CN104803559A - Method for treating ultraviolet absorber UV-531 production waste water - Google Patents
Method for treating ultraviolet absorber UV-531 production waste water Download PDFInfo
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Abstract
The invention is a method for treating ultraviolet absorber UV-531 waste water. Specifically, the method includes the following steps: oil insulative deposition, pre-neutralization, extraction, back extraction, stage I A/O and stage II A/O. After oil slick and suspended solids in waste water are removed through oil insulative deposition, an extraction agent which is specially selected is used for extracting the organic matters, namely, 2,4-dihydroxybenzophenone and 2-hydroxy-4-n-octyloxybenzophenone, which are difficult to biodegrade in the waste water, alkali liquor is adopted for back extraction of an extract phase which can be reused after recycling, and a strip liquor is used for recycling organic matters; the raffinate and sanitary sewage are subjected to homogeneous regulation in quality and amount, matched nutrient elements are added, and then the mixed liquid obtained is introduced into a two-stage A/O biochemical system for biodegradation by domesticated and cultured microorganism. The method provided by the invention is a physicochemical-biochemical combined method, and is reasonable in design and high in operability.
Description
Technical field
The present invention relates to a kind of Chemicals production wastewater treatment method, the method for the waste water produced in the method process ultraviolet absorbent UV-531 production process that specifically one utilizes materialization-biochemistry to combine.
Background technology
Ultraviolet absorbent UV-531 belongs to the efficient anti-aging auxiliary agent of performance brilliance, can absorb the UV-light of certain wavelength, can delay material yellowing as UV light stabilizing agent.Therefore, be widely used in the plastic material such as PE, PVC, PP, PS, PC, synthetic glass, polypropylene fiber and ethene, acetic acid, vinyl acetate to produce.Its factory effluent belongs to typical high density organic acidity used water difficult to degradate, and its features of pollution is as follows: (1) organic pollutant concentration level is high, and COD is at 10,000 more than mg/L, main containing organism such as phenol system thing, benzene homologues, alcohols, acid amides in waste water.(2) composition contained by waste water has bio-toxicity or inhibition, and biodegradability is poor, cannot directly adopt biochemical method to process.(3) acid strong, containing a large amount of chlorine root.(4) waste discharge change in concentration is large.
Domestic and international less about this kind of wastewater treatment research at present, for accomplishing the process of waste water environment protection standard, the method for evaporating that enterprise's more options are traditional carries out analysing salt, and a large amount of steam of its technological process consumption, cost for wastewater treatment are high.And evaporation precipitation mostly is abraum salt, abraum salt processing cost is high, easily produces secondary pollution.
Summary of the invention
Technical problem to be solved by this invention is for the deficiencies in the prior art, provides the treatment process of the ultraviolet absorbent UV-531 factory effluent that a kind of technological design is reasonable, extraction efficiency is high, secondary pollution is little.
Technical problem to be solved by this invention is realized by following technical scheme.The present invention is a kind for the treatment of process of ultraviolet absorbent UV-531 factory effluent, is characterized in, its step is as follows:
(1) oil removal precipitation: first carry out oil removal precipitation process to ultraviolet absorbent UV-531 factory effluent, removes contained oil slick and suspended substance in waste water;
(2) pre-neutralization: regulate waste water ph to 0.6 ~ 4 with water soluble alkali solution, pre-neutralization is carried out to the waste water through oil removal process;
(3) extract: fully mix under waste water normal temperature and pressure by profit phase volume ratio 4:1 ~ 1:8 with extraction agent, after layering, namely extracting phase extracts rear water and enters step (5) adjustment, and extraction phase and loaded extractant send step (4) reextraction regeneration; Extraction progression one-level, described extraction agent is for being selected from phosphoric acid ester, alkyl amine, sec-octyl alcohol, kerosene or diesel oil;
(4) strip: fully mix with alkali lye under getting above-mentioned extraction phase normal temperature and pressure, caustic dosage is to control to be as the criterion 8 ~ 11 by pH end point values, after layering, strip liquor acid out reclaims product 2,4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, extraction agent after regeneration recycles in extraction workshop section, reextraction progression one-level; Described alkali lye is NaOH or 5% ~ 30%KOH solution of mass concentration 5% ~ 30%;
(5) regulate: after extraction, water sends into biochemical system equalizing tank, carries out homogeneous, all measures adjustment, neutralize and control pH to 6.5 ~ 8.5 with water soluble alkali solution, and according to mass ratio BOD
5: N:P=100:5:1 proportioning adds nutritive element; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(6) one-level A/O: equalizing tank waste water is entered biochemical system one-level A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 3 ~ 4 hours residence time,
O pond controls dissolved oxygen Do at 1 ~ 1.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 15 ~ 20 hours residence time, the mixed solution after one-level A/O process is through sedimentation layering, and settled sludge partial reflux enters anoxic reacter, part, through concentration and settlement, is arranged outside after press filtration;
(7) secondary A/O: one-level A/O water outlet enters secondary A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 3 ~ 4 hours residence time, O pond controls dissolved oxygen Do at 2 ~ 4mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 5 ~ 8 hours residence time, mixed solution after secondary A/O process is through sedimentation layering, settled sludge partial reflux enters anoxic reacter, and part, through concentration and settlement, is arranged outside after press filtration, after supernatant liquor adds the process of coagulating agent reaction precipitation, Chinese effluent.
In the treatment process technical scheme of ultraviolet absorbent UV-531 factory effluent of the present invention, preferred technical scheme or technical characteristic are further:
1. in step (2): preferably regulate waste water ph to 0.6 ~ 1 during pre-neutralization.
2. in step (2) and (5): described water soluble alkali solution can be conventional water soluble alkali solution, preferred lime slurry, sodium hydroxide, potassium hydroxide, sodium carbonate or solution of potassium carbonate.
3. in step (3) extraction: fully mix under waste water normal temperature and pressure by profit phase volume ratio 1:1 with extraction agent.
4. during step (4) is stripped: reextraction caustic dosage is preferably to control to be as the criterion 8.5 by pH end point values.
5., during step (5) regulates: after after extracting, water sends into biochemical system equalizing tank, neutralize with water soluble alkali solution and preferred control pH to 7.0.
6. nitrogenous fertilizer described in is preferably from urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is preferably from potassium primary phosphate, dipotassium hydrogen phosphate or ammonium hydrogen phosphate.
Extracting process in the present invention has the following advantages: 1. extraction efficiency is high, has highly selective, high to difficult degradation macromole partition ratio, only needs one-level to extract namely reach effect to the process of UV light absorber waste water; 2. secondary pollution is little, and extraction agent does not pollute strip liquor; 3. extraction agent is easy to regeneration, and back extraction ratio is high, and strip and do not have emulsion, reextraction process interface is clear, solvent-freely carries phenomenon secretly; 4. extraction and reextraction operate and are easy to carry out, and operate all at normal temperatures, cost is low.
In extracting operation step of the present invention, UV light absorber waste water is after extracting and demixing, upper strata is extraction phase (loaded extractant), lower floor is extracting phase (after extraction water), the extraction phase (loaded extractant) on upper strata, through reextraction operation regeneration, send equalizing tank to carry out homogeneous, all measure after extracting phase (after the extraction water) neutralization of lower floor.
Reextraction operation steps described in the present invention utilizes alkali lye to strip to extraction phase (loaded extractant), reclaims after organism can be withdrawn deposit and sell after strip liquor acid out.Described reextraction operation steps, extraction phase (loaded extractant) is after reextraction layering, and upper strata is the extraction agent through regeneration, returns extracting system recycle.
Two-stage A/O Biochemical manipulation step of the present invention, anoxic (A) biochemistry is material that is high for organic concentration in waste water, hydrocarbon chain length, to reduce the molecular weight of organic substance, improves the efficiency of follow-up aerobic treatment.Aerobic (O) Biochemical manipulation step utilizes microorganism to carry out aerobic biochemical to the mixed solution after anoxic biochemical treatment, reduces the COD in waste water further.
Extract the 2,4 dihydroxyl benzophenone obtained in the inventive method to return UV light absorber production system and recycle, extraction obtain 2-hydroxyl-4-n-octyloxy-benzophenone withdraw deposit after as production marketing.
The method of the invention can adopt the mode process of periodical operation or operate continuously.Treating wastewater from ultraviolet absorber production of the prior art, pH value about 0 ~ 0.5, COD is about 20000mg/l, and 2,4 dihydroxyl benzophenone, 2-hydroxyl-4-n-octyloxy-benzophenone concentration are respectively 800 ~ 1000mg/l, 400 ~ 500mg/l.After the inventive method process, after extraction, water pH value about 5, COD is about 1000mg/l, and 2,4 dihydroxyl benzophenone, 2-hydroxyl-4-n-octyloxy-benzophenone concentration are respectively 20mg/l, 25mg/l; After neutralization precipitation, water outlet COD is about 8000 mg/l, salinity about 1% after biochemical equalizing tank regulates, COD about 5000 mg/l, microorganism can adapt to through suitably taming, except 2 in waste water, outside 4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, still there are solvent methanol, trichlorotoluene zotrichloride etc., all can pass through microbiological deterioration.After biochemical treatment, water outlet COD is lower than 500mg/l, can enter chemical industrial park sewage works.
Compared with prior art, the inventive method is a kind of method adopting materialization-biochemistry to combine, physico-chemical process is first utilized to reclaim 2 in waste water, 4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone material, reduce in waste water and be difficult to biological degradation organic concentration, utilize the microorganism through domestication, cultivation to carry out biochemical treatment to waste water more further, thus make waste water reach garden adapter standard.The method is reasonable in design, workable.
Accompanying drawing explanation
Fig. 1 is a kind of process flow sheet of the present invention.
Embodiment
Referring to accompanying drawing, further describe concrete technical scheme of the present invention, so that those skilled in the art understands the present invention further, and do not form the restriction to its right.
Embodiment 1, with reference to Fig. 1, a kind for the treatment of process of ultraviolet absorbent UV-531 factory effluent, its step is as follows:
(1) oil removal precipitation: first carry out oil removal precipitation process to ultraviolet absorbent UV-531 factory effluent, removes contained oil slick and suspended substance in waste water;
(2) pre-neutralization: regulate waste water ph to 0.6 with water soluble alkali solution, pre-neutralization is carried out to the waste water through oil removal process;
(3) extract: fully mix under waste water normal temperature and pressure by profit phase volume ratio 4:1 with extraction agent, after layering, namely extracting phase extracts rear water and enters step (5) adjustment, and extraction phase and loaded extractant send step (4) reextraction regeneration; Extraction progression one-level, described extraction agent is for being selected from phosphoric acid ester, alkyl amine, sec-octyl alcohol, kerosene or diesel oil;
(4) strip: fully mix with alkali lye under getting above-mentioned extraction phase normal temperature and pressure, caustic dosage is to control to be as the criterion 8 by pH end point values, after layering, strip liquor acid out reclaims product 2,4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, extraction agent after regeneration recycles in extraction workshop section, reextraction progression one-level; Described alkali lye is NaOH or 5% ~ 30%KOH solution of mass concentration 5% ~ 30%;
(5) regulate: after extraction, water sends into biochemical system equalizing tank, carries out homogeneous, all measures adjustment, neutralize and control pH to 6.5 with water soluble alkali solution, and according to mass ratio BOD
5: N:P=100:5:1 proportioning adds nutritive element; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(6) one-level A/O: equalizing tank waste water is entered biochemical system one-level A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5, temperature 20 DEG C, 3 hours residence time, O pond controls dissolved oxygen Do at 1mg/L, pH value 6.5, temperature 20 DEG C, 15 hours residence time, the mixed solution after one-level A/O process is through sedimentation layering, and settled sludge partial reflux enters anoxic reacter, part, through concentration and settlement, is arranged outside after press filtration;
(7) secondary A/O: one-level A/O water outlet enters secondary A/O reactor, and A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5, temperature 20 DEG C, 3 hours residence time, O pond controls dissolved oxygen Do at 2mg/L, pH value 6.5, temperature 20 DEG C, 5 hours residence time, mixed solution after secondary A/O process is through sedimentation layering, settled sludge partial reflux enters anoxic reacter, and part, through concentration and settlement, is arranged outside after press filtration, after supernatant liquor adds the process of coagulating agent reaction precipitation, Chinese effluent.
Embodiment 2, with reference to Fig. 1, a kind for the treatment of process of ultraviolet absorbent UV-531 factory effluent, its step is as follows:
(1) oil removal precipitation: first carry out oil removal precipitation process to ultraviolet absorbent UV-531 factory effluent, removes contained oil slick and suspended substance in waste water;
(2) pre-neutralization: regulate waste water ph to 4 with water soluble alkali solution, pre-neutralization is carried out to the waste water through oil removal process;
(3) extract: fully mix under waste water normal temperature and pressure by profit phase volume ratio 1:8 with extraction agent, after layering, namely extracting phase extracts rear water and enters step (5) adjustment, and extraction phase and loaded extractant send step (4) reextraction regeneration; Extraction progression one-level, described extraction agent is for being selected from phosphoric acid ester, alkyl amine, sec-octyl alcohol, kerosene or diesel oil;
(4) strip: fully mix with alkali lye under getting above-mentioned extraction phase normal temperature and pressure, caustic dosage is to control to be as the criterion 11 by pH end point values, after layering, strip liquor acid out reclaims product 2,4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, extraction agent after regeneration recycles in extraction workshop section, reextraction progression one-level; Described alkali lye is NaOH or 5% ~ 30%KOH solution of mass concentration 5% ~ 30%;
(5) regulate: after extraction, water sends into biochemical system equalizing tank, carries out homogeneous, all measures adjustment, neutralize and control pH to 8.5 with water soluble alkali solution, and according to mass ratio BOD
5: N:P=100:5:1 proportioning adds nutritive element; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(6) one-level A/O: equalizing tank waste water is entered biochemical system one-level A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 8.5, temperature 35 DEG C, 4 hours residence time, O pond controls dissolved oxygen Do at 1.5mg/L, pH value 8.5, temperature 35 DEG C, 20 hours residence time, the mixed solution after one-level A/O process is through sedimentation layering, and settled sludge partial reflux enters anoxic reacter, part, through concentration and settlement, is arranged outside after press filtration;
(7) secondary A/O: one-level A/O water outlet enters secondary A/O reactor, and A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 8.5, temperature 35 DEG C, 4 hours residence time, O pond controls dissolved oxygen Do at 4mg/L, pH value 8.5, temperature 35 DEG C, 8 hours residence time, mixed solution after secondary A/O process is through sedimentation layering, settled sludge partial reflux enters anoxic reacter, and part, through concentration and settlement, is arranged outside after press filtration, after supernatant liquor adds the process of coagulating agent reaction precipitation, Chinese effluent.
Embodiment 3, with reference to Fig. 1, a kind for the treatment of process of ultraviolet absorbent UV-531 factory effluent, its step is as follows:
(1) oil removal precipitation: first carry out oil removal precipitation process to ultraviolet absorbent UV-531 factory effluent, removes contained oil slick and suspended substance in waste water;
(2) pre-neutralization: regulate waste water ph to 1 with water soluble alkali solution, pre-neutralization is carried out to the waste water through oil removal process;
(3) extract: fully mix under waste water normal temperature and pressure by profit phase volume ratio 1:1 with extraction agent, after layering, namely extracting phase extracts rear water and enters step (5) adjustment, and extraction phase and loaded extractant send step (4) reextraction regeneration; Extraction progression one-level, described extraction agent is for being selected from phosphoric acid ester, alkyl amine, sec-octyl alcohol, kerosene or diesel oil;
(4) strip: fully mix with alkali lye under getting above-mentioned extraction phase normal temperature and pressure, caustic dosage is to control to be as the criterion 8.5 by pH end point values, after layering, strip liquor acid out reclaims product 2,4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, extraction agent after regeneration recycles in extraction workshop section, reextraction progression one-level; Described alkali lye is NaOH or 5% ~ 30%KOH solution of mass concentration 5% ~ 30%;
(5) regulate: after extraction, water sends into biochemical system equalizing tank, carries out homogeneous, all measures adjustment, neutralize and control pH to 7 with water soluble alkali solution, and according to mass ratio BOD
5: N:P=100:5:1 proportioning adds nutritive element; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(6) one-level A/O: equalizing tank waste water is entered biochemical system one-level A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 7, temperature 25 DEG C, 3.5 hours residence time, O pond controls dissolved oxygen Do at 1.2mg/L, pH value 7.0, temperature 25 DEG C, 18 hours residence time, the mixed solution after one-level A/O process is through sedimentation layering, and settled sludge partial reflux enters anoxic reacter, part, through concentration and settlement, is arranged outside after press filtration;
(7) secondary A/O: one-level A/O water outlet enters secondary A/O reactor, and A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 7.0, temperature 25 DEG C, 3.5 hours residence time, O pond controls dissolved oxygen Do at 3mg/L, pH value 7.0, temperature 25 DEG C, 7 hours residence time, mixed solution after secondary A/O process is through sedimentation layering, settled sludge partial reflux enters anoxic reacter, and part, through concentration and settlement, is arranged outside after press filtration, after supernatant liquor adds the process of coagulating agent reaction precipitation, Chinese effluent.
Embodiment 4, in the step (2) of embodiment 1 or the treatment process described in 2 or 3 and (5): described water soluble alkali solution is selected from lime slurry, sodium hydroxide, potassium hydroxide, sodium carbonate or solution of potassium carbonate.
Embodiment 5, in step (5) adjustment of embodiment 1 or 2 or the treatment process described in 3 or 4: described nitrogenous fertilizer is selected from urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is selected from potassium primary phosphate, dipotassium hydrogen phosphate or ammonium hydrogen phosphate.
Claims (7)
1. a treatment process for ultraviolet absorbent UV-531 factory effluent, is characterized in that, its step is as follows:
(1) oil removal precipitation: first carry out oil removal precipitation process to ultraviolet absorbent UV-531 factory effluent, removes contained oil slick and suspended substance in waste water;
(2) pre-neutralization: regulate waste water ph to 0.6 ~ 4 with water soluble alkali solution, pre-neutralization is carried out to the waste water through oil removal process;
(3) extract: fully mix under waste water normal temperature and pressure by profit phase volume ratio 4:1 ~ 1:8 with extraction agent, after layering, namely extracting phase extracts rear water and enters step (5) adjustment, and extraction phase and loaded extractant send step (4) reextraction regeneration; Extraction progression one-level, described extraction agent is for being selected from phosphoric acid ester, alkyl amine, sec-octyl alcohol, kerosene or diesel oil;
(4) strip: fully mix with alkali lye under getting above-mentioned extraction phase normal temperature and pressure, caustic dosage is to control to be as the criterion 8 ~ 11 by pH end point values, after layering, strip liquor acid out reclaims product 2,4-dihydroxy benaophenonel, 2-hydroxyl-4-n-octyloxy-benzophenone, extraction agent after regeneration recycles in extraction workshop section, reextraction progression one-level; Described alkali lye is NaOH or 5% ~ 30%KOH solution of mass concentration 5% ~ 30%;
(5) regulate: after extraction, water sends into biochemical system equalizing tank, carries out homogeneous, all measures adjustment, neutralize and control pH to 6.5 ~ 8.5 with water soluble alkali solution, and according to mass ratio BOD
5: N:P=100:5:1 proportioning adds nutritive element; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(6) one-level A/O: equalizing tank waste water is entered biochemical system one-level A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 3 ~ 4 hours residence time,
O pond controls dissolved oxygen Do at 1 ~ 1.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 15 ~ 20 hours residence time, the mixed solution after one-level A/O process is through sedimentation layering, and settled sludge partial reflux enters anoxic reacter, part, through concentration and settlement, is arranged outside after press filtration;
(7) secondary A/O: one-level A/O water outlet enters secondary A/O reactor, A pond controls dissolved oxygen Do ﹤ 0.5mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 3 ~ 4 hours residence time, O pond controls dissolved oxygen Do at 2 ~ 4mg/L, pH value 6.5 ~ 8.5, temperature 20 ~ 35 DEG C, 5 ~ 8 hours residence time, mixed solution after secondary A/O process is through sedimentation layering, settled sludge partial reflux enters anoxic reacter, and part, through concentration and settlement, is arranged outside after press filtration, after supernatant liquor adds the process of coagulating agent reaction precipitation, Chinese effluent.
2. treatment process according to claim 1, is characterized in that: in step (2): regulate waste water ph to 0.6 ~ 1 during pre-neutralization.
3. treatment process according to claim 1, is characterized in that: in step (2) and (5): described water soluble alkali solution is selected from lime slurry, sodium hydroxide, potassium hydroxide, sodium carbonate or solution of potassium carbonate.
4. treatment process according to claim 1, is characterized in that: in step (3) extraction: fully mix under waste water normal temperature and pressure by profit phase volume ratio 1:1 with extraction agent.
5. treatment process according to claim 1, is characterized in that: during step (4) is stripped: reextraction caustic dosage is to control to be as the criterion 8.5 by pH end point values.
6. treatment process according to claim 1, is characterized in that: during step (5) regulates: after after extraction, water sends into biochemical system equalizing tank, neutralize and control pH to 7.0 with water soluble alkali solution.
7. treatment process according to claim 1 or 5, is characterized in that: during step (5) regulates: described nitrogenous fertilizer is selected from urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is selected from potassium primary phosphate, dipotassium hydrogen phosphate or ammonium hydrogen phosphate.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105254135A (en) * | 2015-11-17 | 2016-01-20 | 中蓝连海设计研究院 | Coal-to-liquid production wastewater treatment method |
| CN109607915A (en) * | 2018-12-12 | 2019-04-12 | 江苏湖大化工科技有限公司 | A kind of processing method of Benzotriazole Ultraviolet Stabilizer production waste water |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503034A (en) * | 2011-11-08 | 2012-06-20 | 中蓝连海设计研究院 | Treatment method of phenol-containing liquid waste in sebacic acid production |
| CN102515391A (en) * | 2011-12-15 | 2012-06-27 | 中蓝连海设计研究院 | Method for pre-treating wastewater from ultraviolet absorber production |
-
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503034A (en) * | 2011-11-08 | 2012-06-20 | 中蓝连海设计研究院 | Treatment method of phenol-containing liquid waste in sebacic acid production |
| CN102515391A (en) * | 2011-12-15 | 2012-06-27 | 中蓝连海设计研究院 | Method for pre-treating wastewater from ultraviolet absorber production |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105254135A (en) * | 2015-11-17 | 2016-01-20 | 中蓝连海设计研究院 | Coal-to-liquid production wastewater treatment method |
| CN105254135B (en) * | 2015-11-17 | 2017-12-12 | 中蓝连海设计研究院 | Coal liquifaction production wastewater treatment method |
| CN109607915A (en) * | 2018-12-12 | 2019-04-12 | 江苏湖大化工科技有限公司 | A kind of processing method of Benzotriazole Ultraviolet Stabilizer production waste water |
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Application publication date: 20150729 |