CN103588329B - Condensation mother liquid waste water pretreatment and resource system and method in compound neutralization reactor in disperse blue 56 production process - Google Patents
Condensation mother liquid waste water pretreatment and resource system and method in compound neutralization reactor in disperse blue 56 production process Download PDFInfo
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Abstract
The invention discloses condensation mother liquid waste water pretreatment and a resource system and a method in a compound neutralization reactor in a disperse blue 56 production process, which belongs to the waste water treatment field. The method comprises the following steps: highly basic condensation mother liquid waste water in the disperse blue 56 production process and a mixed acid solution (sulfuric acid and sulfamic acid) in the compound neutralization reactor are neutralized, three purposes of reducing the pH value of waste water, precipitating phenol and removing nitrite can be simultaneously realized; the neutralized waste water passes through a fixed bed adsorption column filled with adsorption resin, so that residual phenol in the waste water can absorb on the resin column. Resin after adsorption saturation is carried out with desorption and regeneration by using a NaOH solution and then the resin is repeatedly usable, and the desorption liquid passes through the processes of acidity adjusting and vacuum distillation of phenol to realize recycling of phenol. According to the condensation mother liquid waste water which is pretreated in the disperse blue 56 production process, CODCr value is decreased from about 55000mg/L to less than 500mg/L, the phenols substance concentration is decreased from about 19000mg/L to less than 20mg/L, the nitrite ion is decreased from 87000mg/L to less than 20mg/L; thereby the treatment and resource utilization of waste water can be effectively realized.
Description
Technical field
The present invention relates to Wastewater Pretreatment and resource utilization in a kind of disperse blue 56 production process, the condensed mother liquor Wastewater Pretreatment particularly in a kind of compound neutralization reactor and disperse blue 56 production process and recycling system and method.
Background technology
Disperse blue 56 (Disperse Blue 56, No. CAS: 12217-79-7 is also called for short 56# blue) is a kind of important dyestuff, and it can give off a large amount of high dense strong basicity waste water containing phenol and Sodium Nitrite in process of production, waste water COD
crbe about 55000mg/L, phenol content about 1.9% (massfraction), nitrite ion content about 8.7% (massfraction), pH>14, therefore this wastewater toxicity is large, biodegradability is poor, be difficult to subsequent disposal, can do great damage to environment if do not carry out effective improvement.Three technical barriers that exist in governance process of this waste water need to solve:
Difficult point 1, waste water strong basicity: be strong basicity in the condensed mother liquor waste water in disperse blue 56 production process, and contain the nitrite ion of 8.7%, if acid is added dropwise to waste water neutralize alkalescence by ordinary method, the nitrogen protoxide and the nitrogen dioxide gas that have a large amount of strong and stimulating are overflowed, not only polluted air, more serious harm operator are healthy;
Difficult point 2, waste water are containing high concentration phenol sodium: the condensed mother liquor waste water in disperse blue 56 production process is strong basicity, and phenol in wastewater exists with sodium phenylate form, and conventional resins absorption method is difficult to sodium phenylate in Adsorption alkaline aqueous solution;
Difficult point 3, waste water are containing a large amount of nitrite ion: bio-toxicity is large, and easily becomes the important source of the body eutrophication factor " nitrogen ".
Therefore need the phenol in the alkalescence of neutralized wastewater, recovery waste water in the strong basicity condensed mother liquor waste water treatment process in disperse blue 56 production process, and remove the nitrite ion in waste water.Complete above-mentioned target and effectively can reduce wastewater toxicity, be convenient to the successive depths process of waste water, bring obvious economic benefit to producer simultaneously.
Summary of the invention
1. the technical problem that will solve
In governance process, there are three technical barriers for the waste water produced in disperse blue 56 production process, the object of this invention is to provide condensed mother liquor Wastewater Pretreatment in a kind of compound neutralization reactor and disperse blue 56 production process and recycling system and method, namely neutralized wastewater alkalescence, remove waste water Nitrite ion and reclaim phenol in wastewater class material.
2. technical scheme
A kind of compound neutralization reactor, it is by outside water-in, vapor pipe is (for guiding the nitrogen protoxide generated in reaction process, nitrogen peroxide secondary contacts with alkaline waste water and is absorbed, also discharge nitrogen) simultaneously, inner inlet mouth, mixed acid solution injection port, throw out relief outlet (for discharging the phenol precipitation thing that neutralization precipitation produces), acid solution refluxing opening, stirring rake, condensate return pipe (collects neutralization reaction, the heat that redox reaction process produces, intensification for resin desorption process), sloping plate deposition district (for phenol precipitation solid-liquid separation), gas collection Reflecting pyramid is (for collecting the nitrogen generated in reaction process, nitrogen protoxide, nitrogen peroxide), external outlet, pH meter probe composition.Compound neutralization reactor inside dividing plate is divided into reaction Ι district and reaction two reaction zones territory, П district, and outside water-in and external outlet lay respectively at the upper end of reacting Ι district He reacting П district; Inner inlet mouth is positioned at the bottom of reactor Ι district and П district intersection; Mixed acid solution injection port, throw out relief outlet, acid solution refluxing opening are positioned at the bottom in reactor reaction П district; Stirring rake and condensate return pipe are positioned at the middle and lower part in reaction П district; Sloping plate deposition district is positioned at the top of condensate return pipe; Top, sloping plate deposition district is gas collection Reflecting pyramid; Vapor pipe opening part is the gas collection Reflecting pyramid position of the space bar in reaction Ι district and reaction П district, and exhaust outlet is positioned at the bottom in reaction Ι district; Gas collection Reflecting pyramid top is pH meter probe.
Compared with traditional neutralization reactor, compound neutralization reactor has following innovative point:
(1) there is oxidation restoring function, in reactor, not only carry out acid-base neutralisation reaction, also carry out redox reaction, remove nitrite ion;
(2) there is absorption sour gas function, in acid-base neutralisation reaction process, not only utilize the mixed acid solution neutralized wastewater alkalescence added, the sour gas of waste water self alkaline absorbent, neutralization generation can also be utilized, avoid the release of toxic gas;
(3) there is solid-liquid separation function, the phenol precipitation that neutralization is formed can be separated from waste water.
The pre-treatment of the condensed mother liquor waste water in a kind of disperse blue 56 production process and recycling system, it is by sodium hydroxide solution storage tank, thionamic acid storage tank, vitriol oil storage tank, compound neutralization reactor (neutralized wastewater alkalescence, precipitate a part of phenol, remove nitrite ion), resin absorbing column (reclaiming phenol remaining in compound neutralization reactor processed waste water for adsorbing), acid-base neutralisation solid-liquid separator composition (for precipitating the phenol reclaimed in desorption liquid and throw out); Structural relation between each composition is that compound neutralization reactor water outlet is connected with the water-in of resin absorbing column, its mixed acid solution injection port is connected with vitriol oil storage tank, thionamic acid storage tank respectively, and its throw out relief outlet, acid solution refluxing opening are connected with acid-base neutralisation solid-liquid separator respectively; Resin absorbing column desorption liquid injection port is connected with sodium hydroxide solution storage tank, and the desorption liquid outlet of resin absorbing column is connected with acid-base neutralisation solid-liquid separator.
This system advantage:
(1) with strong basicity waste water in utilizing the vitriol oil in mixed acid solution in compound neutralization reactor, directly phenol precipitation can be reclaimed, and NO and the NO generated
2gas is absorbed by alkaline waste water, avoids being emitted in air working the mischief; Utilize the thionamic acid in mixed acid solution to become nitrogen to discharge waste water Nitrite ion reduction, remove nitrite ion, be convenient to water outlet and carry out subsequent disposal, and the sulfuric acid generated in reaction process can continue neutralized wastewater alkalescence, save the consumption of acid;
(2) heat produced in acid-base neutralisation process is absorbed by the circulating condensing water in inside reactor prolong, is used for heating the resin column of follow-up phase to improve the desorption rate of resin, achieves recovery and the utilization of heat;
(3) adopt resin adsorption method absorption Phenol for Waste Water class material, can effectively reduce waste water COD and phenol content, adsorb saturated after resin adopt thermokalite desorption and regeneration, realize resin and reuse, after desorption liquid acid adjustment, recyclable phenol, realizes resource target.
The pre-treatment of the condensed mother liquor waste water in disperse blue 56 production process and a method of resource, its step comprises:
In step 1. and reduction: by the condensed mother liquor waste water in disperse blue 56 production process in compound neutralization reactor Ι district, with the mixed acid solution adjust pH of sulfuric acid and thionamic acid to 4-6, NO and the NO of N-process generation
2gas is most of by alkaline waste water own absorption (reaction formula 1-3) in floating-upward process, and thionamic acid and nitrite ion react and generate nitrogen (reaction formula 4), nitrogen enters gas collection district through Reflecting pyramid effect, is discharged by reactor П district by vapor pipe;
Concrete reaction equation is as follows:
2H
++NO
2 -+OH
-→HNO
2+H
2O (1)
2HNO
2→NO↑+NO
2↑+H
2O (2)
NO
2+NO+H
2O+2OH
-→2NO
2 -+2H
2O (3)
NH
2-SO
3H+NO
2 -→N
2↑+H
3O
++SO
4 2-(4)
Remaining a small amount of NO and NO
2gas enters gas collection district through Reflecting pyramid effect, after enter compound neutralization reactor I district by escape pipe, again completely by alkaline waste water and absorb (reaction formula 3).The circulating condensing water that in reaction process, liberated heat is condensed in water return line absorbs, and the insulation jacket being entered resin column by the water of condensation heated ensures desorption temperature.After waste water acid adjustment, part phenol forms Precipitation, deposits to reactor bottom, be transported in acidifying solid-liquid separator through peristaltic pump through swash plate effect and waterpower backflow effect.
Step 2. is adsorbed: the waste water after acid adjustment is with certain flow rate by being filled with the resin absorbing column adsorption column of polymeric adsorbent, and the phenol in waste water is attracted on resin;
Step 3. resin desorption: step 2 adsorb saturated after resin NaOH (mass concentration 4-8%) solution desorption and regeneration, desorption temperature 40-60 DEG C;
Step 4. reclaims phenol: desorption liquid enters in acidifying solid-liquid separator, pH≤6 are adjusted to separate out precipitation with sulfuric acid, separate in the lump together with the precipitation in neutralization reactor compound in step 1, drying under reduced pressure distillation obtains crude product phenol (pressure :-0.1 ~-0.075MPa, temperature: 60-80 DEG C), acid solution is then back to compound neutralization reactor.
3, beneficial effect:
(1) utilize compound neutralization reactor, add in nitration mixture and strong basicity condensed mother liquor waste water in disperse blue 56 production process, not only directly resource utilization can reclaim a large amount of phenol precipitation of separating out, its NO and NO produced
2gas by alkaline waste water absorption reaction in uphill process, both can avoid NO and NO
2gas is emitted in air and works the mischief, and utilizes again acid NO
2gas neutralized wastewater alkalescence, saves the consumption of acid;
(2) waste water Nitrite ion reduction becomes nitrogen to discharge by the thionamic acid in added nitration mixture, not only effectively remove nitrite ion, be convenient to water outlet and carry out subsequent disposal, and the sulfuric acid generated in reaction process can continue neutralized wastewater alkalescence, save the consumption of acid;
(3) heat produced in acid-base neutralisation process is absorbed by the circulating condensing water in inside reactor prolong, is used for heating the resin column of follow-up phase to improve the desorption rate of resin, achieves recovery and the utilization of heat, effectively saves the energy;
(4) adopt resin adsorption method absorption Phenol for Waste Water class material, can effectively reduce waste water COD and phenol content, adsorb saturated after resin adopt thermokalite desorption and regeneration, realize resin and reuse, after desorption liquid acid adjustment, recyclable phenol, realizes resource target.
Accompanying drawing explanation
Condensed mother liquor Wastewater Pretreatment in a kind of disperse blue 56 production process of Fig. 1 and recycling system structure iron, 1, sodium hydroxide solution storage tank, 2, thionamic acid storage tank, 3, vitriol oil storage tank, 4, compound neutralization reactor, 5, resin absorbing column, 6, acid-base neutralisation solid-liquid separator;
Fig. 2 resin absorbing column structural representation, 7, water-in, 7 ', desorption liquid injection port, 8, water outlet, 8 ', desorption liquid outlet, 16 ', water of condensation Link Port;
The compound neutralization reactor structural representation of Fig. 3,9, outside water-in, 10, vapor pipe, 11, inner inlet mouth, 12, mixed acid solution injection port, 13, throw out relief outlet, 14, acid solution refluxing opening, 15, stirring rake, 16, condensate return pipe, 17, sloping plate deposition district, 18, gas collection Reflecting pyramid, 19, external outlet, 20, pH meter probe;
Condensed mother liquor Wastewater Pretreatment in a kind of disperse blue 56 production process of Fig. 4 and method of resource schema.
Embodiment
Further illustrate the present invention by the following examples.
Embodiment 1:
Strong basicity condensed mother liquor waste water COD in disperse blue 56 production process
crfor 54400mg/L, pH are greater than 14, aldehydes matter concentration is 18900mg/L.
Wastewater treatment pilot test system as shown in Figure 1, comprise: sodium hydroxide solution storage tank 1, thionamic acid storage tank 2, vitriol oil storage tank 3, compound neutralization reactor 4, resin absorbing column 5, acid-base neutralisation solid-liquid separator 6, compound neutralization reactor water outlet is connected with a water-in of resin absorbing column, its mixed acid solution injection port is connected with vitriol oil storage tank, thionamic acid storage tank respectively, and its throw out relief outlet, acid solution refluxing opening are connected with acid-base neutralisation solid-liquid separator respectively; Resin absorbing column two water-ins are connected with sodium hydroxide solution storage tank, compound neutralization reactor water outlet respectively, and one of them water outlet is connected with acid-base neutralisation solid-liquid separator.Resin absorbing column and compound neutralization reactor structure are as shown in accompanying drawing 2 and accompanying drawing 3, a kind of compound neutralization reactor, it is by outside water-in 9, vapor pipe 10, inner inlet mouth 11, mixed acid solution injection port 12, throw out relief outlet 13, acid solution refluxing opening 14, stirring rake 15, condensate return pipe 16, sloping plate deposition district 17, gas collection Reflecting pyramid 18, external outlet 19, pH meter probe 20 composition, structural relation between each composition is that inside reactor dividing plate is divided into two reaction zones territory, outside water-in and water outlet lay respectively at reactor reaction Ι district and react the top in П district, inner inlet mouth is positioned at the bottom of reactor reaction Ι district and П district intersection, mixed acid solution injection port, throw out relief outlet, acid solution refluxing opening are positioned at bottom reactor reaction П district, stirring rake and condensate return pipe are positioned at the middle and lower part in reactor reaction П district, sloping plate deposition district is positioned at the top of prolong, top, sloping plate deposition district is gas collection Reflecting pyramid, vapor pipe opening part is the gas collection Reflecting pyramid position that reaction Ι district and П separate plate, and exhaust outlet is reaction bottom, Ι district, gas collection Reflecting pyramid top is pH meter probe.Resin absorbing column structural representation, as Fig. 2, comprises water-in 7, desorption liquid injection port 7 ', water outlet 8, desorption liquid outlet 8 ', water of condensation Link Port 16 '.
The pre-treatment of the condensed mother liquor waste water in disperse blue 56 production process and resource utilization process as shown in Figure 4, the steps include:
1.1 by the strong basicity condensed mother liquor waste water in disperse blue 56 production process with flow velocity v
1=10L/min passes into compound neutralization reactor Ι district, sulfuric acid (mass concentration 95%, flow 0.2L/min) and sulfamic acid solution (mass concentration 14.5%, flow 6.8L/min) mixed acid solution enter compound neutralization reactor by acid inlet tube, mechanical stirrer stir speed (S.S.) (120r/min), reaction is adjusted to water outlet (pH=4);
1.2 water outlets are with v
2the flow velocity of=10L/min enters and is filled with in 220L polystyrene-divinylbenzene hypercrosslinked polymeric resin adsorption column, and the COD of the absorption water outlet of front 2200L is down to 424mg/L, and aldehydes matter concentration is down to 13.6mg/L.
1.3 carry out desorption with the flow velocity of 2L/min to resin with 80L NaOH (mass concentration 8%) solution, desorption temperature 40 DEG C.
1.4 desorption liquids enter in acidifying solid-liquid separator, pH=6 is adjusted to separate out precipitation with sulfuric acid (95% mass concentration), separate in the lump together with the precipitation in neutralization reactor compound in step 1.1, underpressure distillation (pressure :-0.075MPa, temperature: 60 DEG C), be cooled to 25 DEG C of crystallisation by cooling.
After aforesaid method process, its Wastewater Pretreatment effect, as following table:
Embodiment 2:
Waste water quality is with embodiment 1, and Waste Water Treatment is similar to embodiment 1, and operation steps is as follows:
2.1 by the strong basicity condensed mother liquor waste water in disperse blue 56 production process with flow velocity v
1=20L/min passes into compound neutralization reactor Ι district, sulfuric acid (mass concentration 95%, flow 0.4L/min) and sulfamic acid solution (mass concentration 14.5%, flow 14L/min) mixed acid solution enter compound neutralization reactor by acid inlet tube, mechanical stirrer stir speed (S.S.) (120r/min), reaction is adjusted to water outlet (pH=5);
2.2 water outlets are with v
2the flow velocity of=20L/min enters and is filled with in 220L polystyrene-divinylbenzene hypercrosslinked polymeric resin adsorption column, and the COD of the absorption water outlet of front 1800L is down to 476mg/L, and aldehydes matter concentration is down to 18.5mg/L.
2.3 carry out desorption with the flow velocity of 2L/min to resin with 80L NaOH (mass concentration 6%) solution, desorption temperature 50 DEG C.
2.4 desorption liquids enter in acidifying solid-liquid separator, pH=5 is adjusted to separate out precipitation with sulfuric acid (95% mass concentration), separate in the lump together with the precipitation in neutralization reactor compound in step 1, underpressure distillation (pressure :-0.09MPa, temperature: 70 DEG C), be cooled to 25 DEG C of crystallisation by cooling.
Wastewater Pretreatment effect is as follows:
Embodiment 3:
Waste water quality is with embodiment 1, and treatment system is similar with embodiment 1 to operation steps, but the resin of filling in process resin post changes macroporous polystyrene-divinylbenzene resins into.
3.1 by the strong basicity condensed mother liquor waste water in disperse blue 56 production process with flow velocity v
1=20L/min passes into compound neutralization reactor Ι district, sulfuric acid (mass concentration 95%, flow 0.4L/min) and sulfamic acid solution (mass concentration 14.5%, flow 14L/min) mixed acid solution enter compound neutralization reactor by acid inlet tube, mechanical stirrer stir speed (S.S.) (120r/min), reaction is adjusted to water outlet (pH=6);
3.2 water outlets are with v
2the flow velocity of=20L/min enters and is filled with in 220L polystyrene-divinylbenzene hypercrosslinked polymeric resin adsorption column, and the COD of the absorption water outlet of front 1800L is down to 476mg/L, and aldehydes matter concentration is down to 18.5mg/L.
3.3 carry out desorption with the flow velocity of 2L/min to resin with 80L NaOH (mass concentration 4%) solution, desorption temperature 60 DEG C.
3.4 desorption liquids enter in acidifying solid-liquid separator, pH=4 is adjusted to separate out precipitation with sulfuric acid (95% mass concentration), separate in the lump together with the precipitation in neutralization reactor compound in step 1, underpressure distillation (pressure :-0.1MPa, temperature: 80 DEG C), be cooled to 25 DEG C of crystallisation by cooling.
Wastewater Pretreatment effect
Embodiment 4:
Waste water quality is with embodiment 1, and treatment system is similar with embodiment 1 to operation steps, but the resin of filling in resin column changes amido modified polystyrene-divinylbenzene hypercrosslinked polymeric resin into, and other operational condition is constant, and its result of implementation is as follows.
Wastewater Pretreatment effect
Embodiment 5:
Step with embodiment 1, but changes the concentration of sodium hydroxide solution in step 1.3 into 4%, and other operational condition is constant, and its result of implementation is as follows.
Wastewater Pretreatment effect
According to above-described embodiment, the present invention has following beneficial effect.
(1) effectively can remove the COD in the strong basicity condensed mother liquor waste water in disperse blue 56 production process, clearance is greater than 99%, water outlet COD<500mg/L;
(2) effectively can remove the nitrite ion in the strong basicity condensed mother liquor waste water in disperse blue 56 production process, clearance is greater than 99%, water outlet nitrite ion concentration <20mg/L;
(3) can effectively in and disperse blue 56 production process in strong basicity condensed mother liquor waste water alkalescence, water outlet pH=5-7;
(4) can aldehydes matter in the strong basicity condensed mother liquor waste water in efficient recovery disperse blue 56 production process, water outlet phenol concentration <20mg/L, the phenol rate of recovery is greater than 70%.
Claims (7)
1. a compound neutralization reactor, it is made up of outside water-in (9), vapor pipe (10), inner inlet mouth (11), mixed acid solution injection port (12), throw out relief outlet (13), acid solution refluxing opening (14), stirring rake (15), condensate return pipe (16), sloping plate deposition district (17), gas collection Reflecting pyramid (18), external outlet (19), pH meter probe (20); Compound neutralization reactor inside dividing plate is divided into reaction Ι district, reaction two reaction zones territory, П district, and outside water-in (9) and external outlet (19) lay respectively at the reaction Ι district of reactor and the top in reaction П district; Inner inlet mouth (11) is positioned at bottom the dividing plate in reactor reaction Ι district and П interval; Mixed acid solution injection port (12), throw out relief outlet (13), acid solution refluxing opening (14) are positioned at the bottom in reaction П district; Stirring rake (15) and condensate return pipe (16) are positioned at the middle and lower part in reaction П district; Sloping plate deposition district is positioned at the top of condensate return pipe; Top, sloping plate deposition district is gas collection Reflecting pyramid; Gas collection Reflecting pyramid top is pH meter probe; Described vapor pipe, its opening part is the gas collection Reflecting pyramid position of two reaction zones dividing plate, exports the bottom into compound neutralization reactor reaction Ι district, inner inlet mouth (11) place.
2. the pre-treatment of the condensed mother liquor waste water in disperse blue 56 production process and a recycling system, it is made up of sodium hydroxide solution storage tank (1), thionamic acid storage tank (2), vitriol oil storage tank (3), compound neutralization reactor according to claim 1 (4), resin absorbing column (5), acid-base neutralisation solid-liquid separator (6); Compound neutralization reactor (4) external outlet is connected with resin absorbing column water-in, its mixed acid solution injection port is connected with vitriol oil storage tank (3), thionamic acid storage tank (2) respectively, compound neutralization reactor (4) throw out relief outlet, acid solution refluxing opening are connected with acid-base neutralisation solid-liquid separator (6) respectively, the desorption liquid injection port of resin absorbing column (5) is connected with sodium hydroxide solution storage tank, and the desorption liquid outlet of resin absorbing column is connected with acid-base neutralisation solid-liquid separator (6).
3. the pre-treatment of the condensed mother liquor waste water in disperse blue 56 production process and a method of resource, its step comprises:
Step 1 neutralized wastewater alkalescence, separate out phenol remove nitrite anions: the condensed mother liquor waste water in disperse blue 56 production process and the mixed acid solution of sulfuric acid and thionamic acid pass into the compound neutralization reactor described in claim 1, neutralization reaction, is adjusted to water outlet pH value 4-6;
Step 2 is adsorbed: the phenol in water, by being filled with the resin absorbing column absorption of polymeric adsorbent, is attracted on resin by the water outlet after step 1 processes;
Step 3 resin desorption: step 2 adsorb saturated after resin sodium hydroxide solution desorption;
Step 4 reclaims phenol: the desorption liquid of step 3 enters in acidifying solid-liquid separator, pH≤6 are adjusted to separate out precipitation with sulfuric acid, separate in the lump together with the precipitation in neutralization reactor compound in step 1, acid solution is then back to compound neutralization reactor, and the precipitation separated obtains crude product phenol through drying under reduced pressure.
4. method according to claim 3, is characterized in that: in the reaction process of described step 1, added thionamic acid is equal with the molar weight of waste water Nitrite ion.
5. method according to claim 3, is characterized in that: the resin in step 2 is skeleton is the polymeric adsorbent of polystyrene-divinylbenzene or amido modified polystyrene-divinylbenzene hypercrosslinked polymeric resin.
6. method according to claim 3, is characterized in that: the desorbing agent in described step 3 is mass concentration 4 ~ 8%NaOH solution, and desorption temperature is 40 ~ 60 DEG C.
7. method according to claim 3, is characterized in that: drying under reduced pressure in described step 4, its pressure :-0.1 ~-0.075MPa, temperature: 60-80 DEG C.
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| CN104556521A (en) * | 2014-12-31 | 2015-04-29 | 绍兴奇彩化工有限公司 | Treatment method for condensed wastewater in disperse blue 56 production process |
| CN104829027A (en) * | 2015-04-10 | 2015-08-12 | 浙江奇彩环境科技有限公司 | Technology for processing disperse blue 56 reduction mother liquor waste water |
| CN105060558B (en) * | 2015-08-04 | 2017-06-27 | 浙江闰土研究院有限公司 | A kind of pretreatment of Disperse Blue-56 condensation waste water and resource utilization method |
| CN105585096A (en) * | 2016-03-04 | 2016-05-18 | 苏州荣能环保科技有限公司 | Waste water treatment device |
| CN108408955A (en) * | 2018-01-22 | 2018-08-17 | 陈贤瑜 | A kind of processing equipment of sulphur cyanogen waste water |
| CN108203150A (en) * | 2018-01-22 | 2018-06-26 | 陈贤瑜 | For the processing system of industrial wastewater |
| CN108314171A (en) * | 2018-01-22 | 2018-07-24 | 陈贤瑜 | A kind of sewage disposal device |
| CN111115744A (en) * | 2020-01-10 | 2020-05-08 | 浙江长征化工有限公司 | Treatment method of disperse red 60 condensed wastewater |
| CN112485099A (en) * | 2020-11-23 | 2021-03-12 | 陕西彩虹新材料有限公司 | Preparation method of COD mixed digesting agent |
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| JP4282962B2 (en) * | 2002-08-01 | 2009-06-24 | 月島環境エンジニアリング株式会社 | Wastewater neutralization method |
| JPWO2004020347A1 (en) * | 2002-08-29 | 2005-12-15 | 住友金属鉱山株式会社 | Treatment method for wastewater containing high concentration nitrate nitrogen |
| CN101591083A (en) * | 2008-05-30 | 2009-12-02 | 河南新天地药业有限公司 | Para hydroxybenzene glycolylurea building-up process treatment of phenolic waste water |
| CN101481170A (en) * | 2009-02-13 | 2009-07-15 | 湖北富农生物科技有限公司 | Use of sulfamic acid for degrading cultivation water nitrite and reducing cultivation water pH value in aquiculture |
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