride 40mg/L, polyacrylamide 5mg/ L；Mixed liquor pH value 9.5.Waste water hydraulic detention time 40min. | Water outlet sulfate radical 400mg/L, SS 45mg/L, turbidity≤10, COD 92g/L, BOD5 For 58g/L, 10200 degree of colourity, BOD5/ COD is 0.63, pH 9.6. |
| Ozone-oxidizing device | PVC material baffling reaction tanks, effectively appearance Product 50L, external ozonator. | Wastewater flow 100L/h；Ozone dosage 40mg/L, ozone pond entrance concentration 100 mg/L；Waste water hydraulic detention time 30min；Mixed liquor pH value 9.2. | Water outlet sulfate radical 400mg/L, SS 45mg/L, COD 77g/L, BOD5For 55g/ L, 20 degree of colourity, BOD5/ COD is 0.71, pH 9.2. |
After method of the present invention process, sulfate radical≤500 mg/L, SS in cellulose ethanol waste water≤50 mg/L,
Colourity≤30 degree, BOD5/ COD >=0.7, COD clearances >=40wt%, can meet the inflow requirement into routine biochemistry process,
And make inlet COD loading reduce more than 40wt%.
Comparative example
Using the processing meanss of embodiment 1, waste water in the same manner as in Example 1 is processed, in not feeding lime alkali condition is analysed
Coagulation clarification and ozone Oxidation Treatment are directly carried out down, and the water treatment effect of acquisition is shown in Table 3.
The main processing units of the comparative example of table 3 are constituted and treatment effect
| Processing unit title | Processing meanss scale and main composition | Main service condition and control parameter | Process water outlet or effect |
| Coagulation clarification pond | PVC materials, volume 100L, it is built-in to stir Mix device to stir flocculant. | Wastewater flow 100L/h；Add bodied ferric sulfate 30mg/L, polyacrylamide 5mg/L；Mixed liquor pH value 4.7.Waste water hydraulic detention time 40min. | Water outlet is muddy, and precipitation is incomplete；Water outlet sulfate radical 9205mg/L, SS >=30g/L, COD 105g/L、BOD5For 63g/L, colourity 11800, BOD5/ COD is 0.60, pH 4.8. |
| Ozone-oxidizing device | PVC material baffling reaction tanks, effectively Volume 50L, external ozonator. | Wastewater flow 100L/h；Ozone dosage 35mg/L, ozone pond entrance concentration 110 mg/L；Waste water hydraulic detention time 20min；Mixed liquor pH value 4.8. | Water outlet is muddy, and precipitation is incomplete；Sulfate radical 9175mg/L, SS >=30g/L, COD 102g/L、BOD5For 62.5g/L, 550 degree of colourity, BOD5/ COD is 0.61, pH 4.6. |
As shown in Table 3, if cellulose ethanol waste water does not carry out Calx alkali analysis, removal effect is undesirable.Sulphuric acid in waste water
Root, SS, colourity, COD etc. can not meet water outlet requirement.
Claims (9)
1. a kind of preprocess method of cellulose ethanol production wastewater, it is characterised in that including following process：
（1）The analysis of Calx alkali is processed, and is filled with lime cream in pipe-line mixer after cooling from cellulose ethanol base product mash
Divide mixing, make the sulfate radical in waste water that calcium sulfate precipitation reaction, removing sulfate ion occur with lime cream；Control lime cream and
The pH value of the mixed liquor of waste water reaches 8.0~10.0；
（2）Coagulation clarification process, step（1）Composite waste after the analysis of Calx alkali is processed enters coagulation clarification pond, in coagulant and
Under remaining lime cream flocculation aid effect, the calcium sulfate precipitation thing generated in water and original high concentration suspended matter are gone by clarification
Remove；The coagulant for being added is organic flocculant and inorganic flocculating agent, and wherein organic flocculant is polyacrylamide, and dosage is
3~10mg/L；Inorganic flocculating agent is bodied ferric sulfate or ferric chloride, and dosage is 20~100mg/L；
（3）Ozone Oxidation Treatment, step（2）Waste water after process sends into ozone-oxidizing device, by ozone oxidation agent, by waste water
In difficult for biological degradation Organic substance and color development degree thing be oxidized to the low-molecular material of biodegradability, reach decolouring and improve waste water can
Biochemical purpose.
2. in accordance with the method for claim 1, it is characterised in that：Step（1）The dosage of lime cream in Calx alkali analysis process
Depend primarily on the pH controlling values of sulfate radical equivalent concentration in waste water and waste water.
3. according to the method described in claim 1 or 2, it is characterised in that：Step（1）Lime cream adopts full during the analysis of Calx alkali is processed
And lime cream.
4. in accordance with the method for claim 1, it is characterised in that：Step（2）Waste water is in coagulation clarification in coagulation clarification process
Hydraulic detention time in pond is 20~60min.
5. in accordance with the method for claim 1, it is characterised in that：Step（2）A water outlet part after coagulation clarification process is sent
Enter ozone Oxidation Treatment, another part then returns step（1）Pipe-line mixer in circulate.
6. in accordance with the method for claim 1, it is characterised in that：Step（3）Ozone-oxidizing device is using reaction tower or connects
Tactile oxidation pond, ozone oxidation agent by processing meanss outside ozonator provide.
7. according to the method described in claim 1 or 6, it is characterised in that：The dosage of ozone oxidation agent, is that 20~50mg/L gives up
Water, the gas access concentration of ozone oxidation agent is 50~120mg/L；Hydraulic detention time of the waste water in reaction tower or oxidation pond
For 10~60min.
8. according to the method described in claim 1 or 6, it is characterised in that：The dosage of ozone oxidation agent, is that 30~40mg/L gives up
Water, the gas access concentration of ozone oxidation agent is 100~120mg/L；During hydraulic retention of the waste water in reaction tower or oxidation pond
Between be 20~30min.
9. according to the method described in claim 1 or 6, it is characterised in that：Step（3）Ozone oxidation reaction is maintained at alkalescence bar
Part is carried out, that is, keep pH value to be 8.0~10.0.
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| CN105060546B (en) * | 2015-07-22 | 2017-07-04 | 中国民用航空总局第二研究所 | A kind of processing method of containing alcohol waste water |
| CN105712453B (en) * | 2016-02-01 | 2018-08-28 | 天津理工大学 | A kind of desalination method of the potassium sulfate containing high concentration and aqueous sodium persulfate solution |
| CN107365030A (en) * | 2017-08-31 | 2017-11-21 | 宜宾海丝特纤维有限责任公司 | It is a kind of to handle half fine method and apparatus in viscose glue sewage |
| CN108147577A (en) * | 2017-12-07 | 2018-06-12 | 青岛华拓科技有限公司 | A kind of sewage water treatment method and sewage-treating agent |
| CN108083502A (en) * | 2017-12-27 | 2018-05-29 | 江苏开放大学 | A kind of preprocess method of high concentration sulfate-aniline/nitrobenzene wastewater |
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| US6932909B2 (en) * | 2002-01-15 | 2005-08-23 | Kroff Chemical Company, Inc. | Method of treating mine drainage |
| CN101372382A (en) * | 2008-08-29 | 2009-02-25 | 北京桑德环保集团有限公司 | Advanced treatment method and processing system for wastepaper pulping and papermaking waste water |
| CN101693569A (en) * | 2009-10-16 | 2010-04-14 | 上海联喆控制设备有限公司 | Device for catalyzing and oxidating ozone effectively |
| CN102381787A (en) * | 2011-05-31 | 2012-03-21 | 南京大学 | Decoloration method for fermentation wastewater biochemical treatment tail water |
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