CN115947493A - Fluorine chemical resin dispersion water treatment process - Google Patents
Fluorine chemical resin dispersion water treatment process Download PDFInfo
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- CN115947493A CN115947493A CN202310035971.9A CN202310035971A CN115947493A CN 115947493 A CN115947493 A CN 115947493A CN 202310035971 A CN202310035971 A CN 202310035971A CN 115947493 A CN115947493 A CN 115947493A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 145
- 238000011282 treatment Methods 0.000 title claims abstract description 104
- 239000006185 dispersion Substances 0.000 title claims abstract description 70
- 229920005989 resin Polymers 0.000 title claims abstract description 66
- 239000011347 resin Substances 0.000 title claims abstract description 66
- 239000000126 substance Substances 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 35
- 230000008569 process Effects 0.000 title claims abstract description 32
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 229910052731 fluorine Inorganic materials 0.000 title claims abstract description 17
- 239000011737 fluorine Substances 0.000 title claims abstract description 17
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 50
- 238000001914 filtration Methods 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 12
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical group OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 40
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 17
- 239000011790 ferrous sulphate Substances 0.000 claims description 17
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 17
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 17
- 238000005273 aeration Methods 0.000 claims description 16
- 238000003756 stirring Methods 0.000 claims description 9
- 239000012028 Fenton's reagent Substances 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 4
- 239000012528 membrane Substances 0.000 abstract description 39
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 17
- 238000011084 recovery Methods 0.000 abstract description 7
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 238000002474 experimental method Methods 0.000 description 16
- 230000000052 comparative effect Effects 0.000 description 15
- 230000004907 flux Effects 0.000 description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 12
- 238000012360 testing method Methods 0.000 description 11
- 230000000694 effects Effects 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 239000000084 colloidal system Substances 0.000 description 6
- 238000005189 flocculation Methods 0.000 description 6
- -1 polytetrafluoroethylene Polymers 0.000 description 6
- 239000004810 polytetrafluoroethylene Substances 0.000 description 6
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 230000016615 flocculation Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 229960004887 ferric hydroxide Drugs 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000007935 neutral effect Effects 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- 230000002411 adverse Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000003311 flocculating effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000004094 surface-active agent Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000001687 destabilization Effects 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000001953 sensory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a fluorine chemical resin dispersion water treatment process, belonging to the technical field of wastewater treatment; the method comprises the following steps: s1, sequentially performing Fenton treatment and filtration on chemical resin dispersion water to obtain a pretreatment solution; s2, carrying out ultrafiltration treatment on the pretreatment liquid to obtain ultrafiltrate; s3, performing RO treatment on the ultrafiltrate to obtain treated water; the chemical resin dispersion water treatment process comprises Fenton treatment, filtration, ultrafiltration treatment and RO membrane treatment, is simple in treatment process and low in cost, and can be widely applied to the chemical resin dispersion water treatment process, after the treatment process, the removal rate of SS in the chemical resin dispersion water is 100%, the content of ammonia nitrogen in the chemical resin dispersion water is controlled to be 10%, and the recovery rate of the dispersion water is more than or equal to 70%.
Description
Technical Field
The invention relates to the technical field of chemical wastewater treatment, in particular to a fluorine chemical resin dispersion water treatment process.
Background
In the fluorine industry, various fluororesin products are widely produced, such as polytetrafluoroethylene dispersion resin, polytetrafluoroethylene concentrated dispersion liquid, polytetrafluoroethylene suspension resin and the like, a large amount of resin dispersion water is generated in the production process, the resin dispersion water contains a large amount of SS (suspended solid concentration), however, the resin dispersion water is stable due to the surfactant and the like, and then colloidal substances and the like in the resin dispersion water are difficult to be fully precipitated and difficult to remove, and meanwhile, the ammonia nitrogen content of the resin dispersion water is extremely high, so that the resin dispersion water does not meet the receiving standard of a sewage treatment plant in a park, and therefore, the resin needs to be subjected to water diversion treatment before being conveyed to the sewage treatment plant.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a fluorine chemical resin dispersion water treatment process so as to at least achieve the aims of reducing SS and ammonia nitrogen concentration in resin dispersion water and improving the recovery rate.
The purpose of the invention is realized by the following technical scheme:
a fluorine chemical resin dispersion water treatment process comprises the following steps:
s1, sequentially performing Fenton treatment and filtration on chemical resin dispersion water to obtain a pretreatment solution;
s2, carrying out ultrafiltration treatment on the pretreatment liquid to obtain ultrafiltrate;
and S3, performing RO treatment on the ultrafiltrate to obtain treated water.
As some possible embodiments of the present application, in step S1, aeration stirring is used during the fenton treatment.
As some possible embodiments of the present application, in the step S1, the fenton reagent in the fenton treatment is hydrogen peroxide and ferrous sulfate, wherein a mass ratio of the hydrogen peroxide to the ferrous sulfate is 1 to 3:1.
As some possible embodiments of the present application, the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1:1.
As some possible embodiments of the present application, in the step S1, the filtration is performed by using a filter with a filter pore size of less than 100 micrometers.
As some possible embodiments of the present application, in the step S2, the pH of the feed water during the ultrafiltration treatment is 5.5 to 6.
As some possible embodiments of the present application, in the step S2, the pH of the feed water during the ultrafiltration treatment is 5.5.
As some possible embodiments of the present application, in the step S3, the pH of the feed water during RO treatment is 5.5 to 6.
As some possible embodiments of the present application, in the step S3, the pH of the feed water during RO treatment is 5.5.
The invention has the beneficial effects that:
the treatment process of the chemical resin dispersion water comprises Fenton treatment, filtration, ultrafiltration treatment and RO membrane treatment, is simple in treatment process and low in cost, and can be widely applied to the treatment process of the chemical resin dispersion water, after the treatment process, the removal rate of SS in the chemical resin dispersion water is 100%, the content of ammonia nitrogen in the chemical resin dispersion water is controlled to be 10mg/l, and meanwhile, the recovery rate of the dispersion water is more than or equal to 70%, and the treatment process meets the receiving standard of sewage treatment plants in gardens.
Detailed Description
The technical solutions in the embodiments of the present application will be described clearly and completely below, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
In the fluorine industry, various fluororesin products such as polytetrafluoroethylene dispersion resin, polytetrafluoroethylene concentrated dispersion, polytetrafluoroethylene suspension resin and the like are widely produced, a large amount of resin dispersion water is generated in the production process, the resin dispersion water contains a large amount of SS (suspended substance) and contains a surfactant and the like, so that the resin dispersion water is stable, glue substances and the like in the resin dispersion water are difficult to be fully precipitated and difficult to remove, the ammonia nitrogen content of the resin dispersion water is extremely high, and the resin dispersion water is not in accordance with the receiving standard of a sewage treatment plant in a park, so that the resin dispersion water needs to be treated before being conveyed to the sewage treatment plant.
Based on the above, the invention provides a fluorine chemical resin dispersion water treatment process, which comprises the following steps:
s1, sequentially performing Fenton treatment and filtration on chemical resin dispersion water to obtain a pretreatment solution;
s2, carrying out ultrafiltration treatment on the pretreatment liquid to obtain ultrafiltrate;
and S3, performing RO treatment on the ultrafiltrate to obtain treated water.
According to the scheme, a Fenton treatment mode is adopted firstly, the stability of the dispersed water is damaged to the greatest extent, then stable colloidal substances and the like in the dispersed water form a large amount of suspended substances, then the suspended substances, the colloidal substances and the like are removed in a filtering mode to obtain a pretreatment solution, the pretreatment solution is subjected to an aeration experiment, and the solution is still clear and transparent, so that the suspended substances and the colloidal substances in the dispersed water subjected to the Fenton treatment and the filtering treatment are few, and further SS in the dispersed water is removed to the greatest extent, and the adverse phenomena of membrane blockage and the like caused by the influence on the permeability of an ultrafiltration membrane during subsequent ultrafiltration treatment are avoided; then, the pretreatment solution is treated by an ultrafiltration membrane, so that impurities such as a few suspended matters and colloidal substances which are not removed in the step S1, as well as suspended matters and colloids which are generated by adding a medicament in the Fenton treatment process can be effectively removed, and the stable operation of a subsequent high-price RO membrane can be ensured; and finally, performing reverse osmosis treatment by an R0 membrane to reduce the content of ammonia nitrogen and the salt in water and completely remove SS. The SS of the resin dispersion water treated by the scheme is completely removed, the content of ammonia nitrogen is controlled to be about 10mg/l, the recovery rate of the dispersion water is more than or equal to 70 percent, and the resin dispersion water meets the receiving standard of sewage treatment plants in parks.
In order to further improve the removal efficiency of SS in the chemical resin dispersion water, as some possible embodiments of the present application, in the step S1, aeration stirring is adopted during the fenton treatment. In the fenton processing procedure, the stirring mode plays an important role in the destabilization degree of colloid in the dispersed water body, can effectively increase the dissolved oxygen content in water through adopting the aeration stirring mode, and then plays an oxidizing action with the fenton reagent in coordination, can increase the mixed effect of dispersed water and medicament simultaneously for the reaction rate.
In order to further improve the removal efficiency of SS in chemical resin dispersed water, as some possible embodiments of the present application, the fenton reagent and the amount of the reagent in the fenton treatment are limited, that is, in step S1, the fenton reagent in the fenton treatment is hydrogen peroxide and ferrous sulfate, wherein the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1-3:1.
in the fenton treatment, the cost and the effect need to be considered, the matching of the hydrogen peroxide and the ferrous sulfate is the most basic matching in the fenton reagent, however, in the fenton treatment, under the condition that the characteristics of the dispersed water are fixed, the quality relation of the hydrogen peroxide and the ferric sulfate is very important, if too much hydrogen peroxide is added, the waste of the oxidant is caused, substances such as tetrafluoroethylene resin and the like in the dispersed water also float, and if the ferrous sulfate is added excessively, the colloid is not easy to suspend, and even the color reversion phenomenon occurs. A large number of experiments show that the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1-3:1, the reaction efficiency is higher, and the SS removal efficiency is highest.
In order to further improve the removal efficiency of SS in chemical resin dispersed water and reduce the conductivity of the dispersed water, as some possible embodiments of the present application, the dosage ratio between Fenton reagents is defined, that is, the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1:1. In practical tests, the mass ratio of hydrogen peroxide to ferrous sulfate is 1-3:1, it can play a significant role in the aspect of SS removal, however, different mass ratios can lead to large differences in the electrical conductivity of the treated dispersed water, and if the electrical conductivity of the dispersed water is far greater than the value originally designed by the ultrafiltration membrane module system, the inlet water pressure of the ultrafiltration membrane equipment can be reduced, and further the water yield can be reduced. The invention limits the mass ratio of hydrogen peroxide to ferrous sulfate to be 1:1, the conductivity of the inlet water of the ultra-ultrafiltration membrane can be controlled to be about 5000us/cm so as to ensure the stable operation of the ultrafiltration membrane and improve the water yield, and if the mass ratio of the hydrogen peroxide to the ferrous sulfate is 3:1, the conductivity of the dispersed water after Fenton is about 8000us/cm, and the water yield is relatively reduced.
In order to further improve the removal efficiency of the SS in the chemical resin dispersed water, as some possible embodiments of the present application, the filter pore size during filtration is defined, that is, in the step S1, a filter with a filter pore size smaller than 100 micrometers is used for filtration. The aperture of the filter hole of the filter is limited, suspended matters in the filter can be removed to the maximum extent, and the SS removal rate is further improved.
In order to further improve the removal efficiency of SS in chemical resin dispersed water, as some possible embodiments of the present application, the pH of the feed water during the ultrafiltration treatment is defined, that is, in step S2, the pH of the feed water during the ultrafiltration treatment is 5.5 to 6. During the ultrafiltration treatment, if the pH is higher, part of flocculated impurities such as ferric hydroxide colloid still exist in the dispersed water, and during the ultrafiltration treatment, the flux of the ultrafiltration membrane is adversely affected, and even the membrane blockage phenomenon occurs. If the pH is too low, the hydrophobicity of the organic matter remaining in the dispersion increases, and the membrane is contaminated to some extent. By limiting the pH to 5.5 to 6, the fouling of the ultrafiltration membrane can be reduced and the flux of the ultrafiltration membrane can be ensured to be stable.
In order to further improve the removal efficiency of SS in the chemical resin dispersion water, as some possible embodiments of the present application, the pH of the feed water during the ultrafiltration treatment is defined, that is, in the step S2, the pH of the feed water during the ultrafiltration treatment is 5.5.
In order to further improve the removal efficiency of ammonia nitrogen in chemical resin dispersion water, as some possible embodiments of the present application, the influent water during RO treatment is defined, that is, in step S3, the pH of the influent water during RO treatment is 5.5 to 6. When the RO membrane is actually operated, the pH value of inlet water has great influence on the ammonia nitrogen in the produced water, and when the pH value of the inlet water is 5.5-6, the ammonia nitrogen content in the produced water is less than or equal to 25mg/l.
In order to further improve the removal efficiency of ammonia nitrogen in chemical resin dispersion water, as some possible embodiments of the present application, the influent water during RO treatment is defined, that is, in step S3, the influent water during RO treatment has a pH of 5.5. When the pH value of inlet water is 5.5, the content of ammonia nitrogen in produced water can be controlled to be about 10 mg/l.
The following will explain the treatment process of the resin dispersion water according to the present application in more detail with reference to the specific embodiments;
it is worth mentioning that: the raw materials in the examples are all commercial products;
example 1
S1, taking 2L of chemical resin dispersion water, adjusting the pH value to 3 by using dilute sulfuric acid, adding hydrogen peroxide with the mass of 1 per thousand of that of the dispersion water (the mass fraction of hydrogen peroxide is 30%) and ferrous sulfate with the mass of 1 per thousand of that of the dispersion water, stirring in an aeration stirring mode, adjusting the pH value of the dispersion water to be neutral after the reaction is finished, and filtering by using a bag filter with the aperture of 100 mu m to obtain a pretreatment solution;
s2, adjusting the pH value of the pretreatment liquid to 5.5 by using sulfuric acid, and then performing ultrafiltration treatment to obtain ultrafiltrate;
s3, adjusting the pH value of the ultrafiltrate to 5.5 by using sulfuric acid, and then performing RO treatment to obtain treated water.
Example 2
S1, taking 2L of chemical resin dispersion water, adjusting the pH value to 3 by using dilute sulfuric acid, adding hydrogen peroxide with the mass of 2 per thousand of that of the dispersion water (the mass fraction of hydrogen peroxide is 30%) and ferrous sulfate with the mass of 1 per thousand of that of the dispersion water, stirring in an aeration stirring mode, adjusting the pH value of the dispersion water to be neutral after the reaction is finished, and filtering by using a bag filter with the aperture of 100 mu m to obtain a pretreatment solution;
s2, adjusting the pH value of the pretreatment liquid to 5.5 by using sulfuric acid, and then performing ultrafiltration treatment to obtain ultrafiltrate;
s3, adjusting the pH value of the ultrafiltrate to 5.8 by using sulfuric acid, and then performing RO treatment to obtain treated water.
Comparative example 1
Compared with example 1, the pH was not adjusted before the step S2 of the pretreatment, and the rest of the steps and parameters were the same as those of example 1.
Comparative example 2
Compared with the embodiment 1, the step in the step S1 is changed, and the Fenton + filtration process is changed into an aeration and flocculation mode, and the specific steps are as follows:
s1, adding chemical resin dispersion water into a vat, adjusting the pH of raw water to be neutral, aerating for 1h, adding 5 per mill of PAC solution (flocculating), fully flocculating and filtering; and after filtration, continuing aeration and flocculation according to the previous mode, and after filtration, continuing aeration and flocculation, and filtering to obtain the pretreatment solution.
The rest of the steps and parameters were the same as in example 1.
Test examples
Experimental example 1 the effect of removing SS in step S1 in example 1 and comparative example 2 was compared.
In this test example, the chemical resin dispersion water used in example 1 and comparative example 1 was obtained from the same batch, and the index of the chemical resin dispersion water is shown in table 1.
TABLE 1 chemical resin Dispersion Water index
| Name of water sample | Resin dispersed water |
| pH (dimensionless) | 8.0 |
| SS(mg/l) | 67mg/L |
| Ammonia nitrogen | 447mg/L |
| Fluorine | 3.4mg/L |
| Electrical conductivity of | 3800us/cm |
| COD(mg/L) | 14mg/L |
| Sensory description | The raw water had floating substances and was white and turbid |
The pretreatment liquid in example 1 was taken out and found to be clear in water quality, and thereafter subjected to aeration treatment to find that no suspended matter was produced, thereby illustrating that fenton treatment can effectively treat suspended matter in resin-dispersed water; wherein, the conductivity of the pretreatment liquid in example 1 was only 5000us/cm.
The comparative example 2 generates white suspension in the three times of aeration and flocculation processes, and the pretreatment liquid in the comparative example 2 is taken and subjected to aeration treatment to find that suspended matters still exist, so that the aeration and flocculation mode cannot completely remove the white suspended matters in the water, and the remarkable effect which can be achieved by Fenton treatment is further embodied; wherein the conductivity of the pretreatment liquid in comparative example 2 was 4500us/cm, which is relatively close to that in example 1.
Experimental example 2 ultrafiltration membrane plugging in comparative example 1, comparative example 1 and comparative example 2
The parameters of the resin dispersion water used in this test example were the same as those in test example 1.
1. 5 sets of parallel tests were conducted in the same manner as in S1 of comparative example 2, and thereafter, the obtained 5 sets of pretreatment liquids were subjected to ultrafiltration treatment, the parameters of which are shown in Table 2.
Wherein 1-4 group is the continuous experiment, and 5 th group is for wasing the back experiment to look over the dirty stifled condition of ultrafiltration and wash the recovery effect, prevent that the experimental result from having the deviation, washed the ultrafiltration before the experiment.
TABLE 2
As can be seen from table 2: the yield of the ultrafiltration is in a descending state, which indicates that the water treated by the aeration and flocculation modes is easy to pollute and block the ultrafiltration membrane; in addition, the data of table 2 were analyzed as follows: (1) the first group of ultrafiltration membranes has lower flux, is related to lower temperature in the day and is also related to uncleanness of equipment; (2) the second group of ultrafiltration was normal flux at 18.6 ℃; (3) the ultrafiltration is backwashed before the third group begins, the membrane flux is slightly reduced, and the membrane flux is within an error range because the field timing and the water sample volume slightly deviate; (4) the ultrafiltration backwashing is not carried out before the fourth group begins, and the membrane flux is reduced to about 20%; (5) the fifth group is back washed and acid and alkali cleaned, and the flux is recovered, but is also obviously reduced.
2. 3 parallel tests were carried out in example 1 and 1 test in comparative example 1 according to the method of S1 in example 1, and then ultrafiltration treatment was carried out according to S2, the parameters of which are shown in Table 3, to examine the fouling of ultrafiltration after Fenton. Note: each set of tests was followed by only a water backwash, as engineering is also normal water production for about 1 hour and then a backwash for 3 minutes.
TABLE 3
As can be seen from table 3: there was not much change in membrane flux at the start and end of ultrafiltration in the 3 experiments in example 1 and the experiment in comparative example 1; all 3 experiments in example 1 increased, and the membrane flux in comparative example 1 slightly decreased; the reason why the 3 groups of experiments in example 1 are increased is that the temperature of the membrane equipment is gradually increased along with the prolonging of the membrane experiment time, the membrane flux is increased, and amphoteric colloids (ferric hydroxide and aluminum hydroxide) are difficult to exist under an acidic condition, so that the fouling of the membrane is less; the reason for the decrease of the membrane flux of comparative example 1 is that the pH was not adjusted, resulting in that some flocculated impurities (such as ferric hydroxide colloid) remained; as can be seen from table 2, the fenton oxidation treatment was performed before the ultrafiltration treatment, and the fouling did not substantially occur during the ultrafiltration treatment.
This experiment shows that: after the raw water is subjected to ultrafiltration and aeration treatment, more suspended matters still exist, and the ultrafiltration treatment is directly carried out by using the raw water, so that the ultrafiltration membrane is easy to generate dirt blockage; after the raw water is subjected to Fenton treatment, almost no suspended matters exist, and the raw water is subjected to ultrafiltration treatment, so that the condition of pollution and blockage basically does not exist, and the remarkable effect of the Fenton treatment on removal of SS is reflected.
Test example 3 demonstrates the effect of the present invention in treating dispersed water.
After the experimental examples 1 and 2 compare the processes of S1 and S2, the experimental example directly compares S3, and S3 is the last step of the scheme of the invention, and the parameters of the water produced in the step can be used for testing the feasibility and the superiority of the scheme of the invention.
4 experiments were conducted in the same manner as in example 1, and 1 experiment was conducted in the same manner as in example 2, wherein the resin dispersion water (i.e., raw water in Table 4) was varied in parameters in each experiment, and the specific parameters are shown in Table 4:
TABLE 4 comparison of relevant parameters for RO Membrane treatment
As can be seen from table 4: in the 4 groups of experiments in the example 1 and the RO membrane treatment process in the example 2, the flux of the RO membrane is not changed greatly, which shows that the RO membrane is polluted and blocked by the water after ultrafiltration; in example 1, the 4 th experiment was performed, and the membrane flux after cleaning was recovered to the highest value, indicating that the fouling was effectively removed. In addition, from 5 sets of experimental data in Table 3, it can be understood that the recovery rate of the dispersion water is not less than 76%. As the difference between the example 1 and the example 2 lies in the difference of the pH value of the feed water of the RO membrane, the ammonia nitrogen content in the produced water is 20.7mg/l when the pH value of the feed water is 5.8 as can be seen from the table 3; when the pH value of inlet water is stabilized at 5.5, the ammonia nitrogen produced in the water can be stabilized at about 10mg/l, so that the influence of the pH value on the ammonia nitrogen removal rate is reflected; furthermore, after the treatment by the process of the invention, SS in the dispersed water is zero, that is, SS is not detected, which indicates that the removal rate is 100%.
To sum up: according to the experimental examples 1-3, the process of Fenton, ultrafiltration and RO can be used for effectively treating the dispersed water, so that the ammonia nitrogen in the produced water is stabilized at 10mg/l, the SS removal rate is 100%, the customer requirements are met, meanwhile, the RO recovery rate is more than 70%, the flux of ultrafiltration and RO membranes is large, the design requirements are completely met, the fouling and blocking of the membranes are effectively controlled, and the long-term stable operation can be realized; meanwhile, the dosing cost is low, and engineering treatment can be performed.
The foregoing is illustrative of the preferred embodiments of this invention, and it is to be understood that the invention is not limited to the precise form disclosed herein and that various other combinations, modifications, and environments may be resorted to, falling within the scope of the concept as disclosed herein, either as described above or as apparent to those skilled in the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. A fluorine chemical resin dispersion water treatment process is characterized by comprising the following steps:
s1, sequentially performing Fenton treatment and filtration on chemical resin dispersion water to obtain a pretreatment solution;
s2, carrying out ultrafiltration treatment on the pretreatment liquid to obtain ultrafiltrate;
and S3, performing RO treatment on the ultrafiltrate to obtain treated water.
2. The fluorine chemical resin dispersion water treatment process according to claim 1, wherein in the step S1, aeration stirring is adopted in the Fenton treatment process.
3. The fluorine chemical resin dispersion water treatment process according to claim 1, wherein in the step S1, the fenton reagent in the fenton treatment is hydrogen peroxide and ferrous sulfate, wherein the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1-3:1.
4. the fluorine chemical resin dispersion water treatment process according to claim 3, wherein the mass ratio of the hydrogen peroxide to the ferrous sulfate is 1:1.
5. The process of claim 1, wherein in step S1, the filtration is performed by using a filter having filtration pores with a diameter of less than 100 μm.
6. The fluorine chemical resin dispersion water treatment process according to claim 1, wherein the pH of the feed water in the ultrafiltration treatment in step S2 is 5.5 to 6.
7. The fluorine chemical resin dispersion water treatment process according to claim 6, wherein the pH of the feed water in the ultrafiltration treatment in step S2 is 5.5.
8. The fluorine chemical resin dispersion water treatment process according to claim 1, wherein in the step S3, the pH of feed water in RO treatment is 5.5-6.
9. The process according to claim 1, wherein the feed water during RO treatment in step S3 has a pH of 5.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310035971.9A CN115947493A (en) | 2023-01-10 | 2023-01-10 | Fluorine chemical resin dispersion water treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202310035971.9A CN115947493A (en) | 2023-01-10 | 2023-01-10 | Fluorine chemical resin dispersion water treatment process |
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| CN118598441A (en) * | 2024-08-07 | 2024-09-06 | 杭州水处理技术研究开发中心有限公司 | Coagulation wastewater recycling treatment system and method |
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