CN114590944A - Resource treatment method for nanofiltration membrane brackish water - Google Patents
Resource treatment method for nanofiltration membrane brackish water Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 46
- 239000012528 membrane Substances 0.000 title claims abstract description 39
- 238000001728 nano-filtration Methods 0.000 title claims abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title description 8
- 239000012267 brine Substances 0.000 claims abstract description 44
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 44
- 150000003839 salts Chemical class 0.000 claims abstract description 37
- 238000000926 separation method Methods 0.000 claims abstract description 29
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 21
- JRKICGRDRMAZLK-UHFFFAOYSA-L peroxydisulfate Chemical compound [O-]S(=O)(=O)OOS([O-])(=O)=O JRKICGRDRMAZLK-UHFFFAOYSA-L 0.000 claims abstract description 21
- 230000003647 oxidation Effects 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 9
- 239000007800 oxidant agent Substances 0.000 claims abstract description 8
- 230000001590 oxidative effect Effects 0.000 claims abstract description 5
- 238000004064 recycling Methods 0.000 claims abstract description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 10
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 10
- 235000011152 sodium sulphate Nutrition 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 9
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 6
- CHQMHPLRPQMAMX-UHFFFAOYSA-L sodium persulfate Chemical compound [Na+].[Na+].[O-]S(=O)(=O)OOS([O-])(=O)=O CHQMHPLRPQMAMX-UHFFFAOYSA-L 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 3
- YMGGAHMANIOXGP-UHFFFAOYSA-L disodium;oxido sulfate Chemical compound [Na+].[Na+].[O-]OS([O-])(=O)=O YMGGAHMANIOXGP-UHFFFAOYSA-L 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 238000007725 thermal activation Methods 0.000 claims description 2
- 239000012295 chemical reaction liquid Substances 0.000 claims 1
- 230000001678 irradiating effect Effects 0.000 claims 1
- 238000004321 preservation Methods 0.000 claims 1
- 238000005070 sampling Methods 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 10
- 230000007547 defect Effects 0.000 abstract description 5
- 239000010842 industrial wastewater Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 description 19
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 14
- 239000000243 solution Substances 0.000 description 11
- 238000001994 activation Methods 0.000 description 6
- 230000004913 activation Effects 0.000 description 6
- 238000004939 coking Methods 0.000 description 6
- 238000002425 crystallisation Methods 0.000 description 6
- 230000008025 crystallization Effects 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000002189 fluorescence spectrum Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000007832 Na2SO4 Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 2
- 230000003213 activating effect Effects 0.000 description 2
- -1 anion salt Chemical class 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000004021 humic acid Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- PUKLDDOGISCFCP-JSQCKWNTSA-N 21-Deoxycortisone Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@@](C(=O)C)(O)[C@@]1(C)CC2=O PUKLDDOGISCFCP-JSQCKWNTSA-N 0.000 description 1
- FCYKAQOGGFGCMD-UHFFFAOYSA-N Fulvic acid Natural products O1C2=CC(O)=C(O)C(C(O)=O)=C2C(=O)C2=C1CC(C)(O)OC2 FCYKAQOGGFGCMD-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 229940095100 fulvic acid Drugs 0.000 description 1
- 239000002509 fulvic acid Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 231100000956 nontoxicity Toxicity 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000002604 ultrasonography 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- 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
- C02F1/048—Purification of waste water by 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
- C02F2101/38—Organic compounds containing nitrogen
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/20—Total organic carbon [TOC]
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
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- 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
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Abstract
The present invention provides: a recycling treatment method of strong brine in a salt separation process of a nanofiltration membrane comprises advanced oxidation, wherein the strong brine generated by the separation of the nanofiltration membrane is treated by adopting an advanced oxidation method, so that the total organic carbon content of the strong brine is reduced; preheating, namely, removing the residual persulfate oxidant in the concentrated brine by preheating; the invention makes up the defects of the prior art, overcomes the defects of poor treatment effect and unstable operation of the strong brine generated in the salt separation process of the nanofiltration membrane in the prior art, and ensures the realization of the target of zero discharge of industrial wastewater.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a resource treatment method of strong brine in a salt separation process of a nanofiltration membrane.
Background
The wastewater recycling and resource utilization in the industrial industries such as steel, coal chemical industry, coking and the like are realized by adopting the technologies of pretreatment, biochemical treatment, advanced treatment, double-membrane method and evaporative crystallization. The double membrane is formed by combining a nanofiltration membrane and a reverse osmosis membrane, wherein the nanofiltration membrane is mainly used for separating divalent anion salt (mainly sodium sulfate salt) and monovalent anion salt (mainly sodium chloride salt) in wastewater. The strong brine wastewater generated in the nanofiltration salt separation process has high sodium sulfate content, high COD and poor biodegradability. Because the concentration of organic matters in the high-salinity wastewater is high, if the high-salinity wastewater directly enters the evaporative crystallization unit without being pretreated, on one hand, the foaming phenomenon is serious in the evaporative crystallization process, and the operation of the evaporative crystallization unit is influenced; on the other hand, the purity of the subsequent Na2SO4 crystal salt is reduced, and the crystal salt is impure and has no recovery value. Therefore, the concentration of the organic matters in the concentrated wastewater of the salt separation membrane is reduced, and the method has important significance for the continuous safety of an evaporative crystallization system and the guarantee of the purity of the crystallized salt reaching the standard.
The traditional Fenton (Fenton), O3, activated persulfate and other advanced oxidation technologies can remove organic matters in the concentrated wastewater of the salt separation membrane to a certain extent. However, the Fenton process introduces new impurities into the nanofiltration membrane concentrated brine, such as Fe2+ and Fe3+ in the Fenton reaction; crushing a catalyst used in the process of catalyzing ozone and dissolving out metal substances; a metal ion catalyst used for activating persulfate, and the like. Meanwhile, the high inorganic salt component of the concentrated brine is deposited on the surface of the catalyst to inhibit the activity of the catalyst, so that the above methods are not suitable for separating organic matters in the nanofiltration membrane concentrated wastewater and cannot be used as a resource technical method.
The persulfate advanced oxidation technology based on energy activation has the advantages of high oxidation-reduction potential of free radicals, simple and convenient generation, wide pH application and the like, and becomes a new technology for treating refractory organic pollutants. At present, main energy activation means comprise ultraviolet light, ultrasound, microwave and the like, and an ultraviolet light activation method (UV + PS) is widely concerned due to the characteristics of simple operation, environmental protection, high reaction efficiency and the like. The ultraviolet light activation method (UV + PS) can be coupled with other advanced oxidation modes, so that a better treatment effect is obtained, the input cost of light energy can be saved, and the economic benefit is higher. The technology is introduced into the treatment of the nanofiltration membrane concentrated brine, and the method has the remarkable advantages that firstly, reduction products of persulfate are all sulfate radicals, secondary impurities cannot be brought, and even if a small amount of persulfate is left, the persulfate can be thoroughly eliminated through subsequent heating and evaporation processes; secondly, the ultraviolet light activation mode is easy to realize engineering and does not bring new impurities; finally, the project provides an ozone synergistic mode, the efficiency of the ultraviolet light activated persulfate method can be further improved, and organic matters in the concentrated brine can be efficiently removed. Therefore, the invention provides a new idea for the treatment of the nanofiltration membrane concentrated brine.
Disclosure of Invention
Technical problem to be solved
Aiming at the defects of the prior art, the invention provides a recycling treatment method of concentrated brine in a nanofiltration membrane salt separation process, which aims to solve the problems in the background art.
(II) technical scheme
In order to achieve the purpose, the invention is realized by the following technical scheme: a resource treatment method for strong brine in a nanofiltration membrane salt separation process comprises the following steps
S1: advanced oxidation, namely treating the strong brine generated by the separation of the nanofiltration membrane by adopting an advanced oxidation method to reduce the total organic carbon content of the strong brine;
s2: preheating, namely, removing the residual persulfate oxidant in the concentrated brine by preheating;
s2: and (4) evaporating and concentrating, namely evaporating and crystallizing preheated concentrated brine through an evaporator to obtain sodium sulfate with the purity reaching the industrial salt recovery standard.
Preferably, the advanced oxidation method treatment process in the step 1 is specifically that persulfate is added into concentrated brine generated in the salt separation process of the nanofiltration membrane, the concentrated brine is irradiated by ultraviolet light and is introduced with ozone, oxidation reaction is carried out under the condition of full stirring, total organic carbon in the reaction solution is sampled and detected until the content is lower than 15mg/L, and the reaction is terminated.
As a further preference, the persulfate is specifically one or a mixture of both of sodium peroxymonosulfate and sodium peroxydisulfate.
More preferably, the molar ratio of the added persulfate to the total organic carbon in the concentrated brine is 1: 1 to 20: 1.
more preferably, the amount of ozone added is 10-100 mg/(L.min).
Further preferably, the ultraviolet irradiation in the advanced oxidation method is performed by using an ultraviolet lamp having an irradiation wavelength of less than 300nm and an ultraviolet intensity of more than 0.5 μ Einstein s-1.
Preferably, the preheating temperature in the step 2 is 80 ℃ at the lowest, the temperature is kept for more than 30 minutes, and the residual oxidant is removed through thermal activation.
(III) advantageous effects
The invention provides a resource treatment method of strong brine in a nanofiltration membrane salt separation process, which has the following beneficial effects: the method is used for the resource treatment of the strong brine in the salt separation process of the nanofiltration membrane; by using a UV advanced oxidation process, oxidizing agents persulfate and ozone are catalytically decomposed to generate free radicals with extremely strong oxidability, such as sulfate radical free radicals, hydroxyl free radicals and the like, so that various pollutants in water are decomposed or mineralized, organic matters in wastewater can be effectively removed, simultaneously, the preheating energy is used for further activating and eliminating the persulfate oxidizing agent remained in the concentrated salt water, and the concentrated salt oxidizing agent is evaporated and crystallized to obtain the sodium sulfate salt with the purity reaching the industrial salt recovery standard.
The method has good treatment effect, combines sulfate radicals with no toxicity, environmental protection and strong oxidation performance, has little influence on the generation of the sulfate radicals by water quality, does not introduce other impurity elements to influence the subsequent salt purification, has the advantages of simple equipment, simple and convenient operation and the like, and has no pollution, high stability and more economy.
The method makes up for the defects of the prior art, overcomes the defects of poor treatment effect and unstable operation of the strong brine generated in the salt separation process of the nanofiltration membrane in the prior art, and ensures the realization of the zero discharge target of the industrial wastewater.
Drawings
FIG. 1 is a flow chart of a resource treatment method of concentrated brine in a nanofiltration membrane salt separation process of the invention;
FIG. 2 shows UV + PS + O in example 1 of the present invention3Removing quinoline and TOC effect graphs;
FIG. 3 is a graph showing the effect of removing persulfate during the preheating process;
FIG. 4 is a three-dimensional fluorescence spectrum of the coking wastewater before the advanced oxidation treatment in example 2;
FIG. 5 is a diagram showing a matter of example 2, before the advanced oxidation treatment of the coking wastewater;
FIG. 6 is a three-dimensional fluorescence spectrum of the coking wastewater after the advanced oxidation treatment in example 2;
FIG. 7 is a diagram showing a sample after the advanced oxidation treatment of the coking wastewater in example 2.
Detailed Description
The invention discloses a resource treatment method of concentrated brine in a nanofiltration membrane salt separation process, which is further detailed by specific embodiments.
Example 1
An application of a resource treatment method of concentrated brine in a salt separation process of a nanofiltration membrane in a Quinoline (QL) -containing high-salt solution is as follows:
step 1: 1000mg/L of QL solution and 75000mg/L of Na2SO4 solution are prepared, 12mL of QL solution and 48mL of Na2SO4 solution are put into a reactor, and then pure water is added to 240 mL. Adding 0.5g/L NaS2O8 solution, introducing O3, and adding 20 mg/(L.min) of O3 to obtain a reaction solution. Adjusting the temperature to 20 ℃ and the pH value to 7, then putting the reaction solution into a photoreactor for reaction, using UV light to irradiate, wherein the ultraviolet light intensity is 0.6 mu Einstein & s < -1 >, and keeping the concentration of each component in the reaction solution uniform through electromagnetic stirring. The reaction temperature is controlled by a low-temperature constant-temperature tank in the experimental process, and the reaction time is 60 min.
And 2, step: the reacted solution was heated to 80 ℃ for 8 h.
And step 3: and (4) evaporating and crystallizing the preheated strong brine through an evaporator to obtain sodium sulfate with the purity reaching the industrial salt recovery standard.
And (3) testing results:
the effect of the UV + PS + O3 system on quinoline and TOC removal is shown in figure 2. The reaction is carried out for 60min under the experimental conditions, the removal rate of quinoline by the UV + PS + O3 system is 90.78%, and the TOC content is reduced to below 15 mg/L.
The effect of persulfate removal during preheating is shown in fig. 3. After the UV + PS + O3 system was reacted for 60min, the residual S2O 82-concentration was 0.25 g/L. The concentration of S2O 82-in the solution is gradually reduced and almost completely removed after heating at 80 ℃ for 8h by taking the initial heating time as the reaction zero point. Therefore, heating is an effective means for removing the residual PS, and the PS added in the evaporation crystallization process of the salt separation membrane concentrated wastewater can be further decomposed and activated. After evaporation and concentration, the purity of the obtained sodium sulfate salt reaches the A class first-class standard (whiteness is more than or equal to 82 percent and total organic carbon is less than or equal to 50mg/Kg) in coal chemical industry byproduct industrial sodium sulfate (T/CCT 001-2019).
Example 2
A resource treatment method of concentrated brine in a nanofiltration membrane salt separation process is applied to the treatment of the concentrated brine in the nanofiltration membrane salt separation of a wastewater treatment system of a certain coking plant, and the specific application method is as follows:
step 1: a UV + PS + O3 system is selected to treat actual wastewater for 2 hours under the conditions that the adding amount of persulfate is 2.0g/L, O3, the concentration is 50 mg/(L.min), the ultraviolet light intensity is 0.6 mu Einstein.s < -1 >, the pH value is 7.7 +/-0.1 and the temperature is 25 ℃.
Step 2: and heating the reacted wastewater to 80 ℃ for 8-10 h.
And step 3: and (4) evaporating and crystallizing the preheated strong brine through an evaporator to obtain sodium sulfate with the purity reaching the industrial salt recovery standard.
And (3) testing results:
the change trends of the PS concentration and the TOC concentration of the water sample after being processed are basically consistent. The PS concentration is reduced to 0.12g/L, the activation rate is 94.00 percent, the TOC concentration is reduced to 13.12mg/L, and the removal rate is 85.49 percent.
Three-dimensional fluorescence spectra and physical images before and after advanced oxidation treatment of wastewater are shown in FIGS. 4-7. The waste water is treated by a UV + PS + O3 system, the color change is large, and the waste water is light yellow. The three-dimensional fluorescence spectrum shows that the raw water mainly contains fulvic acid (area II) and humic acid (area III) organic matters, and the fluorescence intensity of the humic acid organic matters is greatly reduced after 2 hours of treatment, which indicates that most organic matters in the area are degraded; in the case of fulvic acid-type organic compounds (region ii), the fluorescence intensity is conversely increased, probably because the UV + PS + O3 system generates small molecule products during mineralization, and has strong fluorescence absorption at the very same place. After preheating and evaporation concentration, the purity of the obtained sodium sulfate salt reaches the A class first-class standard (whiteness is more than or equal to 82 percent and total organic carbon is less than or equal to 50mg/Kg) in coal chemical industry byproduct industrial sodium sulfate (T/CCT 001-2019).
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and the preferred embodiments of the present invention are described in the above embodiments and the description, and are not intended to limit the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. A resource treatment method of strong brine in a nanofiltration membrane salt separation process is characterized by comprising the following steps: comprises the following steps
S1: advanced oxidation, namely treating the strong brine generated by the separation of the nanofiltration membrane by adopting an advanced oxidation method to reduce the total organic carbon content of the strong brine;
s2: preheating, namely, removing the residual persulfate oxidant in the concentrated brine by preheating;
s2: and (4) evaporating and concentrating, namely evaporating and crystallizing preheated concentrated brine through an evaporator to obtain sodium sulfate with the purity reaching the industrial salt recovery standard.
2. The resource treatment method of the concentrated brine generated in the salt separation process of the nanofiltration membrane according to claim 1, which is characterized in that: the advanced oxidation method treatment process in the step 1 specifically comprises the steps of adding persulfate into concentrated brine generated in the salt separation process of the nanofiltration membrane, irradiating by ultraviolet light, introducing ozone, carrying out oxidation reaction under the condition of full stirring, sampling and detecting total organic carbon in reaction liquid until the content is lower than 15mg/L, and stopping the reaction.
3. The resource treatment method of the concentrated brine generated in the salt separation process of the nanofiltration membrane according to claim 2, which is characterized in that: the persulfate is specifically one or a mixture of sodium peroxymonosulfate and sodium peroxydisulfate.
4. The resource treatment method of the concentrated brine generated in the salt separation process of the nanofiltration membrane according to claim 3, which is characterized in that: the molar concentration ratio of the persulfate to the total organic carbon in the concentrated brine is 1: 1 to 20: 1.
5. the resource treatment method of the concentrated brine generated in the salt separation process of the nanofiltration membrane according to claim 1, which is characterized in that: the adding amount of the ozone is 10-100 mg/(L.min).
6. The recycling treatment method of the concentrated brine in the nanofiltration membrane salt separation process according to claim 2, characterized in that: in the advanced oxidation method, an ultraviolet lamp with the irradiation wavelength less than 300nm is adopted for ultraviolet irradiation, and the ultraviolet intensity of the ultraviolet lamp is more than 0.5 mu Einstein & s & lt-1 & gt.
7. The resource treatment method of the concentrated brine generated in the salt separation process of the nanofiltration membrane according to claim 1, which is characterized in that: and in the step 2, the preheating temperature is 80 ℃ at the lowest, the heat preservation is carried out for more than 30 minutes, and the residual oxidant is removed through thermal activation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202210289088.8A CN114590944A (en) | 2022-03-22 | 2022-03-22 | Resource treatment method for nanofiltration membrane brackish water |
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