CN101885568A - High-salinity waste water treatment method - Google Patents
High-salinity waste water treatment method Download PDFInfo
- Publication number
- CN101885568A CN101885568A CN 201010248027 CN201010248027A CN101885568A CN 101885568 A CN101885568 A CN 101885568A CN 201010248027 CN201010248027 CN 201010248027 CN 201010248027 A CN201010248027 A CN 201010248027A CN 101885568 A CN101885568 A CN 101885568A
- Authority
- CN
- China
- Prior art keywords
- waste water
- water
- salinity
- layer
- gaseous
- 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
Images
Landscapes
- Biological Treatment Of Waste Water (AREA)
Abstract
The invention belongs to the technical field of environmental protection, and in particular relates to a high-salinity waste water treatment method. The high-salinity waste water treatment method is implemented by the following steps of: A, applying 7 to 9 standard atmospheric pressures to gaseous dimethyl enther for liquefaction, and mixing the liquefied dimethyl enther and the high-salinity waste water at the temperature of between 25 and 35 DEG C; B, forming a water-containing dimethyl enther layer and a waste water layer with higher salinity, demixing and separating the liquid; C, depressurizing the water-containing dimethyl enther layer obtained by the step B, and feeding the depressurized water-containing dimethyl enther layer into a distilling tower for distilling, wherein the dimethyl enther is changed into gaseous state and separated from water; the gaseous dimethyl enther is collected and reused; and the waste water produced by distilling is fed into a biological treatment system for treatment; and D, repeating the steps on the gaseous dimethyl enther obtained by the step C and the waste water layer with higher salinity obtained by the step B, wherein the salt concentration in the waste water with high salinity is gradually increased, and salt is separated out after concentration. The separated salt is recycled. The separation technology separates the water from the waste water with high salinity, and has an energy consumption of about 1,100kJ/kg, about half that of the evaporation method.
Description
Technical field
The invention belongs to environmental protection technical field, be specifically related to a kind of treatment process of high salinity waste water.
Background technology
High salinity waste water is one of present unmanageable waste water, and this waste water not only contains (as oil, organism, heavy metal and radioactive substance etc.) multiple material, also contains a large amount of as Cl
-, SO
4 2-, Na
+, Ca
2+Etc. solvability inorganic salt material.Contained solvability salt is many more in the waste water, and ionic strength is big more, and general microorganism is difficult to growth and breeding more, so traditional biological process is difficult to handle high salinity waste water.And physico-chemical processes evaporation concentration method running cost height commonly used, energy expenditure is big, and concentrated residue liquid need carry out burning disposal, and facility investment and working cost are higher.
According to the solvent pairing effect, partial organic substances matter can make the solubleness of salt in water reduce.Organic pollutant in water and the water also has certain solubleness in organic solvent, but the solubleness of salt in organic solvent is very low.Utilize above-mentioned principle, can realize that water separates with brinish, progressively improve the final salt of brinish concentration and can separate out and resource utilization.Particularly adopt dme can realize separating of dme and water well, realize that with minimum energy consumption water separates with brinish.
Summary of the invention
The high-salinity waste water treatment method that the purpose of this invention is to provide a kind of efficient, less energy-consumption.
A kind of treatment process of high salinity waste water is characterized in that realizing as follows:
A, with gaseous dimethyl 7-9 standard atmospheric pressure liquefaction of pressurizeing, under temperature 25-35 ℃, liquefied dimethyl ether is mixed with high salinity waste water;
The waste water that B, the moisture dme layer of formation and salinity are higher is two-layer, treats to carry out the separatory separation after the layering;
C, moisture dme layer that step B is obtained by decompression after, enter the distillation tower distillation, dme becomes gaseous state and water sepn, gaseous dimethyl is collected and is utilized, the waste water that distillation produces enters biological treatment system and handles;
The waste water layer that the salinity that D, the gaseous dimethyl that step C is obtained and step B obtain is higher repeats above-mentioned steps, and the salt concn in the high salinity waste water progressively improves, and salts out after concentrating.The salt of separating out carries out resource utilization.
Biological treatment system described in the present invention refers to and utilizes biology in the treatment system, and Metabolic activity of microorganism particularly and various characteristics are handled the system of all contaminations, comprise activated sludge process, biomembrance process and combination process thereof.Can be biological treatment tank as biological treatment system, this biological treatment tank contains inlet, outlet, filler, aerating apparatus; Waste water is entered by inlet, and outlet is discharged, and the organic pollutant in the water is removed by the saccharomycetic complex microorganism that contains of biofilm on filler, and aerating apparatus provides microorganism growth needed oxygen.As a kind of optimal way filler is combined fiber filler, elastic solid filler, Pall ring or fibrous nodules filler.
The present invention has following advantage:
1, a kind of high-salinity waste water treatment method provided by the invention, be that dme is mixed with high salinity waste water, the saturation solubility of water in dme is 8wt%, after portion water enters the dme layer, moisture dme layer separates with brine layer, and the concentration of salt is improved in the brine layer.Moisture dme layer is taked to reduce pressure and the mode that heats just can make dme and water sepn, and dme recycles.So repeat, salt can be separated out after progressively concentrating in the waste water.
2, adopt above-mentioned isolation technique that water is separated from high salinity waste water, its energy consumption is about 1100kJ/kg, is about half of method of evaporation.
3, employed raw material organic solvent dme is cheap, easily decomposes, and toxicity is low, and environmental influence is little, can reuse.
4, the removal effect of salt is good, and the salt clearance of high salinity waste water is reached more than 99%.
Description of drawings
Accompanying drawing 1 is a dme salt water separating system schema.
Fig. 2 is the cross-sectional view of biological treatment tank.
Embodiment
Now reaching embodiment in conjunction with the accompanying drawings further is described in down the present invention:
Embodiment 1
Gaseous dimethyl is pressurized to 7 standard atmospheric pressure liquefaction, under 35 ℃ of temperature, gets the 10L liquefied dimethyl ether and mix with the high salinity waste water that 1L contains 15% sodium-chlor.
Treat that carrying out separatory after moisture dme layer and the waste water layer layering separates.Enter the distillation tower distillation after separating the moisture dme layer decompression that obtains, collect gaseous dimethyl.Separate the waste water obtain and leave standstill and treat that sodium-chlor separates out after-filtration, filter and obtain saturated sodium-chloride waste water.
The pressurized liquefied back of gaseous dimethyl that distillation tower distillation is obtained and saturated sodium-chloride waste water repeat the above-mentioned step mix, separatory separates, distilation steps, sodium-chlor will all be separated out.
The waste water that twice distillation tower produced merges, and its saltiness is 0.2% to enter biological treatment system and handle.The sodium chloride salt recycling that the salt that twice crystallization separated out obtains through recrystallization.
Described biological treatment system is a biological treatment tank, and this biological treatment tank 5 contains inlet 1, outlet 2, filler 4 and aerating apparatus 3; Waste water is entered by inlet 1, and outlet 2 is discharged, and the organic pollutant in the water is removed by the saccharomycetic complex microorganism that contains of biofilm on combined fiber filler 4, and aerating apparatus 3 provides microorganism growth needed oxygen.
Embodiment 2
Gaseous dimethyl is pressurized to 9 standard atmospheric pressure liquefaction, under 25 ℃ of temperature, gets the 12L liquefied dimethyl ether and mix with the high salinity waste water that 1L contains 10% sodium sulfate.
Treat that carrying out separatory after moisture dme layer and the waste water layer layering separates, entering the distillation tower distillation after separating the moisture dme layer decompression that obtains, collect gaseous dimethyl.Separate the waste water obtain and leave standstill and treat that sodium sulfate separates out after-filtration, filter and obtain saturated sodium sulfate waste water.
The pressurized liquefied back of gaseous dimethyl that distillation tower distillation is obtained and saturated sodium sulfate waste water repeat the above-mentioned step mix, separatory separates, distilation steps, sodium sulfate will all be separated out.
The waste water that twice distillation tower produced merges, and its saltiness is 0.1% to enter biological treatment system and handle.The sodium sulfate salt recycling that the salt that twice crystallization separated out obtains through recrystallization.
Described biological treatment system is a biological treatment tank, and this biological treatment tank 5 contains inlet 1, outlet 2, filler 4 and aerating apparatus 3; Waste water is entered by inlet 1, and outlet 2 is discharged, and the organic pollutant in the water is removed by the saccharomycetic complex microorganism that contains of biofilm on fibrous nodules filler 4, and aerating apparatus 3 provides microorganism growth needed oxygen.
Claims (2)
1. the treatment process of a high salinity waste water is characterized in that realizing as follows:
A, with gaseous dimethyl 7-9 standard atmospheric pressure liquefaction of pressurizeing, under temperature 25-35 ℃, liquefied dimethyl ether is mixed with high salinity waste water;
The waste water that B, the moisture dme layer of formation and salinity are higher is two-layer, treats to carry out the separatory separation after the layering;
C, moisture dme layer that step B is obtained by decompression after, enter the distillation tower distillation, dme becomes gaseous state and water sepn, gaseous dimethyl is collected and is utilized, the waste water that distillation produces enters biological treatment system and handles;
The waste water layer that the salinity that D, the gaseous dimethyl that step C is obtained and step B obtain is higher repeats above-mentioned steps, and the salt concn in the high salinity waste water progressively improves, and salts out after concentrating.The salt of separating out carries out resource utilization.
2. the treatment process of a kind of high salinity waste water according to claim 1 is characterized in that described biological treatment system is a biological treatment tank, and this biological treatment tank (5) contains inlet (1), outlet (2), filler (4) and aerating apparatus (3); Waste water is entered by inlet (1), and outlet (2) is discharged, and the organic pollutant in the water is removed by the saccharomycetic complex microorganism that contains of biofilm on filler (4), and aerating apparatus (3) provides microorganism growth needed oxygen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010248027 CN101885568A (en) | 2010-08-06 | 2010-08-06 | High-salinity waste water treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010248027 CN101885568A (en) | 2010-08-06 | 2010-08-06 | High-salinity waste water treatment method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101885568A true CN101885568A (en) | 2010-11-17 |
Family
ID=43071692
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010248027 Pending CN101885568A (en) | 2010-08-06 | 2010-08-06 | High-salinity waste water treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101885568A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3135742A1 (en) | 2015-08-27 | 2017-03-01 | Shell Internationale Research Maatschappij B.V. | Process for oil recovery |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4710301A (en) * | 1985-09-30 | 1987-12-01 | S.A. Innovi N.V. | Wastewater purification process |
| CN1034537A (en) * | 1987-10-29 | 1989-08-09 | 清华大学 | Acetonitrile with salt phase-splitting process for refining |
-
2010
- 2010-08-06 CN CN 201010248027 patent/CN101885568A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4710301A (en) * | 1985-09-30 | 1987-12-01 | S.A. Innovi N.V. | Wastewater purification process |
| CN1034537A (en) * | 1987-10-29 | 1989-08-09 | 清华大学 | Acetonitrile with salt phase-splitting process for refining |
Non-Patent Citations (3)
| Title |
|---|
| 《中国优秀硕士学位论文全文数据库 基础科学辑》 20080915 张宁 高盐度浓海水的冷冻脱盐技术研究 A010-13 1-2 , 第09期 2 * |
| 《应用化学》 20051130 林金清等 亲水有机相-含盐水两相体系的形成机理与分相能力 第1203-1207页 1-2 第22卷, 第11期 2 * |
| 《环境科学研究》 20061231 彭光霞等 高含盐有机废水MDAT-IAT生物处理工艺研究 第71-74页 1-2 第19卷, 第3期 2 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3135742A1 (en) | 2015-08-27 | 2017-03-01 | Shell Internationale Research Maatschappij B.V. | Process for oil recovery |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Zico et al. | Sustainable ammonia resource recovery from landfill leachate by solar-driven modified direct contact membrane distillation | |
| Date et al. | Zero liquid discharge technology for recovery, reuse, and reclamation of wastewater: A critical review | |
| US10781143B2 (en) | Method and plant for treatment of organic waste | |
| CN102633414B (en) | Method for treating sludge and extracting organic substances by using microwave | |
| CN102249498B (en) | Biochemical treatment method for waste water from small and medium-sized starch factories | |
| US20110219668A1 (en) | Method of using contaminated water from an oilwell effluent stream | |
| CN106396234A (en) | Zero-discharge treatment method for reverse osmosis concentrated water | |
| CN105236650B (en) | A kind of wastewater treatment method | |
| KR101312809B1 (en) | Complex method of foodwaste leachate using the pulpwastewater engineering | |
| CN102276113A (en) | Combined fresh water increment method of forward osmosis membrane bioreactor / reverse osmosis | |
| CN108996865A (en) | Pretreatment method and device for producing biogas from sludge | |
| CN110550833A (en) | System and method for recycling carbon, nitrogen, phosphorus and water in sewage | |
| Shi et al. | Water and green ammonia recovery from anaerobic digestion effluent by two-stage membrane distillation | |
| CN109455865A (en) | A kind of epoxy propane waste water pretreating process | |
| CN106219852B (en) | Novel method and device for comprehensively treating benzyl alcohol production wastewater | |
| CN108349766A (en) | The system for handling organic detritus by hydrothermal carbonization | |
| CN103601616B (en) | Alcohol-water separation recycling method of Fischer-Tropsch synthesis reaction water | |
| CN201284276Y (en) | System for extracting concentrated liquor from water at deep layer of ocean | |
| CN102757153A (en) | Method for treating wastewater generated during production of 12-hydroxy stearic acid | |
| CN108531401A (en) | A method of utilizing the useless mash of microalgae processing molasses | |
| CN101885568A (en) | High-salinity waste water treatment method | |
| CN104609606B (en) | A kind of petrochemical wastewater preprocess method | |
| CN205528214U (en) | High advanced oxidation - who contains salt industrial waste water divides salt crystallization combined system | |
| CN201250135Y (en) | Disposing device capable of efficiently removing the ammonia nitrogen in ammonia-nitrogen wastewater | |
| CN102731262A (en) | Method for recovering phenolic compounds from coal-derived oil products |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20101117 |