CN105174561A - Treatment process of high-salinity concentrated water difficult to biodegrade - Google Patents
Treatment process of high-salinity concentrated water difficult to biodegrade Download PDFInfo
- Publication number
- CN105174561A CN105174561A CN201510574093.3A CN201510574093A CN105174561A CN 105174561 A CN105174561 A CN 105174561A CN 201510574093 A CN201510574093 A CN 201510574093A CN 105174561 A CN105174561 A CN 105174561A
- Authority
- CN
- China
- Prior art keywords
- water
- difficult
- dense
- biological degradation
- dense water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses a treatment process of high-salinity concentrated water difficult to biodegrade. According to a method, the high-salinity concentrated water difficult to biodegrade is treated through a combined process of dosing hardness removal, microfiltration and electrolysis, hardness, organic matters difficult to degrade and chlorine ions in waste water can be remarkably removed, the effluent quality meets the GB50335 standard about using of recycled water as circulating cooling water supplementary water, and the recycling rate of concentrated water can exceed 95 percent, so that the utilization of water resources is realized, and the environment is protected.
Description
Technical field
The invention belongs to technical field of waste water processing, the treatment process of the dense water of difficult for biological degradation height salt produced after being specifically related to a kind of draining of reverse-osmosis treated petrochemical plant Sewage treatment systems.
Background technology
The sewage reaching discharging standards after the sewage disposal that petroleum chemical enterprise produces can be passed through reverse osmosis (RO) technique and carries out reuse, but the dense water of high salt of 30% ~ 40% difficult for biological degradation can be produced in RO process, wherein mainly comprise total dissolved solid (TDS) and the Persistent organic pollutants of high level, it is very slow that this kind of organic pollutant comprises microbial decomposition speed, decompose halfway organism again, also some organic meta-bolites is comprised, this kind of pollutant chemistry good stability, the time existed in the environment is long, by food chain enrichment, be detrimental to health.Along with the fast development of China's chemical industry, the environmental pollution that the dense water of difficult degradation height salt brings and harm problem also more and more serious, directly cause river water quality salinity to significantly improve, accelerate salinization, Desertification process, bring serious negative impact to ecology.Therefore, the countermeasured to bring inflation under control of the dense water of difficult for biological degradation height salt and technology are important subject of field of Environment Protection always.At present, the treatment process of the dense water of difficult for biological degradation height salt mainly contains Physical, physico-chemical processes, electrochemical process and biological process.
Physical has membrane separation process and distillation method.Membrane separation process utilizes special film to carry out the general designation of selectivity through method to some composition in liquid, and electroosmose process, reverse osmosis method, osmose process etc. all belong to membrane separation process.Membrane separation process as a kind of novel water treatment method compared with conventional water treatment method, have that floor space is little, applied widely, processing efficiency high and device is simple, simple to operate, separation efficiency is high, but because the cost of film is higher, and the tolerance of some film to acid or alkali is poor, membrane separation process investment is also higher.In addition, membrane separation process is higher to pretreated requirement, and single film can not process the hard-degraded substance in high salt sewage effectively, must combine with other method, this all makes membrane separation process process high salt chemical engineering effluent charge remain high, and can not take into account environmental benefit and economic benefit well.Distillation method required equipment is simple and compact for structure, processing ease, volatile and not volatile separating substances can be come, also liquid mixtures different for boiling point can be separated, safe and reliable to operation, technology maturation, but distillation plant is perishable, fouling, and investment and running cost all relatively high.
The method of electrochemical oxidation degradable organic pollutant mainly contains Electrocatalytic Oxidation method and Indirect Electrooxidation.The former is that the free radical (as hydroxyl radical free radical) utilizing electrode surface to produce carrys out oxidative degradation organism; The latter is that the oxygenant (as hypochlorous acid) generated carrys out oxidative degradation organism.In the process of high salt wastewater electrochemical treatment method, adopt Indirect Electrooxidation more, because the Cl in sewage
-can discharge on anode, the chlorine of a generation part is dissolved and in the solution secondary reaction is occurred and generate hypochlorite and oxymuriate, plays oxidation and bleaching action to organism, and high salinity organic sewage is because of containing C1
-, Na
+, Ca
2+, Mg
2+, SO
4 2-, CO
3 2-deng mineral ion, have good specific conductivity, adopt electrochemical method process to be one and reasonably select, this method can remove the organism in sewage effectively, purifies liquid waste.
Biological process comprises activated sludge process, biomembrance process, anaerobic reaction method, acidication-aerobic integrated process etc., Biological Treatment of Wastewater comparatively physical method to have construction investment low, the advantages such as working cost is low, and operational administrative is simple.But Cl in this type of waste water
-considerably beyond water in routine biochemistry process to the inhibition concentration of microorganism, although the biodegradability of water increases after pre-treatment, Cl
-change, total salt concentration does not change, from microbiological angle, the water body of high salt concentration can reduce the activity of water, be unfavorable for microbial growth, only have some may grow very well in hypersaline environment addicted to salt, salt-durable microbe, by tame and screening obtains salt-durable microbe, improve biological treatment system to the endurance of high salt, thus ensure normally carrying out of biochemical treatment.Therefore, as adopted biological process, the endurance of biological treatment system to high chlorine root, high saliferous is key factor, and microorganism has biological activity at a certain temperature simultaneously, the microorganism active that goes beyond the scope can reduce, and temperature is also the restraining factors of wastewater biological method treatment process.
But in engineer applied, above-mentioned single treatment technology water outlet is often difficult to reach required standard.
Summary of the invention
Technical problem to be solved by this invention is the shortcoming overcoming the existence of above-mentioned difficult for biological degradation height salt concentrated water treatment method, there is provided a kind of economically feasible, the simple to operate and combined treatment process technology that processing efficiency is high, water outlet can reach recirculated cooling water moisturizing standard-required.
Solving the problems of the technologies described above adopted technical scheme is: the dense water of difficult for biological degradation height salt produced after the draining of reverse-osmosis treated sewage from oil refinery treatment system is placed in dense tank, calcium oxide and sodium carbonate is metered in dense tank, make the calcium in water, magnesium ion changes into calcium carbonate, magnesium hydroxide, then inorganic carbon film device is adopted to carry out cross flow filter to it, water outlet after filtration enters electrolyzer, and hydrogen peroxide 30 ~ 60mg/L is added in the water outlet in electrolyzer, be 10 ~ 30A at electric current, voltage is electrolysis 3 ~ 6 hours under the condition of 5 ~ 10V, water outlet after electrolysis treatment can reach recirculated cooling water moisturizing standard.
BOD in the dense water of difficult for biological degradation height salt of the present invention
5be 10 ~ 60mg/L, COD
crbe 60 ~ 200mg/L, Cl
-content is 250 ~ 550mg/L, total hardness be 450 ~ 2000mg/L, TDS is 1000 ~ 2700mg/L.
Above-mentioned inorganic carbon film device is provided by Zhejiang Zhongkai Ripe Environmental Engineering Co., Ltd., it is the micro-filtration product adopting the best inorganic Carbon Materials (SiC) of wetting ability to manufacture, film core is polynuclear plane, the porosity of film is greater than 45%, aperture is 0.1 ~ 3 μm, the porosity of preferred film is 90%, and aperture is 1 μm.
Above-mentioned electrolyzer be make negative electrode with carbon steel tank skin, the Ti electrode of surface-coated nickel oxide coating layer makes anode.
The present invention adopts the technique that dosing removes firmly, micro-filtration filters, electrolysis combines to process the dense water of difficult for biological degradation height salt, and dosing is softening except middle most of hardness and the some organic pollutants of anhydrating, also can reduce the total dissolved solid of dense water simultaneously; The inorganic carbon film with excellent contamination resistance, high filtration flux, superpower chemical stability (the pH value scope of application 0 ~ 14) and great physical strength is adopted to carry out cross flow filter, film cored structure adopts polynuclear plane, the porosity of film is up to 45%, its filtration flux can up to more than five of conventional ceramic film times, most of hardness and some organic pollutants in water can be removed, purify water; Electrolysis treatment can remove hardness and chlorion in water, the strong oxidizer labile organic compound such as free chlorine, ozone, hydroxyl radical free radical of anode generation simultaneously, Killing Microorganisms In Water.
The inventive method can make effluent quality reach GB50335 reuse water and be used as recirculated cooling water make up water standard, and dense Water Sproading utilization ratio can reach more than 95%, realizes protecting environment again while water resources utilizes.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is described in more detail, but protection scope of the present invention is not limited only to these embodiments.
Embodiment 1
With dense water (the quantity discharged 100m of difficult for biological degradation height salt produced after the draining of reverse-osmosis treated sewage from oil refinery treatment system
3/ hour) be example, its concrete water quality is in table 1.
The dense water water quality of table 1
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Control criterion (mg/L≤) | 10 | 60 | 250 | 450 | 350 | 1000 |
| Dense water water quality (mg/L) | 12 | 101 | 351 | 650.1 | 525.8 | 1086 |
Note: in table, control criterion is that in GB50335-2002, reuse water is used as recirculated cooling water make up water standard set quota.
As can be seen from Table 1, the dense water BOD/COD (0.11) that reverse osmosis produces is on the low side, and hardness, basicity are higher than moisturizing standard, and water quality has the characteristic of high saliferous, difficult for biological degradation.
As shown in Figure 1, the dense water of above-mentioned for 1L difficult for biological degradation height salt is placed in dense tank, 0.506g calcium oxide, 0.236g sodium carbonate is added in dense tank, make the calcium in water, magnesium ion changes into calcium carbonate, magnesium hydroxide suspends precipitation, then inorganic carbon film device is adopted to carry out cross flow filter to it, except the most of carbonate in anhydrating and non-carbonate hardness and part Persistent organic pollutants.The film core of inorganic carbon film device is polynuclear plane, and the porosity of film is 90%, and aperture is 1 μm.The concentrated solution horizontal centrifuge that inorganic carbon film device cross flow filter produces carries out solid-liquid separation, and centrifugate returns dense tank and proceeds process, the solid residue outward transport after centrifugal.950mL water outlet after inorganic carbon film device cross flow filter enters electrolyzer, and in the water outlet in electrolyzer, add 57mg hydrogen peroxide (adding 60mg hydrogen peroxide in the water outlet namely after often liter of cross flow filter), electrolyzer be make negative electrode with carbon steel tank skin, the Ti electrode of surface-coated nickel oxide coating layer makes anode, electric current be 20A, voltage be the condition of 6.7V under electrolysis 6 hours, except middle chlorion, Persistent organic pollutants and the hardness of anhydrating, the effluent quality after electrolysis treatment is in table 2.
Table 2 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 0 | 31 | 152 | 61.5 | 210.3 | 395 |
| Clearance (%) | 100 | 69.3 | 56.7 | 90.5 | 60 | 63.6 |
From table 2, the water outlet COD after process drops to 31mg/L by the 101mg/L of former water, clearance 69.3%; Chlorion drops to 152mg/L from 351mg/L, clearance 56.7%; Hardness drops to 61.5mg/L, clearance 90.5%, and effluent quality reaches recirculated cooling water moisturizing standard, and dense Water Sproading utilization ratio can reach more than 95%.
Comparative example 1
In embodiment 1, electrolysis time foreshortens to 2 hours, and other processing condition and embodiment 1, effluent quality is in table 3.
Table 3 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 0 | 71 | 270.8 | 75.5 | 192.3 | 562 |
| Clearance (%) | 100 | 29.7 | 22.8 | 88.4 | 63.4 | 48.2 |
From table 3, the water outlet COD after the method process only drops to 71mg/L by the 101mg/L of former water, and clearance is 29.7%; Chlorion only drops to 270.8mg/L from 351mg/L, and clearance is 22.8%; TDS clearance is also only 48.2%, and in water outlet, COD and chlorion all to exceed in GB50335-2002 reuse water and be used as recirculated cooling water make up water standard set quota.
Comparative example 2
In embodiment 1, do not add hydrogen peroxide, other processing condition and embodiment 1, effluent quality is in table 4.
Table 4 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 0 | 65 | 258.7 | 63.5 | 192.3 | 492 |
| Clearance (%) | 100 | 35.6 | 26.4 | 90.2 | 63.4 | 54.7 |
From table 4, the method is all very low to the clearance of COD, chlorion and TDS, and the clearance of COD is only 35.6%, and the clearance that the clearance of chlorion is only 26.4%, TDS is only 54.7%, and it is for COD and Cl
-after slightly exceeding the dense water treatment of standard, effluent quality still cannot be up to standard, and COD and chlorion all exceed standard.
Embodiment 2
In embodiment 1, changing hydrogen peroxide add-on is 28.5mg (adding 30mg hydrogen peroxide in the water outlet namely after often liter of cross flow filter), and other processing condition and embodiment 1, effluent quality is in table 5.
Table 5 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 0 | 51 | 195.7 | 63.5 | 192.3 | 492 |
| Clearance (%) | 100 | 49.5 | 44.2 | 90.2 | 63.4 | 54.7 |
From table 5, the water outlet COD after process drops to 51mg/L by the 101mg/L of former water, clearance 49.5%; Chlorion drops to 195.7mg/L from 351mg/L, clearance 44.2%; Hardness drops to 63.5mg/L, clearance 90.2%, TDS clearance 54.7%, and effluent quality reaches recirculated cooling water moisturizing standard, and dense Water Sproading utilization ratio can reach more than 95%.
Embodiment 3
In embodiment 1, change dense water water quality (dense water water quality is specifically in table 6), other processing condition and embodiment 1, effluent quality is in table 7.
The dense water water quality of table 6
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Dense water water quality (mg/L) | 51 | 182 | 451 | 1250.1 | 544.0 | 1988 |
Table 7 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 5.9 | 49.1 | 197.1 | 150.4 | 192.3 | 720 |
| Clearance (%) | 88.4 | 73.0 | 56.3 | 88.0 | 64.6 | 63.8 |
From table 7, the water outlet COD after process drops to 49.1mg/L by the 182mg/L of former water, clearance 73.0%; Chlorion drops to 197.1mg/L from 451mg/L, clearance 56.3%; Hardness drops to 150.4mg/L, clearance 88%; TDS clearance 63.8%, effluent quality reaches recirculated cooling water moisturizing standard, and dense Water Sproading utilization ratio can reach more than 95%.
Embodiment 4
In embodiment 3, the membrane pore size changing inorganic carbon film device is 3 μm, and other processing condition are identical with embodiment 3, and effluent quality is in table 8.
Table 8 effluent quality
| Index | BOD 5 | COD Cr | Cl - | Total hardness | Total alkalinity | TDS |
| Effluent quality (mg/L) | 8.7 | 52.3 | 199.2 | 293.1 | 252.5 | 814 |
| Clearance (%) | 82.9 | 71.3 | 55.8 | 76.6 | 53.6 | 59.0 |
From table 8, the water outlet COD after process drops to 52.3mg/L by the 182mg/L of former water, clearance 71.3%; Chlorion drops to 199.2mg/L from 451mg/L, clearance 55.8%; Hardness drops to 293.1mg/L, clearance 76.6%; TDS clearance 59.0%, effluent quality reaches recirculated cooling water moisturizing standard, and dense Water Sproading utilization ratio can reach more than 95%.
Claims (5)
1. the dense water technology of difficult for biological degradation height salt, it is characterized in that: the dense water of difficult for biological degradation height salt produced after the draining of reverse-osmosis treated sewage from oil refinery treatment system is placed in dense tank, calcium oxide and sodium carbonate is metered in dense tank, make the calcium in water, magnesium ion changes into calcium carbonate, magnesium hydroxide, then inorganic carbon film device is adopted to carry out cross flow filter to it, water outlet after filtration enters electrolyzer, and hydrogen peroxide 30 ~ 60mg/L is added in the water outlet in electrolyzer, be 10 ~ 30A at electric current, voltage is electrolysis 3 ~ 6 hours under the condition of 5 ~ 10V, namely water outlet after electrolysis treatment reaches recirculated cooling water moisturizing standard.
2. the dense water technology of difficult for biological degradation height salt according to claim 1, is characterized in that: BOD in the described dense water of difficult for biological degradation height salt
5be 10 ~ 60mg/L, COD
crbe 60 ~ 200mg/L, Cl
-content is 250 ~ 550mg/L, total hardness be 450 ~ 2000mg/L, TDS is 1000 ~ 2700mg/L.
3. the dense water technology of difficult for biological degradation height salt according to claim 1, is characterized in that: the film core of described inorganic carbon film device is polynuclear plane, and the porosity of film is greater than 45%, and aperture is 0.1 ~ 3 μm.
4. the dense water technology of difficult for biological degradation height salt according to claim 1, is characterized in that: the film core of described inorganic carbon film device is polynuclear plane, and the porosity of film is 90%, and aperture is 1 μm.
5. the dense water technology of difficult for biological degradation height salt according to claim 1, is characterized in that: described electrolyzer be make negative electrode with carbon steel tank skin, the Ti electrode of surface-coated nickel oxide coating layer makes anode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510574093.3A CN105174561A (en) | 2015-09-10 | 2015-09-10 | Treatment process of high-salinity concentrated water difficult to biodegrade |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510574093.3A CN105174561A (en) | 2015-09-10 | 2015-09-10 | Treatment process of high-salinity concentrated water difficult to biodegrade |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105174561A true CN105174561A (en) | 2015-12-23 |
Family
ID=54897100
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510574093.3A Pending CN105174561A (en) | 2015-09-10 | 2015-09-10 | Treatment process of high-salinity concentrated water difficult to biodegrade |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105174561A (en) |
Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4852698A (en) * | 1971-11-05 | 1973-07-24 | ||
| JPS4934497A (en) * | 1972-07-31 | 1974-03-29 | ||
| US4746441A (en) * | 1986-02-21 | 1988-05-24 | Kabushiki Kaisha Sanshin Seisakusho | Method of purifying brine for electrolytic chemical production |
| DE20306347U1 (en) * | 2002-05-30 | 2003-07-24 | GEHLERT WASSERTECHNIK GmbH, 63755 Alzenau | Device for producing a sodium hypochlorite solution comprises a water softener connected to the cathode chambers of a membrane electrolysis cell, and a salt solution container connected to the anode chambers of the cell for introducing sols |
| JP2004121969A (en) * | 2002-10-01 | 2004-04-22 | Kurita Water Ind Ltd | Cooling water treatment method |
| CN102320641A (en) * | 2011-05-25 | 2012-01-18 | 吉林大学 | Resource utilization method for saponification waste water producing epoxypropane by chlorohydrination process |
| CN102381788A (en) * | 2011-09-05 | 2012-03-21 | 常州大学 | Electrolytic oxidation process for raising aromatic alcohol waste water biodegradability |
| CN102452751A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Deep desalting and recycling method for industrial wastewater |
| CN102863105A (en) * | 2012-09-12 | 2013-01-09 | 浙江工商大学 | Technology and system for treating high-salt high-nitrogen high-organic matter chemical wastewater |
| CN103265133A (en) * | 2013-06-14 | 2013-08-28 | 波鹰(厦门)科技有限公司 | Recycling method of papermaking advanced treatment wastewater based on chemical decalcification |
| US20130248375A1 (en) * | 2012-03-02 | 2013-09-26 | Miox Corporation | Waste to Product On Site Generator |
| CN103754828A (en) * | 2013-12-23 | 2014-04-30 | 内蒙古工业大学 | Sodium dichromate closed circulation clean production method for preparing sodium chlorate |
| CN203741143U (en) * | 2013-12-18 | 2014-07-30 | 厦门紫金矿冶技术有限公司 | Electrolysis pretreatment system of saliferous wastewater in mine |
| CN104556533A (en) * | 2013-10-15 | 2015-04-29 | 中国石油化工股份有限公司 | Treatment method for reverse osmosis concentrated water |
-
2015
- 2015-09-10 CN CN201510574093.3A patent/CN105174561A/en active Pending
Patent Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4852698A (en) * | 1971-11-05 | 1973-07-24 | ||
| JPS4934497A (en) * | 1972-07-31 | 1974-03-29 | ||
| US4746441A (en) * | 1986-02-21 | 1988-05-24 | Kabushiki Kaisha Sanshin Seisakusho | Method of purifying brine for electrolytic chemical production |
| DE20306347U1 (en) * | 2002-05-30 | 2003-07-24 | GEHLERT WASSERTECHNIK GmbH, 63755 Alzenau | Device for producing a sodium hypochlorite solution comprises a water softener connected to the cathode chambers of a membrane electrolysis cell, and a salt solution container connected to the anode chambers of the cell for introducing sols |
| JP2004121969A (en) * | 2002-10-01 | 2004-04-22 | Kurita Water Ind Ltd | Cooling water treatment method |
| CN102452751A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Deep desalting and recycling method for industrial wastewater |
| CN102320641A (en) * | 2011-05-25 | 2012-01-18 | 吉林大学 | Resource utilization method for saponification waste water producing epoxypropane by chlorohydrination process |
| CN102381788A (en) * | 2011-09-05 | 2012-03-21 | 常州大学 | Electrolytic oxidation process for raising aromatic alcohol waste water biodegradability |
| US20130248375A1 (en) * | 2012-03-02 | 2013-09-26 | Miox Corporation | Waste to Product On Site Generator |
| CN102863105A (en) * | 2012-09-12 | 2013-01-09 | 浙江工商大学 | Technology and system for treating high-salt high-nitrogen high-organic matter chemical wastewater |
| CN103265133A (en) * | 2013-06-14 | 2013-08-28 | 波鹰(厦门)科技有限公司 | Recycling method of papermaking advanced treatment wastewater based on chemical decalcification |
| CN104556533A (en) * | 2013-10-15 | 2015-04-29 | 中国石油化工股份有限公司 | Treatment method for reverse osmosis concentrated water |
| CN203741143U (en) * | 2013-12-18 | 2014-07-30 | 厦门紫金矿冶技术有限公司 | Electrolysis pretreatment system of saliferous wastewater in mine |
| CN103754828A (en) * | 2013-12-23 | 2014-04-30 | 内蒙古工业大学 | Sodium dichromate closed circulation clean production method for preparing sodium chlorate |
Non-Patent Citations (5)
| Title |
|---|
| 吴智淼: "《工业循环冷却水处理技术与监测控制方法及标准规范实务全书（三）》", 31 December 2002 * |
| 展惠英: "《环境化学》", 30 June 2008 * |
| 张元兴等: "《生物反应器工程》", 31 October 2001 * |
| 李国彬: "宏伟热电厂水系统优化的探索与应用", 《黑龙江电力》 * |
| 王学松: "《气体膜技术》", 30 June 2010 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Aljuboury et al. | Treatment of petroleum wastewater by conventional and new technologies-A review | |
| CN105541017B (en) | Method and device for zero emission of strong brine | |
| CN104016547B (en) | A kind of coking waste water deep treatment zero-emission process | |
| Awaleh et al. | Waste water treatment in chemical industries: the concept and current technologies | |
| CN102786183B (en) | Method for processing garbage leachate | |
| Venu et al. | Treatment of stabilized landfill leachate using peroxicoagulation process | |
| Xiong et al. | Recovery of NH3-N from mature leachate via negative pressure steam-stripping pretreatment and its benefits on MBR systems: A pilot scale study | |
| CN102786182B (en) | Device for processing landfill leachate | |
| CN105540967A (en) | Processing method for reducing and recycling organic waste water and processing system | |
| CN103265133B (en) | Recycling method of papermaking advanced treatment wastewater based on chemical decalcification | |
| CN105399287B (en) | A kind of organic wastewater with difficult degradation thereby integrated treatment and Zero discharge treatment method and its system | |
| CN104743717A (en) | Method and system for reduction of concentrated brine | |
| Battistelli et al. | Application of low-density electric current to performance improvement of membrane bioreactor treating raw municipal wastewater | |
| CN107381712A (en) | Difficult degradation, high-salt wastewater strengthen the photoelectricity catalytic ozonation method administered | |
| Wilk et al. | Electrochemical oxidation of landfill leachate using boron-doped diamond anodes: pollution degradation rate, energy efficiency and toxicity assessment | |
| CN111170587A (en) | Spraying wastewater treatment process | |
| Bashir et al. | Effects of ion exchange resins in different mobile ion forms on semi-aerobic landfill leachate treatment | |
| CN202610073U (en) | Processing apparatus of garbage percolating liquid | |
| Beni et al. | Petroleum wastewater treatment | |
| CN105461107A (en) | Water resource recovering technology for coking wastewater biochemical treatment effluent | |
| CN110563232A (en) | Mineral recovery and zero discharge process for high-salinity high-organic-matter wastewater | |
| CN110683687A (en) | Method and device for improving quality of reclaimed water | |
| CN105174561A (en) | Treatment process of high-salinity concentrated water difficult to biodegrade | |
| Wei et al. | Petrochemical wastewater and produced water | |
| Nowak et al. | Treatment and utilization of the concentrate from membrane separation processes of landfill leachates |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20151223 |
|
| RJ01 | Rejection of invention patent application after publication |