CN111847747A - System and method for treating high-salinity high-organic-matter wastewater - Google Patents
System and method for treating high-salinity high-organic-matter wastewater Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000002351 wastewater Substances 0.000 title claims abstract description 33
- 239000005416 organic matter Substances 0.000 title claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 150000003839 salts Chemical class 0.000 claims abstract description 12
- 239000012466 permeate Substances 0.000 claims description 66
- 238000001223 reverse osmosis Methods 0.000 claims description 60
- 238000001704 evaporation Methods 0.000 claims description 42
- 230000008020 evaporation Effects 0.000 claims description 38
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 30
- 238000000926 separation method Methods 0.000 claims description 29
- 239000012528 membrane Substances 0.000 claims description 24
- 239000004576 sand Substances 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 9
- 238000001728 nano-filtration Methods 0.000 claims description 9
- 238000010612 desalination reaction Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 7
- 239000012141 concentrate Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 3
- 239000010865 sewage Substances 0.000 abstract description 6
- 238000004065 wastewater treatment Methods 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000009287 sand filtration Methods 0.000 description 12
- 239000000126 substance Substances 0.000 description 12
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 238000004043 dyeing Methods 0.000 description 7
- 238000007639 printing Methods 0.000 description 7
- 238000001514 detection method Methods 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005188 flotation Methods 0.000 description 3
- 238000010979 pH adjustment Methods 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000013043 chemical agent Substances 0.000 description 2
- 239000003712 decolorant Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 239000003899 bactericide agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000006352 cycloaddition reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- QGBSISYHAICWAH-UHFFFAOYSA-N dicyandiamide Chemical compound NC(N)=NC#N QGBSISYHAICWAH-UHFFFAOYSA-N 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- -1 focuses on physical Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000000269 nucleophilic effect Effects 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 230000002085 persistent effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- GNHOJBNSNUXZQA-UHFFFAOYSA-J potassium aluminium sulfate dodecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GNHOJBNSNUXZQA-UHFFFAOYSA-J 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
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- Water Supply & Treatment (AREA)
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- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the technical field of wastewater treatment, in particular to a system and a method for treating high-salinity high-organic-matter wastewater. The sewage is treated by the treatment system and the method, so that the energy consumption can be greatly reduced, the salt and the organic matters are basically separated, the cost for treating ton water is greatly reduced, and the equipment is convenient to operate.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a system and a method for treating high-salinity high-organic-matter wastewater.
Background
The problem of water pollution is always concerned in the development process of human socioeconomic, and how to effectively remove persistent and nondegradable high-concentration salts and organic pollutants in wastewater is an environmental problem concerned by people.
At present, the treatment method of the waste water mainly focuses on physical, chemical and biological methods, and achieves certain achievement, specifically: 1) the physical and chemical treatment method is characterized in that a large amount of impurities which are difficult to biodegrade or insoluble are contained in the wastewater and need to be removed by physical and chemical methods such as grid filtration, dosing coagulation precipitation, air flotation and the like, so that the load of subsequent biochemical treatment is reduced, and the biochemical treatment efficiency is improved. 2) The biochemical treatment method is to decompose organic matters in the printing and dyeing wastewater by utilizing the oxidation or reduction of microorganisms to destroy easily degradable unsaturated bonds and chromophoric groups, thereby achieving the purpose of treating the wastewater by utilizing the microbial technology. 3) An advanced oxidation treatment method, which utilizes the oxidation reduction technology such as ozone or medicament to decompose macromolecular substances which are difficult to degrade in the biochemical treatment stage into micromolecular substances and simultaneously improve the biodegradability of water body, or directly mineralize organic substances which are difficult to degrade to generate CO 2、H2O and N2And the like. The water quality of effluent water treated by the current wastewater generally has COD of 200-500mg/L, chroma of 200-300mg and TN of 30-50mg/L, and still cannot meet the requirements of discharge or water quality recycling, and the main problem is that the residual COD in the treated effluent water is organic matters which are difficult to be biochemically degraded or not degraded, and the commonly adopted methods such as coagulation, precipitation, adsorption, air flotation and the like are difficult to remove.
The common advanced wastewater treatment technologies mainly comprise a Fenton oxidation method, an electrochemical oxidation method and an ozone oxidation method, the former two technologies have secondary pollution due to the need of adding chemical agents or increasing sludge amount, and the application range is small. At present, the ozone oxidation method is applied more, the main way is direct reaction and indirect reaction, namely the direct reaction is that ozone directly reacts with pollutants through cycloaddition, electrophilic or nucleophilic action; the indirect reaction is that ozone generates hydroxyl with stronger oxidability under the action of illumination, catalyst or other factorsA free radical. For example, 2014 Guoshei, et al, published patent No. CN103570165A, is characterized in that the wastewater is subjected to pretreatment of adjusting aeration, neutralizing coagulation and precipitation, and then subjected to combined treatment by microwave, photoelectrocatalysis and industrial waste residue filtration and adsorption. For example, in 2016 publication of patent publication No. CN105858950A by Silent et al, a method and a device for advanced treatment of printing and dyeing wastewater by ozone and hydrogen peroxide activated carbon are characterized in that H is added into the effluent of a rapid mixing tank 2O2Then the wastewater enters an ozone contact tank and then enters an activated carbon filter tank, wherein the activated carbon contains load Fe2O3-CuO-MnO2-CeO2The catalyst, ozone, is added in stages. For example, published patent publication No. CN106630472A of Tortoise-Fei et al in 2017, a process for treating printing and dyeing wastewater is characterized in that the printing and dyeing wastewater is pretreated and biochemically treated, then enters a deep high-efficiency shallow air flotation machine and is treated by adding a flocculating agent, and finally enters an oxidation decolorant. For example, in 2017, the publication No. CN106986500A of Licong, a method for treating printing and dyeing wastewater is characterized in that the printing and dyeing wastewater is pretreated by filtration, flocculation and the like; then the wastewater enters an anaerobic hydrolysis acidification tank and an aerobic tank, the effluent is added with sodium hypochlorite, sodium hydroxide and the effluent finally enters an activated carbon filter to finish wastewater treatment. As disclosed in chenhongxing in 2019, patent publication No. CN109231694A, a process for treating printing and dyeing wastewater, which is characterized by removing particulate impurities through several steps, such as a first step of filtration and separation; adding dicyandiamide and formaldehyde decolorants; adding iron trichloride, aluminum potassium sulfate dodecahydrate, aluminum hydroxide, potassium permanganate, polyacrylamide and other medicaments; and step four, carrying out disinfection treatment by using ozone, and discharging the sewage which meets the standard.
Obviously, in the disclosed wastewater treatment process, a large amount of chemical agents, bactericides and active carbon are added, so that the salt content of the wastewater is easily increased; and secondly, the utilization rate of ozone is low, the sludge amount is increased, and the catalyst is easy to cause secondary pollution. And the prior process structure for treating the wastewater by the physical and chemical treatment method is more complex. Some treatment processes are simple evaporation processes, and have the problems of high energy consumption, difficult separation of salt and organic matters, easy pollution and blockage of pipelines, high cost for treatment of ton water, complex operation and the like in the process operation process.
Disclosure of Invention
In order to solve the problems in the background art, the invention provides a system and a method for treating high-salinity high-organic wastewater.
In order to achieve the purpose, the invention provides the following technical scheme: the utility model provides a processing system of high organic matter waste water of high salt, includes concentrated separator, one section reverse osmosis unit, two-stage reverse osmosis unit and evaporation plant, concentrated separator one section reverse osmosis unit two-stage reverse osmosis unit and evaporation plant establish ties in proper order and set up, concentrated separator with evaporation plant is linked together.
Preferably, the concentration and separation device comprises a nanofiltration membrane, the first-stage reverse osmosis device and the second-stage reverse osmosis device both comprise a disc tube type reverse osmosis membrane, and the evaporation device is a triple-effect evaporation device.
Preferably, the device further comprises a sand filter which is communicated with the concentration and separation device.
The invention also provides a treatment method of high-salinity and high-organic matters based on the treatment system, which comprises the following steps:
s1, filtering the wastewater through a sand filter;
s2, adding hydrochloric acid into the filtered water obtained in the step S1, and adjusting the pH value of the filtered water to 6.3-6.6;
s3, performing pressure separation on the filtered water adjusted by hydrochloric acid in the step S2 through a concentration separation device to obtain a first permeate and a first concentrated solution;
s4, introducing the first concentrated solution into an evaporation device for evaporation treatment;
s5, introducing the first permeate into the first-stage reverse osmosis device for pressure separation to obtain a second permeate and a second concentrated solution;
s6, introducing the second concentrated solution into the second-stage reverse osmosis device for pressure separation, and simultaneously discharging the second permeate or introducing the second permeate into the second-stage reverse osmosis device for pressure separation again; separating the second concentrated solution and/or the second permeate through the two-stage reverse osmosis device to obtain a third permeate and a third concentrated solution;
s7, introducing the third concentrated solution into an evaporation device for evaporation treatment; discharging the third permeate.
Preferably, in step S3, the operation pressure of the concentration and separation device is 0.4-0.7 MPa, the CODcr concentration of the first permeate is 60-100 mg/l, the electrical conductivity is 39000-41000 mus/cm, the pH value is 6.2-6.5, the CODcr concentration of the first concentrate is 28000-29000 mg/l, the electrical conductivity is 44000-48000 mus/cm, and the pH value is 6.3-6.7.
Preferably, in the step S5, the desalination rate of the first permeate in the first-stage reverse osmosis device is 95% to 97.5%, and the operating pressure of the first-stage reverse osmosis device is 6.5 to 7.6 MPa.
Preferably, the CODcr concentration of the second permeate liquid in the step S5 is 5-20 mg/l, the conductance is 1000-2000 mus/cm, and the pH is 6.1-6.4; the CODcr concentration of the second concentrated solution is 180-240 mg/l, the conductance is 76000-82000 mu s/cm, and the pH value is 6.4-6.8.
Preferably, in the step S6, the desalination rate of the second permeate in the second-stage reverse osmosis device is 95-98%, and the operating pressure of the second-stage reverse osmosis device is 9-11 MPa.
Preferably, the CODcr concentration of the third permeate liquid in the step S6 is 0-10 mg/l, the conductance is 1600-2800 mus/cm, and the pH value is 6.0-6.4; the CODcr concentration of the third concentrated solution is 200-400 mg/l, the conductance is 106000-118000 mu s/cm, and the pH value is 6.4-7.0.
Preferably, the hydrochloric acid is industrial hydrochloric acid.
The invention has the beneficial effects that: according to the invention, the high-salinity high-organic-matter wastewater is filtered and separated step by step for multiple times through the reverse osmosis devices which are sequentially connected in series, so that the filtering effect of the system is greatly increased, and the organic matters, the salt content and the like in the filtered water are greatly reduced; most of sewage is purified in a filtering and separating mode, the rest of a small part of high-concentration sewage (concentrated solution) is purified in an evaporating mode, and the two modes are matched with each other, so that the operation energy consumption of the system can be greatly reduced, and the cost of sewage treatment is saved; the sewage treatment process is simple, the operation is convenient, excessive chemical reagents are not introduced in the treatment process, and secondary pollution is avoided.
Drawings
FIG. 1 is a process system flow diagram of the present invention.
Wherein: 1-a concentration separation device, 2-a first-stage reverse osmosis device, 3-a second-stage reverse osmosis device, 4-an evaporation device and 5-a sand filter.
Detailed Description
The present invention will be described in further detail below with reference to specific embodiments and drawings, but the present invention is not limited to the specific embodiments below.
The following examples are not provided to limit the scope of the present invention, nor are the steps described to limit the order of execution, and the directions described are limited to the drawings. Modifications of the invention which are obvious to those skilled in the art in view of the prior art are also within the scope of the invention as claimed.
The utility model provides a processing system of high salt high organic matter, as shown in figure 1, includes concentration separator 1, one section reverse osmosis unit 2, two-stage segment reverse osmosis unit 3 and evaporation plant 4, concentration separator one section reverse osmosis unit two-stage segment reverse osmosis unit and evaporation plant establish ties in proper order and set up, concentration separator with evaporation plant is linked together.
In this embodiment, concentration separator includes the nanofiltration membrane, one section reverse osmosis unit and two-stage reverse osmosis unit all include dish tubular reverse osmosis membrane, evaporation plant is triple effect evaporation plant.
In this embodiment, a sand filter 5 is further included, which is in communication with the concentration and separation device.
A treatment method for high-salt and high-organic matters comprises the following steps:
s1, filtering the wastewater through a sand filter;
s2, adding hydrochloric acid into the filtered water obtained in the step S1, wherein the hydrochloric acid is industrial hydrochloric acid, and adjusting the pH value of the filtered water to 6.3-6.6;
s3, performing pressure separation on the filtered water adjusted by hydrochloric acid in the step S2 through a concentration separation device to obtain a first permeate and a first concentrated solution;
s4, introducing the first concentrated solution into an evaporation device for evaporation treatment;
S5, introducing the first permeate into the first-stage reverse osmosis device for pressure separation to obtain a second permeate and a second concentrated solution;
s6, introducing the second concentrated solution into the second-stage reverse osmosis device for pressure separation, and simultaneously discharging the second permeate or introducing the second permeate into the second-stage reverse osmosis device for pressure separation again; separating the second concentrated solution and/or the second permeate through the two-stage reverse osmosis device to obtain a third permeate and a third concentrated solution;
s7, introducing the third concentrated solution into an evaporation device for evaporation treatment; discharging the third permeate.
In this embodiment, the operation pressure of the concentration and separation device in step S3 is 0.4-0.7 MPa, the CODcr concentration of the first permeate is 60-100 mg/l, the conductance is 39000-41000 μ S/cm, the pH value is 6.2-6.5, the CODcr concentration of the first concentrate is 28000-29000 mg/l, the conductance is 44000-48000 μ S/cm, and the pH value is 6.3-6.7.
In this embodiment, in step S5, the desalination rate of the first permeate in the first-stage reverse osmosis device is 95% to 97.5%, and the operating pressure of the first-stage reverse osmosis device is 6.5 to 7.6 MPa.
In this embodiment, the second permeate solution in step S5 has a CODcr concentration of 5-20 mg/l, an electrical conductance of 1000-2000 μ S/cm, and a pH of 6.1-6.4; the CODcr concentration of the second concentrated solution is 180-240 mg/l, the conductance is 76000-82000 mu s/cm, and the pH value is 6.4-6.8.
In this embodiment, the desalination rate of the second permeate in the second-stage reverse osmosis device in step S6 is 95-98%, and the operating pressure of the second-stage reverse osmosis device is 9-11 MPa.
In this embodiment, the third permeate solution in step S6 has a CODcr concentration of 0-10 mg/l, an electrical conductance of 1600-2800 μ S/cm, and a pH of 6.0-6.4; the CODcr concentration of the third concentrated solution is 200-400 mg/l, the conductance is 106000-118000 mu s/cm, and the pH value is 6.4-7.0.
Example 1
The process is used for treating high-salinity and high-organic wastewater of a chemical plant. The high-salt and high-organic wastewater of the chemical plant is firstly treated by a sand filter, the CODcr concentration of the produced water after sand filtration treatment is 3000mg/l, the conductance is 42000 mu s/cm, and the pH value is 8.2.
10 tons of sand filtration produced water is taken, and then industrial hydrochloric acid is added into the sand filtration produced water to adjust the pH value to 6.5. And then separating the sand filtration produced water after the pH adjustment by using a nanofiltration membrane, wherein the operating pressure of the nanofiltration membrane is 0.6MPa, and obtaining 9 tons of first permeate and 1 ton of first concentrated solution after separation, the CODcr concentration of the first permeate is 80mg/l, the electric conductivity is 40000 mu s/cm, the pH value is 6.4, the CODcr concentration of the first concentrated solution is 29000mg/l, the electric conductivity is 46000 mu s/cm, and the pH value is 6.6.
And then evaporating the first concentrated solution by an evaporation device. The first permeate is treated by a first section of disc-tube reverse osmosis membrane to obtain 6.3 tons of second permeate and 2.7 tons of second concentrated solution, the salt rejection rate of the first section of disc-tube reverse osmosis membrane is 96.4%, and the operating pressure is 7.0 MPa. Through detection, the CODcr concentration of the second permeate is 10mg/l, the conductance is 1500 mus/cm, the pH is 6.3, and the second permeate reaches the discharge standard; the second concentrate CODcr had a concentration of 200mg/l, a conductance of 80000. mu.s/cm, and a pH of 6.7. And treating the second concentrated solution by using a second disc-tube type reverse osmosis membrane to obtain 1.1 ton of third permeate and 1.6 ton of third concentrated solution, wherein the desalination rate of the second disc-tube type reverse osmosis membrane is 96.05%, and the operating pressure is 10 MPa. Through detection, the CODcr concentration of the third permeate is 7mg/l, the conductance is 2000 mus/cm, the pH value is 6.2, and the third permeate is discharged after reaching the standard; the CODcr concentration of the third concentrated solution is 300mg/l, the conductance is 118000 mu s/cm, the pH value is 6.8, and the third concentrated solution is introduced into an evaporation device for evaporation treatment.
Example 2
The method is adopted to treat the high-salinity and high-organic wastewater of a chemical plant. The high-salt and high-organic wastewater of the chemical plant is firstly treated by a sand filter, the CODcr concentration of the produced water after the sand filtration treatment is 2900mg/l, the conductance is 43000 mu s/cm, and the pH value is 8.0.
10 tons of sand filtration produced water is taken, and then industrial hydrochloric acid is added into the sand filtration produced water to adjust the pH value to 6.6. And then separating the sand filtration produced water after the pH adjustment by using a nanofiltration membrane, wherein the operating pressure of the nanofiltration membrane is 0.7MPa, and obtaining 9 tons of first permeate and 1 ton of first concentrated solution after separation, the CODcr concentration of the first permeate is 100mg/l, the conductance is 41000 mu s/cm, the pH value is 6.5, the CODcr concentration of the first concentrated solution is 28000mg/l, the conductance is 44600 mu s/cm, and the pH value is 6.7.
And then evaporating the first concentrated solution by an evaporation device. The first permeate is treated by a first section of disc-tube reverse osmosis membrane to obtain 6.5 tons of second permeate and 2.5 tons of second concentrated solution, the salt rejection rate of the first section of disc-tube reverse osmosis membrane is 97%, and the operating pressure is 7.6 MPa. Through detection, the CODcr concentration of the second permeate is 5mg/l, the conductance is 1000 mus/cm, the pH is 6.4, and the second permeate reaches the discharge standard; the second concentrate CODcr had a concentration of 180mg/l, a conductance of 76000. mu.s/cm and a pH of 6.8. And treating the second concentrated solution by using a second disc-tube type reverse osmosis membrane to obtain 1.1 ton of third permeate and 1.6 ton of third concentrated solution, wherein the desalination rate of the second disc-tube type reverse osmosis membrane is 97.92%, and the operating pressure is 11 MPa. Through detection, the CODcr concentration of the third permeate is 3mg/l, the conductance is 1600 mus/cm, the pH value is 6.4, and the third permeate reaches the discharge standard; the CODcr concentration of the third concentrated solution is 200mg/l, the conductance is 106000 mu s/cm, the pH value is 7.0, and the third concentrated solution is introduced into an evaporation device for evaporation treatment.
Example 3
The method is adopted to treat the high-salinity and high-organic wastewater of a chemical plant. The high-salt and high-organic wastewater of the chemical plant is firstly treated by a sand filter, the CODcr concentration of the produced water after the sand filtration treatment is 2900mg/l, the electric conductivity is 41000 mu s/cm, and the pH value is 8.1.
10 tons of sand filtration produced water is taken, and then industrial hydrochloric acid is added into the sand filtration produced water to adjust the pH value to 6.3. And then separating the sand filtration produced water after the pH adjustment by using a nanofiltration membrane, wherein the operating pressure of the nanofiltration membrane is 0.4MPa, and 9 tons of first permeate and 1 ton of first concentrated solution are obtained after separation, the CODcr concentration of the first permeate is 60mg/l, the conductance is 39000 mu s/cm, the pH value is 6.2, the CODcr concentration of the first concentrated solution is 28000mg/l, the conductance is 44600 mu s/cm, and the pH value is 6.4.
And then evaporating the first concentrated solution by an evaporation device. The first permeate is treated by a first section of disc-tube reverse osmosis membrane to obtain 6.8 tons of second permeate and 2.2 tons of second concentrated solution, the salt rejection rate of the first section of disc-tube reverse osmosis membrane is 96.6%, and the operating pressure is 6.6 MPa. Through detection, the CODcr concentration of the second permeate is 20mg/l, the conductance is 2000 mus/cm, the pH is 6.1, and the second permeate reaches the discharge standard; the second concentrate CODcr had a concentration of 240mg/l, an electrical conductance of 82000. mu.s/cm and a pH of 6.5. And treating the second concentrated solution by using a second disc tube type reverse osmosis membrane to obtain 1.0 ton of third permeate and 1.73 ton of third concentrated solution, wherein the desalination rate of the second disc tube type reverse osmosis membrane is 95.83%, and the operating pressure is 9 MPa. Through detection, the CODcr concentration of the third permeate is 8mg/l, the electric conductivity is 2700 mus/cm, the pH value is 6.1, and the third permeate is discharged after reaching the standard; the CODcr concentration of the third concentrated solution is 400mg/l, the conductance is 118000 mu s/cm, the pH value is 6.8, and the third concentrated solution is introduced into an evaporation device for evaporation treatment.
Claims (10)
1. The utility model provides a processing system of high salt high organic matter, its characterized in that, includes concentration separator (1), one section reverse osmosis unit (2), two-stage segment reverse osmosis unit (3) and evaporation plant (4), concentration separator one section reverse osmosis unit two-stage segment reverse osmosis unit and evaporation plant establish ties in proper order and set up, concentration separator with evaporation plant is linked together.
2. The high-salinity and high-organic matter treatment system according to claim 1, wherein the concentration and separation device comprises a nanofiltration membrane, the first-stage reverse osmosis device and the second-stage reverse osmosis device comprise a disc tube type reverse osmosis membrane, and the evaporation device is a triple-effect evaporation device.
3. The high-salinity high-organic matter treatment system according to claim 2, characterized in that the system further comprises a sand filter (5), wherein the sand filter is communicated with the concentration and separation device.
4. The method for treating high salinity and high organic matter based on the treatment system of any one of claims 1 to 3, characterized in that the method comprises the following steps:
s1, filtering the wastewater through a sand filter;
s2, adding hydrochloric acid into the filtered water obtained in the step S1, and adjusting the pH value of the filtered water to 6.3-6.6;
S3, performing pressure separation on the filtered water adjusted by hydrochloric acid in the step S2 through a concentration separation device to obtain a first permeate and a first concentrated solution;
s4, introducing the first concentrated solution into an evaporation device for evaporation treatment;
s5, introducing the first permeate into the first-stage reverse osmosis device for pressure separation to obtain a second permeate and a second concentrated solution;
s6, introducing the second concentrated solution into the second-stage reverse osmosis device for pressure separation, and simultaneously discharging the second permeate or introducing the second permeate into the second-stage reverse osmosis device for pressure separation again; separating the second concentrated solution and/or the second permeate through the two-stage reverse osmosis device to obtain a third permeate and a third concentrated solution;
s7, introducing the third concentrated solution into an evaporation device for evaporation treatment; discharging the third permeate.
5. The method according to claim 4, wherein the operation pressure of the concentration and separation device in step S3 is 0.4-0.7 MPa, the CODcr concentration of the first permeate is 60-100 mg/l, the conductance is 39000-41000 μ S/cm, the pH value is 6.2-6.5, the CODcr concentration of the first concentrate is 28000-29000 mg/l, the conductance is 44000-48000 μ S/cm, and the pH is 6.3-6.7.
6. The method for treating high-salinity high-organic matter according to claim 4, wherein the first permeate in the step S5 has a desalination rate of 95% to 97.5% in the first-stage reverse osmosis device, and the first-stage reverse osmosis device has an operating pressure of 6.5 to 7.6 MPa.
7. The method for treating high-salt and high-organic compounds according to claim 4, wherein the second permeate solution in step S5 has a CODcr concentration of 5-20 mg/l, an electrical conductance of 1000-2000 μ S/cm, and a pH of 6.1-6.4; the CODcr concentration of the second concentrated solution is 180-240 mg/l, the conductance is 76000-82000 mu s/cm, and the pH value is 6.4-6.8.
8. The method for treating high-salinity high-organic matter according to claim 4, wherein the second permeate in step S6 has a salt rejection ratio of 95-98% in the second-stage reverse osmosis device, and the operating pressure of the second-stage reverse osmosis device is 9-11 MPa.
9. The method for treating high-salt and high-organic compounds according to claim 4, wherein the third permeate solution in step S6 has a CODcr concentration of 0-10 mg/l, an electrical conductance of 1600-2800 μ S/cm, and a pH of 6.0-6.4; the CODcr concentration of the third concentrated solution is 200-400 mg/l, the conductance is 106000-118000 mu s/cm, and the pH value is 6.4-7.0.
10. The method for treating high-salinity high-organic matter according to claim 4, wherein the hydrochloric acid is industrial hydrochloric acid.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114790059A (en) * | 2022-04-11 | 2022-07-26 | 倍杰特集团股份有限公司 | Device and method for concentrating and filtering concentrated water of synthetic ammonia and ethylene glycol wastewater |
| CN116177647A (en) * | 2023-02-23 | 2023-05-30 | 山东大学 | High-salt organic wastewater evaporation crystallization salt-making equipment |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114790059A (en) * | 2022-04-11 | 2022-07-26 | 倍杰特集团股份有限公司 | Device and method for concentrating and filtering concentrated water of synthetic ammonia and ethylene glycol wastewater |
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| CN116177647A (en) * | 2023-02-23 | 2023-05-30 | 山东大学 | High-salt organic wastewater evaporation crystallization salt-making equipment |
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