CN108609804B - BDP wastewater treatment method - Google Patents
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- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
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- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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Abstract
The invention discloses a BDP wastewater treatment method, which comprises the following steps: (1) ozone oxidation: ozone enters from the lower part of an ozone reaction tower in a counter-current mode, BDP wastewater with the COD concentration of 12000-18000 mg/L enters from the upper part of the ozone reaction tower, and is subjected to ozone oxidation in the ozone reaction tower, and the contact reaction time is 60-180 s; (2) biochemical treatment: adjusting the pH value of BDP wastewater after ozone oxidation to 7.0-9.0, performing flocculation and precipitation, and then sequentially entering an ABR anaerobic reaction tank and an aerobic activated sludge tank for advanced treatment; (3) film treatment: after biochemical treatment, the effluent enters sand filtration, and then enters an electrodialysis system for desalination, and the COD concentration of the effluent after desalination is less than 40 mg/L; the salt content is less than 500 mg/L. The COD concentration of the BDP wastewater treated by the method is less than 40 mg/L; the salt content is less than 500 mg/L.
Description
Technical Field
The invention relates to the technical field of organic wastewater treatment, in particular to a BDP wastewater treatment method.
Background
The bisphenol A type phosphate oligomer is BDP for short, and is a novel phosphorus flame retardant. BDP is usually synthesized by a two-step method, firstly, phosphorus oxychloride and bisphenol A are condensed into an intermediate product bisphenol A tetrachlorodiphosphonate under the action of a catalyst magnesium chloride, then the intermediate product bisphenol A tetrachlorodiphosphonate and phenol are subjected to esterification reaction to obtain a crude product of bisphenol A type phosphate oligomer, finally, solvents of toluene and methyl cyclohexane with equal mass are added into the crude product, and the final high-purity product is obtained through multiple acid washing, alkali washing and water washing processes. The waste water with high salt (main salt is NaOH and NaCl) and high toxicity (main components are phenol and bisphenol A) is generated in the production process, and simultaneously contains a large amount of macromolecular substances which are difficult to degrade (mainly polycondensation byproducts such as dimers, trimers, polymers and the like), and the waste water has the characteristics of large water discharge amount, difficult degradation and the like, is difficult to degrade under natural environmental conditions, is easy to enrich in organisms through food chains, and is recognized high-toxicity waste water.
At present, the treatment methods aiming at the wastewater at home and abroad are few, and the treatment mainly adopts the combination of physical chemistry and biochemistry. Physicochemical methods including incineration, wet oxidation, membrane methods, and the like; biochemical methods, mainly including activated sludge method and biofilm method; but the physical and chemical method has the disadvantages of high treatment cost, large investment and short membrane life. The biochemical method is convenient to operate and manage, but because organic matters in the wastewater have high toxicity, are difficult to degrade and have poor biodegradability, the organic matters directly enter a biochemical system to cause great impact on microorganisms, and the growth of the microorganisms is seriously inhibited. Moreover, the biochemical method has good treatment effect on aliphatic hydrocarbon and poor treatment effect on high-toxicity aromatic compounds, and particularly, a large amount of polycyclic substances exist in wastewater.
The wastewater treatment usually adopts physicochemical pretreatment and biochemical treatment, the cost is the lowest, but in the physical pretreatment, microelectrolysis and Fenton require the acid regulation of the wastewater, and a large amount of acid and alkali are consumed for the strong alkali wastewater to generate a large amount of iron mud; advanced oxidation processes, such as catalytic oxidation, electrochemical processes, require catalysts with high costs, high investment and high operating costs, and the latter have high requirements on equipment and complex technology. The ozone oxidation method has strong oxidizability, and particularly has good treatment effect on benzene ring substances. The half-life of ozone is only half an hour, the reaction is thorough, no sludge and secondary pollution exist, the reaction is less influenced by the environment, the wastewater is directly treated without adjusting the pH value, and the ozone is prepared on site, so that the problems of storage and transportation of raw materials do not exist, and the operation and management are convenient.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: aiming at the defects in the prior art, the BDP wastewater treatment method is provided, and the method can thoroughly degrade BDP wastewater with high concentration, high toxicity and high salt, has no secondary pollution and low operation cost, and can make up for the defects in the background art.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a BDP wastewater treatment method comprises the following steps:
(1) ozone oxidation: feeding ozone with the ozone concentration of 150-450 mg/L from the lower part of an ozone reaction tower in a counter-current mode, feeding BDP wastewater with the COD concentration of 12000-18000 mg/L from the upper part of the ozone reaction tower, and carrying out ozone oxidation in the ozone reaction tower for 60-180 s; macromolecular benzene ring substances generate micromolecular benzene ring substances, and the color of the wastewater is changed from colorless to deep red.
(2) Biochemical treatment: adjusting the pH of BDP wastewater after ozone oxidation to 7.0-9.0 by using hydrochloric acid, respectively adding PAC and PAM for flocculation and precipitation, and then sequentially adding water into an ABR anaerobic reaction tank and an aerobic activated sludge tank for advanced treatment; the retention time in the ABR anaerobic reaction tank is 32-42 h; the retention time in the aerobic activated sludge tank is 20-30 h.
(3) Film treatment: after biochemical treatment, the effluent enters sand filtration, and then enters an electrodialysis system for desalination, and the COD concentration of the effluent after desalination is less than 40 mg/L; the salt content is less than 500 mg/L.
As an improved technical scheme, the wastewater treatment method further comprises the following steps: if the COD of the biochemical effluent is higher than 150mg/L, the wastewater after biochemical treatment enters a Fenton pool, ferrous sulfate and hydrogen peroxide are added for Fenton reaction, and neutralization coagulation precipitation is carried out; relative to the amount of raw water, the adding amounts of ferrous sulfate and hydrogen peroxide are 0.25-0.5 g/L and 0.5-1 mL/L respectively; the reaction time is 20-40 min; then enters a sand filtration and electrodialysis system for desalting.
As an improved technical scheme, the ozone comes from an ozone generator, and the air source of the ozone generator is air or oxygen; the ratio of the addition amount of the ozone to the concentration of COD in the BDP wastewater is 1: 35-45.
Preferably, the ozone comes from an ozone generator, and the air source of the ozone generator is air or oxygen; the ratio of the addition amount of the ozone to the concentration of COD in the BDP wastewater is 1: 40.
As an improved technical scheme, the ozone reaction tower is provided with a filler.
As an improved technical scheme, the ABR anaerobic reaction tank comprises 8 ABR anaerobic reaction tanks, the aerobic activated sludge tank comprises 2 aerobic activated sludge tanks, and activated carbon fillers are arranged in the ABR anaerobic reaction tanks; phenol reducing strains are put in the ABR anaerobic reaction tank.
As an improved technical scheme, the phenol-degrading strain is phenol-degrading strain screened after high-efficiency ECM complex bacteria are separated and cultured.
As an improved technical scheme, the screening method of the phenol degrading bacteria comprises the following steps: firstly, carrying out enrichment culture of strains, inoculating the high-efficiency ECM complex bacteria into a culture solution with the phenol concentration of 0.5g/L, and carrying out shake culture at the temperature of 28 ℃ and the rotating speed of 160 r/min; then carrying out microbial acclimation on the wastewater subjected to ozone oxidation at the temperature of 30 ℃ and the rotating speed of 160r/min, separating out a single bacterial colony by using a plate dilution method, and storing; inoculating the separated bacterial colony into the wastewater after ozone oxidation, performing shake culture at 30 ℃ and at the rotating speed of 160r/min, measuring the phenol concentration in the culture, and screening out the bacterial strain with the highest phenol degradation rate.
Preferably, the addition amount of the phenol degrading bacteria is 3-8/120 (volume ratio) relative to the original water amount.
As a further preferable technical scheme, the adding amount of the phenol degrading bacteria is 5/120 (volume ratio) relative to the original water amount.
As a preferred technical scheme, after water is distributed to the wastewater after flocculation and precipitation, the wastewater is heated to 28-30 ℃ and then sequentially enters an ABR anaerobic reaction tank and an aerobic activated sludge tank for advanced treatment.
As an improved technical scheme, the brine obtained after the desalination of the electrodialysis system is evaporated by an evaporator to obtain solid salt.
As a preferred technical solution, the evaporator is a multi-effect evaporator or an MVR evaporator.
Preferably, the sand filtration in the step (3) uses a sand filtration tank, and the sand filtration tank is filled with a mixture of quartz sand, activated carbon and manganese sand and is used for the pretreatment of electrodialysis.
As a preferable technical scheme, biochemical effluent is used for water distribution in the step (3), and the COD concentration in the water after water distribution is 4000-5000 mg/L.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
the BDP wastewater treatment method disclosed by the invention is an organic combination of several treatment steps including ozone oxidation, biochemical treatment and membrane treatment, so that respective advantages are fully exerted, and respective defects are made up. Compared with other pretreatment in the prior art, the BDP does not need to be regulated, sludge is not generated, the investment is not large, the operation cost is low, macromolecular substances in the wastewater can be effectively opened and are micromolecules, the biodegradability of the wastewater is obviously improved, part of phenol is removed, the toxicity of the wastewater is reduced, and most of organic substances in the wastewater are removed after the BDP is subjected to ozone oxidation treatment, so that the follow-up biochemical treatment is utilized. The membrane treatment system removes salt in the wastewater and prepares solid salt as a byproduct, thereby improving the economic benefit. In addition, the invention treats the wastewater under the condition of high salt, reduces the subsequent desalting water quantity and the evaporation water quantity, and saves the cost. The COD concentration of the BDP wastewater treated by the method is less than 40 mg/L; the salt content is less than 500 mg/L.
The phenol degrading bacteria in the biochemical pool in the biochemical treatment step are phenol degrading bacteria screened from high-efficiency ECM composite bacteria after ozone oxidation effluent culture, can accelerate anaerobic starting rate and improve anaerobic removal rate.
Detailed Description
The invention is further illustrated below with reference to specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
Example 1
The basic conditions of the raw water to be treated are as follows: BDP waste water mainly contains phenol, toluene, polycondensation by-products such as dimers, trimers, polymers and the like. The pH value of the waste water is 10.2, the COD value is 12300mg/L, the BOD5/CODcr is 0.22, the salt content is 14000mg/L, and the waste water belongs to high-toxicity high-salt refractory waste water.
At room temperature, BDP wastewater enters from an inlet at the upper part of an ozone reaction tower, ozone with the concentration of 250mg/L generated by an ozone generator enters from an inlet at the lower part, raw water is added from the upper part at the speed of 0.48L/h, the reaction time is 120s, the pH of effluent is 9.2, the COD is 11500mg/L, then the pH is adjusted to 8.2, PAC and PAM are added for coagulation and precipitation, the pH of the effluent is 7.6, the COD is 10900mg/L, and the salt content is 13000 mg/L.
And (3) preparing the effluent after coagulating sedimentation into the influent of a biochemical system by using biochemical effluent, wherein the COD is 4000mg/L and the salt content is 11900 mg/L. The water temperature of the distributed water is heated to 28 ℃, the distributed water sequentially flows through 8 ABR reaction tanks, the retention time in the 8 ABR reaction tanks is totally 36h, the CODcr of the effluent is 780mg/L, and the salt content is 11000 mg/L. The strain type in the ABR reaction tank is phenol degrading bacteria screened after high-efficiency ECM composite bacteria are subjected to ozone oxidation effluent culture, and the addition amount of the phenol degrading bacteria (liquid bacteria) is 5/120 relative to the original water amount. Anaerobic effluent enters 2 parallel aerobic activated sludge tanks for treatment, the temperature is 26 ℃, the retention time is 24 hours, the CODcr of the effluent is 110mg/L, the CODcr is 38mg/L after flocculation and precipitation, and the salinity is 10300 mg/L.
Part of the biochemical effluent is recycled for water distribution for dilution, the rest is subjected to sand filtration and then electrodialysis desalination, the COD of the desalted wastewater is 32mg/L, and the salinity is 341mg/L, and the wastewater is directly discharged; the brine obtained after electrodialysis desalination has salt content of 12.3%, and is subjected to evaporative crystallization.
Example 2
The basic conditions of the raw water to be treated are as follows: BDP waste water mainly contains phenol, toluene, polycondensation by-products such as dimers, trimers, polymers and the like. The pH value of the wastewater is 12, the COD value is 16800mg/L, BOD5/CODcr0.19, and 20800mg/L of salt, belonging to high-toxicity high-salt refractory wastewater.
At room temperature, BDP wastewater enters from an upper inlet of an ozone reaction tower, ozone with the concentration of 320mg/L generated by an ozone generator enters from a lower inlet, raw water is added from the upper part at the speed of 0.54L/min, the reaction time is 170s, the pH of effluent is 11.3, the COD is 15700mg/L, then the pH is adjusted to 8.0, PAC and PAM are added for coagulation and precipitation, the pH of the effluent is 7.3, the COD is 14800mg/L, and the salt content is 20500 mg/L.
The effluent after coagulating sedimentation is used as biochemical effluent to prepare the influent water of a biochemical system, wherein the COD is 4500mg/L and the salinity is 19500 mg/L. The water temperature of the distributed water is heated to 29 ℃, the distributed water sequentially flows through 8 ABR reaction tanks, the retention time in the 8 ABR reaction tanks is 38h totally, the CODcr of the effluent is 720mg/L, and the salt content is 18700 mg/L. The strain type in the ABR reaction tank is phenol degrading bacteria screened after high-efficiency ECM composite bacteria are subjected to ozone oxidation effluent culture, and the addition amount of the phenol degrading bacteria (liquid bacteria) is 5/120 relative to the original water amount. And treating the anaerobic effluent in an aerobic activated sludge tank at 25 ℃ for 25 hours, wherein the effluent CODcr is 158mg/L and the salt content is 18400 mg/L.
Feeding the wastewater after biochemical treatment into a Fenton pool, and sequentially adding ferrous sulfate and hydrogen peroxide which are 0.35g/L and 0.8mL/L relative to the raw water for Fenton reaction, and performing neutralization coagulation precipitation; the reaction time is 25min, and the COD of the flocculated effluent is 45. And recycling a part of the effluent for water distribution for dilution, filtering the rest effluent by sand, performing electrodialysis desalination, directly discharging desalted wastewater with COD (chemical oxygen demand) of 39mg/L and salinity of 421mg/L, and performing evaporative crystallization, wherein the salinity of the brine is 14.5%.
Comparative Experimental example 1
Comparative experiment example 1 and example 2 used the same raw water, and the effluent after ozone oxidation and coagulating sedimentation of example 2 was biochemically treated. Comparative experiment example 1 is different from example 2 in that the type of the strain in the ABR reaction tank at the time of biochemical treatment is high-efficiency ECM complex bacteria (produced by Jiangsu Huaguan environmental protection equipments, Ltd.). The biochemical treatment steps are as follows:
the effluent after coagulating sedimentation is used as biochemical effluent to prepare the influent water of a biochemical system, wherein the COD is 4500mg/L and the salinity is 19500 mg/L. The water temperature of the distributed water is heated to 29 ℃, the distributed water sequentially flows through 8 ABR reaction tanks, the retention time in the 8 ABR reaction tanks is 38h in total, the CODcr of the effluent is 3000mg/L, and the salt content is 19200 mg/L. The strain type in the ABR reaction tank is high-efficiency ECM (Huaguan), and the addition amount of the high-efficiency ECM is about half of the volume of the anaerobic device (the rest volume is filled with volcanic rock filler). And the anaerobic effluent enters an aerobic activated sludge tank for treatment at the temperature of 25 ℃ for 25 hours, the effluent CODcr is 1050mg/L, and the salt content is 18800 mg/L.
Feeding the wastewater after biochemical treatment into a Fenton pool, and sequentially adding ferrous sulfate and hydrogen peroxide which are 0.35g/L and 0.8mL/L relative to the raw water for Fenton reaction, and performing neutralization coagulation precipitation; the reaction time is 25min, and the COD of the flocculated effluent is 498. And recycling a part of the effluent for water distribution for dilution, filtering the rest effluent by sand, performing electrodialysis desalination, and performing evaporative crystallization, wherein COD (chemical oxygen demand) of the desalted wastewater is 374mg/L, the salt content is 421mg/L, and the salt content of the brine is 14.5%.
Comparative experiment example 2
Comparative experiment example 2 the same raw water as in example 2 was used, and effluent water after ozone oxidation and coagulation precipitation in example 2 was used to carry out biochemical treatment, except that the type of the strain in the ABR reaction tank during the biochemical treatment was a general norphenol strain (produced by bevofeng biotechnology limited, fosthan). The biochemical treatment steps are as follows:
the effluent after coagulating sedimentation is used as biochemical effluent to prepare the influent water of a biochemical system, wherein the COD is 4500mg/L and the salinity is 19500 mg/L. Heating the water to 29 ℃, enabling the water to sequentially flow through 8 ABR reaction tanks, wherein the retention time of the water in the 8 ABR reaction tanks is 38h, the CODcr of effluent is 2860mg/L, and the salt content is 19000 mg/L. The strain type in the ABR reaction tank is common phenol-reducing strain (Bivofeng), and the adding amount of the common phenol-reducing strain is about half of the volume of the anaerobic device (the rest volume is filled with volcanic rock filler). And the anaerobic effluent enters an aerobic activated sludge tank for treatment at the temperature of 25 ℃ for 25 hours, the effluent CODcr is 760mg/L, and the salt content is 18500 mg/L.
Feeding the wastewater after biochemical treatment into a Fenton pool, and sequentially adding ferrous sulfate and hydrogen peroxide which are 0.35g/L and 0.8mL/L relative to the raw water for Fenton reaction, and performing neutralization coagulation precipitation; the reaction time is 25min, and the COD of the flocculated effluent is 342. And recycling a part of the effluent for water distribution for dilution, filtering the rest effluent by sand, performing electrodialysis desalination, and performing evaporative crystallization, wherein COD (chemical oxygen demand) of the desalted wastewater is 310mg/L, the salinity is 421mg/L, and the salinity of the brine is 14.5%.
As can be seen from the comparative experimental examples, COD in the wastewater can reach below 40 by using the phenol degrading bacteria screened out after the ozone oxidation effluent culture, while the water quality of the comparative experimental examples 1 and 2 respectively treated by using the high-efficiency ECM composite bacteria sold on the market and the common phenol-reducing bacteria can not reach the discharge standard.
Claims (8)
1. A BDP wastewater treatment method is characterized by comprising the following steps:
(1) ozone oxidation: feeding ozone with the ozone concentration of 150-450 mg/L from the lower part of an ozone reaction tower in a counter-current mode, feeding BDP wastewater with the COD concentration of 12000-18000 mg/L from the upper part of the ozone reaction tower, and carrying out ozone oxidation in the ozone reaction tower for 60-180 s;
(2) biochemical treatment: adjusting the pH value of BDP wastewater after ozone oxidation to 7.0-9.0, performing flocculation and precipitation, and then sequentially entering an ABR anaerobic reaction tank and an aerobic activated sludge tank for advanced treatment; phenol degrading bacteria are put into the ABR anaerobic reaction tank, wherein the phenol degrading bacteria are phenol degrading bacteria screened after efficient ECM composite bacteria are subjected to ozone oxidation effluent culture; the retention time in the ABR anaerobic reaction tank is 32-42 h; the retention time in the aerobic activated sludge tank is 20-30 h;
(3) film treatment: the wastewater after biochemical treatment enters a Fenton pool, ferrous sulfate and hydrogen peroxide are added for Fenton reaction, neutralization coagulation sedimentation is carried out, then sand filtration is carried out, desalting is carried out in an electrodialysis system, and the COD concentration of effluent after desalting is less than 40 mg/L; the salt content is less than 500 mg/L.
2. The BDP wastewater treatment process of claim 1, wherein: the ozone comes from an ozone generator, and an air source of the ozone generator is air or oxygen; the ratio of the addition amount of the ozone to the concentration of COD in the BDP wastewater is 1: 35-45.
3. The BDP wastewater treatment process of claim 1, wherein: the ozone reaction tower is provided with a filler.
4. The BDP wastewater treatment process of claim 1, wherein: the ABR anaerobic reaction tank comprises 8 ABR anaerobic reaction tanks, the aerobic activated sludge tank comprises 2 aerobic activated sludge tanks, and activated carbon fillers are arranged in the ABR anaerobic reaction tanks.
5. The BDP wastewater treatment process of claim 1, wherein: the screening method of the phenol degrading bacteria comprises the following steps: inoculating the high-efficiency ECM complex bacteria into a culture solution with the phenol concentration of 0.5g/L, and carrying out shake culture at the temperature of 28 ℃ and the rotating speed of 160 r/min; then carrying out microbial acclimation on the wastewater subjected to ozone oxidation at the temperature of 30 ℃ and the rotating speed of 160r/min, separating out a single bacterial colony by using a plate dilution method, and storing; inoculating the separated bacterial colony into the wastewater after ozone oxidation, performing shake culture at 30 ℃ and at the rotating speed of 160r/min, measuring the phenol concentration in the culture, and screening out the bacterial strain with the highest phenol degradation rate.
6. The BDP wastewater treatment process of claim 1, wherein: the adding amount of the phenol degrading bacteria is 3-8/120 relative to the original water amount.
7. A BDP wastewater treatment process as set forth in any of the claims 1 to 6, characterized in that: and evaporating the brine obtained after the desalting of the electrodialysis system by using an evaporator to obtain solid salt.
8. The BDP wastewater treatment process of claim 7, wherein: the evaporator is a multi-effect evaporator or an MVR evaporator.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203668181U (en) * | 2014-01-02 | 2014-06-25 | 南京德邦金属装备工程股份有限公司 | Sewage treatment equipment |
| CN104628231A (en) * | 2015-02-12 | 2015-05-20 | 山东默锐环保科技有限公司 | Biochemical-photocatalytic advanced water treatment method for PBBC wastewater |
| WO2015192367A1 (en) * | 2014-06-20 | 2015-12-23 | 必德普(北京)环保科技有限公司 | Bio-dopp sewage denitrification system and sewage denitrification method |
| CN105417887A (en) * | 2015-12-18 | 2016-03-23 | 郑州大学综合设计研究院有限公司 | Clindamycin phosphate waste water processing technology |
| CN206173177U (en) * | 2016-10-22 | 2017-05-17 | 台州市环源环保工程有限公司 | Adhesive organic wastewater system |
| CN106746184A (en) * | 2016-12-02 | 2017-05-31 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for processing epoxychloropropane waste water |
| CN106746159A (en) * | 2015-11-19 | 2017-05-31 | 中国石油化工股份有限公司 | A kind of processing method of antibiotic production wastewater |
| CN107814449A (en) * | 2016-09-13 | 2018-03-20 | 神华集团有限责任公司 | A kind of processing method of brine waste |
| CN107963764A (en) * | 2017-12-28 | 2018-04-27 | 盐城师范学院 | The recovery method of abraum salt in a kind of organic synthesis industry brine waste |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BRPI0802601B1 (en) * | 2008-05-07 | 2018-12-26 | Nattech Consultoria Desenvolvimento E Pesquisa Ind Ltda | detoxification process and wastewater treatment in large volumes with water recycling and utilization of organic and inorganic fillers |
| US20120080374A1 (en) * | 2010-10-04 | 2012-04-05 | Pacific Advanced Civil Engineering, Inc. | Ozone and anaerobic biological pretreatment for a desalination process |
| WO2012118986A1 (en) * | 2011-03-01 | 2012-09-07 | Molycorp Minerals Llc | Contaminant removal from waters using rare earths |
| CN102583908B (en) * | 2012-03-22 | 2013-09-04 | 南京工业大学 | Garbage leachate treatment process |
| CN206266392U (en) * | 2016-11-01 | 2017-06-20 | 北京华福环境工程科技有限公司 | A kind of papermaking wastewater zero-discharge treatment system |
| CN106565063A (en) * | 2016-11-18 | 2017-04-19 | 湖南万容科技股份有限公司 | Disposal method of pyrolysis comprehensive wastewater of solid waste |
| CN106630171A (en) * | 2017-02-03 | 2017-05-10 | 广州市香根草业科技有限公司 | Ecological compound microcirculating sewage treatment method |
-
2018
- 2018-05-04 CN CN201810418431.8A patent/CN108609804B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203668181U (en) * | 2014-01-02 | 2014-06-25 | 南京德邦金属装备工程股份有限公司 | Sewage treatment equipment |
| WO2015192367A1 (en) * | 2014-06-20 | 2015-12-23 | 必德普(北京)环保科技有限公司 | Bio-dopp sewage denitrification system and sewage denitrification method |
| CN104628231A (en) * | 2015-02-12 | 2015-05-20 | 山东默锐环保科技有限公司 | Biochemical-photocatalytic advanced water treatment method for PBBC wastewater |
| CN106746159A (en) * | 2015-11-19 | 2017-05-31 | 中国石油化工股份有限公司 | A kind of processing method of antibiotic production wastewater |
| CN105417887A (en) * | 2015-12-18 | 2016-03-23 | 郑州大学综合设计研究院有限公司 | Clindamycin phosphate waste water processing technology |
| CN107814449A (en) * | 2016-09-13 | 2018-03-20 | 神华集团有限责任公司 | A kind of processing method of brine waste |
| CN206173177U (en) * | 2016-10-22 | 2017-05-17 | 台州市环源环保工程有限公司 | Adhesive organic wastewater system |
| CN106746184A (en) * | 2016-12-02 | 2017-05-31 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for processing epoxychloropropane waste water |
| CN107963764A (en) * | 2017-12-28 | 2018-04-27 | 盐城师范学院 | The recovery method of abraum salt in a kind of organic synthesis industry brine waste |
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