CN114538653A - Industrial wastewater treatment method - Google Patents
Industrial wastewater treatment method Download PDFInfo
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- CN114538653A CN114538653A CN202210145599.2A CN202210145599A CN114538653A CN 114538653 A CN114538653 A CN 114538653A CN 202210145599 A CN202210145599 A CN 202210145599A CN 114538653 A CN114538653 A CN 114538653A
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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
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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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
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Engineering & Computer Science (AREA)
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- Water Supply & Treatment (AREA)
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- Organic Chemistry (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The application discloses an industrial wastewater treatment method, which comprises the following steps: s1, preprocessing; s2, feeding water into the adsorption tank I, and adsorbing organic matters through resin; s3, stopping water inflow after the first adsorption tank reaches the working exchange capacity, allowing the second adsorption tank to inflow water and adsorb, allowing the resin in the first adsorption tank to enter a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank; s4, transferring the resin in the desorption tank to a first adsorption tank through a resin transfer pipe after the resin desorption is finished; s5, stopping water inflow after the second adsorption tank reaches the working exchange capacity, allowing the first adsorption tank to inflow water and adsorb, allowing the resin in the second adsorption tank to enter a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank; s6, transferring the resin in the desorption tank to a second adsorption tank through a resin transfer pipe after the resin desorption is finished; s7, repeating the steps S2-S6. According to the technical scheme, the process of adsorption and desorption in the resin tank in the prior art is improved into the process of 'in-vivo adsorption + in-vitro desorption', and the desorption effect of the polluted resin is obviously improved.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to an industrial wastewater treatment method.
Background
Industrial wastewater, particularly phenol-cyanogen wastewater, can meet the discharge standard after being treated, the conventional treatment mode of phenol-cyanogen wastewater needs biochemical treatment, advanced treatment and salt separation treatment, and when the phenol-cyanogen wastewater after the biochemical treatment is subjected to the advanced treatment, organic matters accumulated during the membrane filtration step can block filtration holes in the membrane due to the organic matters, so that the service life of the membrane is seriously influenced. The prior art discloses that an organic matter adsorption device is used for treating wastewater to reduce the content of organic matters in the wastewater, but in the conventional adsorption device and method, when a medium with weak adsorption is adopted for adsorption, the desorption effect is good but the adsorption effect is poor, and when a medium with strong adsorption is adopted for adsorption, the desorption effect is insufficient, so that the cost is overhigh. For example, in the existing adsorption mode, a resin tower is used for organic matter adsorption, and after the resin is adsorbed for a certain time, in-situ desorption needs to be performed in the resin tower to recover the adsorption capacity of the resin, but the desorption device is limited by the structural characteristics of the adsorption tower, and when the desorption device is arranged in the adsorption tower, the desorption effect is unsatisfactory, and the desorption device needs to be matched with the adsorption device, so that the cost is high.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides an industrial wastewater treatment method.
The industrial waste water treating process includes three parallelly connected adsorption tanks, three desorption tanks connected via resin transferring pipes, and three standby adsorption tanks, including the following steps:
s1, preprocessing;
s2, feeding water into the adsorption tank I, and adsorbing organic matters through resin;
s3, stopping water inflow after the first adsorption tank reaches the working exchange capacity, allowing the second adsorption tank to inflow water and adsorb, allowing the resin in the first adsorption tank to enter a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank;
s4, transferring the resin in the desorption tank to a first adsorption tank through a resin transfer pipe after the resin desorption is finished;
s5, stopping water inflow after the second adsorption tank reaches the working exchange capacity, allowing the first adsorption tank to inflow water and adsorb, allowing the resin in the second adsorption tank to enter a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank;
s6, transferring the resin in the desorption tank to a second adsorption tank through a resin transfer pipe after the resin desorption is finished;
s7, repeating the steps S2-S6.
Further, in steps S3 and S5, after the water inflow is stopped, the resin in the adsorption tank is aerated and backwashed.
Further, the desorbing comprises: s100, acid cleaning, S200, saline-alkali + organic cleaning solution cleaning, S300, saline-alkali cleaning, and S400, acid cleaning.
Further, the first acid cleaning is as follows: adopting (2-8) wt% hydrochloric acid 1.5-3BV, temperature 52-58 deg.C, cleaning in two steps, half amount of each step, soaking in the first step for not less than 1 hr, stirring with compressed air, and washing with deionized water.
Further, the saline-alkali + organic cleaning solution is: (2-5) NaOH (8-12) NaCl (20-30) and organic cleaning solution 0.5BV, the temperature is 52-58 ℃, the soaking time is 2 hours, and then the washing is carried out by deionized water.
Further, the organic cleaning solution is organic acid, organic alcohol or a combination thereof.
Further, the organic acid is oxalic acid, acetic acid or citric acid or a combination thereof; the organic alcohol is methanol or isopropanol or a combination thereof.
Further, saline-alkali cleaning comprises the following steps: (2-5) NaOH + (8-12) NaCl solution 2-4BV, the temperature is 52-58 ℃, the cleaning is carried out in three steps, the using amount of one sixth of the first two steps is one, the soaking time in the first step is not less than 2 hours, and then the cleaning is carried out by deionized water and the cleaning is carried out; in the second step, the soaking time is not less than 2 hours, the stirring is carried out by compressed air in the soaking process, and after the soaking is finished, the washing is carried out by deionized water and the water is drained; and thirdly, using two thirds of the dosage, and then washing with deionized water.
Further, acid cleaning is as follows: (2-3) 0.5-1.5BV of hydrochloric acid, normal temperature, and finally washing with deionized water.
Further, the elution waste liquid is treated by adopting a wet oxidation process, wherein the wet oxidation process comprises the following steps: adjusting pH of the elution waste liquid to 2-4 with sulfuric acid, adding hydrogen peroxide according to the concentration of 2-5%, and mixing uniformly; heating the reaction tower to 145-150 ℃ by using steam, and then sending the prepared stock solution into the reaction tower, wherein the effective retention time of the stock solution in the reaction tower is 1.5-2 h.
Specifically, compared with the prior art, the invention has the advantages that: according to the technical scheme, the process of adsorption and desorption in the resin tank in the prior art is improved into the process of 'in-vivo adsorption + in-vitro desorption', and the desorption effect of the polluted resin is obviously improved. Specifically, the method comprises the following steps:
1. through improving resin adsorption tank and desorption jar, be connected adsorption tank and desorption jar, adsorption tank sets up a plurality ofly, and the quantity of desorption jar reduces for prior art by a wide margin, carries out the air entrainment backwash before the resin is carried to desorption jar, can make the resin fluffy, more is favorable to carrying.
2. The desorption process is more thorough outside the jar, and the desorption is higher in the adsorption tank is compared to the operatable degree, through increasing the compressed air stirring, is showing and is improving desorption efficiency.
3. The desorption solution for desorbing the resin adsorbing the organic matters is improved, the composition ratio of the desorption solution is continuously tried to be adjusted, the desorption effect is optimal, the organic cleaning solution is added in a breakthrough manner on the basis of the existing saline-alkali desorption solution, the unexpected excellent desorption effect is obtained, and the better content ratio of the organic cleaning solution is continuously tried to be determined.
4. The desorption process is further optimized and improved, the dosage and the soaking time of each step in the desorption process are optimized, and the process parameter combination with excellent desorption effect is obtained.
5. The desorption waste liquid is treated by adopting a wet catalytic oxidation process, the removal rate of organic matters in the desorption waste liquid reaches over 80 percent and can reach 92 percent at most, the organic matters can be efficiently removed, and the method provides powerful guarantee for zero discharge of industrial waste water.
Drawings
FIG. 1 is a schematic structural diagram of the present invention
Reference numerals:
1. adsorption tanks one, 2, two, 3, three, 4, desorption tanks, 5, eluent processing apparatus, 6, deionized water tank, 7, acid desorption liquid tank, 8, saline-alkali desorption liquid tank
Detailed Description
The treatment device and the treatment method mainly aim at phenol-cyanogen wastewater, and the phenol-cyanogen wastewater comprises effluent of a biochemical treatment system, concentrated brine from a desalted water station, and salt solution obtained after wet acid preparation and neutralization of coke oven gas desulfurization waste liquid (2% dilute sulfuric acid is neutralized by NaOH), but the treatment device and the treatment method are not limited to the ranges. The percentages referred to in the present invention are mass percentages.
A method for treating industrial wastewater is disclosed, as shown in figure 1, the adopted device comprises three adsorption tanks (an adsorption tank I1, an adsorption tank II 2 and an adsorption tank III 3) which are connected in parallel, and desorption tanks 4 which are connected with the three adsorption tanks through resin transfer pipes, wherein two of the three adsorption tanks work alternately, the third is reserved, the desorption tanks 4 are connected with an eluent treatment device 5, a deionized water tank 6, an acid desorption liquid tank 7 and a saline-alkali desorption liquid tank 8, wherein (2-8) wt% of HCl is contained in the acid desorption liquid tank, and (2-5) wt% of NaOH + (8-12) wt% of NaCl solution and (2-5) wt% of NaOH + (8-12) wt% of NaCl + (20-30) wt% of organic cleaning solution are contained in the saline-alkali desorption liquid tank; the processing method comprises the following steps:
s1, preprocessing; may include chemical pre-softening, filtering, resin re-softening;
s2, feeding water into the adsorption tank I1, and adsorbing organic matters through resin;
s3, stopping water inflow after the first adsorption tank 1 reaches the working exchange capacity, allowing the second adsorption tank 2 to inflow water and adsorb, transferring the resin in the first adsorption tank 1 to the desorption tank 4 through a resin transfer pipe, and desorbing the resin in the desorption tank 4;
s4, transferring the resin in the desorption tank 4 to the first adsorption tank 1 through a resin transfer pipe after the resin desorption is finished;
s5, stopping water inflow after the second adsorption tank 2 reaches the working exchange capacity, allowing the first adsorption tank 1 to inflow and adsorb, transferring the resin in the second adsorption tank 2 to the desorption tank 4 through a resin transfer pipe, and desorbing the resin in the desorption tank 4;
s6, transferring the resin in the desorption tank to a second adsorption tank 2 through a resin transfer pipe after the resin desorption is finished;
s7, repeating the steps S2-S6.
Alternatively, in steps S3 and S5, after the water supply is stopped, the resin in the adsorption tank is aerated and backwashed.
Optionally, the desorbing comprises: s100, acid cleaning, S200, saline-alkali + organic cleaning solution cleaning, S300, saline-alkali cleaning, and S400, acid cleaning. Each desorption step adopts a liquid feeding mode of countercurrent.
Wherein, the first acid cleaning is as follows: adopting (2-8) wt% hydrochloric acid 1.5-3BV at 52-58 deg.C, cleaning in two steps, half the amount of each step, soaking in the first step for not less than 1 hr, stirring with compressed air, and washing with deionized water;
the saline-alkali + organic cleaning solution is as follows: (2-5) NaOH (8-12) NaCl (20-30) and organic cleaning solution (0.5-1 BV) in weight percent, the temperature is 52-58 ℃, the soaking is carried out for 2 hours, and then the washing is carried out by deionized water;
in an alternative embodiment, the organic cleaning solution is an organic acid, an organic alcohol, or a combination thereof.
Optionally, the organic acid is oxalic acid, acetic acid or citric acid; the organic alcohol is methanol or isopropanol.
The saline-alkali cleaning is as follows: 2-4BV of (2-5)% NaOH + (8-12)% NaCl solution at 52-58 deg.C, three-step cleaning, one sixth of the first step, soaking for no less than 2 hr, washing with deionized water, and draining; in the second step, the soaking time is not less than 2 hours, the stirring is carried out by compressed air in the soaking process, and after the soaking is finished, the washing is carried out by deionized water and the water is drained; and thirdly, using two thirds of the dosage, and then washing with deionized water.
The second acid cleaning step is as follows: (2-3) 0.5-1.5BV of hydrochloric acid, normal temperature, and finally washing with deionized water.
Specifically, the desorption can be carried out using the specific steps in table 1.
TABLE 1
Along with the extension of operating time, conventional jar interior desorption mode is after through the manifold cycles, the adsorption performance of resin can fall to below 80% of initial adsorption performance usually, jar interior desorption is difficult to promote the adsorption performance of resin again, the desorption degree that adopts the desorption method in this application can show improvement resin, adopt the concrete step in table 1 to carry out the desorption back, the adsorption performance of resin can be recovered to more than 90% by below 80% of original adsorption performance, the desorption effect obviously promotes, thereby can reduce the use cost of resin by a wide margin.
Optionally, the elution waste liquid is treated by a wet oxidation process, wherein the wet oxidation process comprises the following steps: adjusting pH of the elution waste liquid to 2-4 with sulfuric acid, adding hydrogen peroxide according to the concentration of 2-5%, and mixing uniformly; heating the reaction tower to 145-150 ℃ by using steam, and then sending the prepared stock solution into the reaction tower, wherein the effective retention time of the stock solution in the reaction tower is 1.5-2 h.
The results of the elution waste liquid after the wet oxidation process are shown in table 2. As can be seen from Table 2, the removal rate of the elution waste liquid is more than 80%, and the maximum removal rate can reach 92%, so that the organic matters in the elution waste liquid can be efficiently removed, and the standard discharge of the waste liquid is realized.
TABLE 2
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention. Furthermore, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In the description of the present invention, reference to the description of the terms "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
While embodiments of the invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.
Claims (10)
1. The industrial wastewater treatment method is characterized in that the adopted device comprises three adsorption tanks connected in parallel and a desorption tank connected with the three adsorption tanks through resin transfer pipes, two of the three adsorption tanks work alternately, and the third adsorption tank is standby, and the treatment method comprises the following steps:
s1, preprocessing;
s2, feeding water into the adsorption tank I, and adsorbing organic matters through resin;
s3, stopping water inflow after the first adsorption tank reaches the working exchange capacity, allowing the second adsorption tank to inflow water and adsorb, transferring the resin in the first adsorption tank to a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank;
s4, after the resin in the desorption tank is desorbed, the resin enters the first adsorption tank through a resin transfer pipe;
s5, stopping water inflow after the second adsorption tank reaches the working exchange capacity, allowing the first adsorption tank to inflow water and adsorb the water, transferring the resin in the second adsorption tank to a desorption tank through a resin transfer pipe, and desorbing the resin in the desorption tank;
s6, repeating the steps S2-S5.
2. The method of claim 1, wherein in steps S3 and S5, after the water feed is stopped, the resin in the adsorption tank is aerated and backwashed.
3. The method of claim 1, wherein the desorbing comprises: s100, acid cleaning, S200, saline-alkali + organic cleaning solution cleaning, S300, saline-alkali cleaning, and S400, acid cleaning.
4. The method of claim 1, wherein the first acid wash is: adopting (2-8) wt% hydrochloric acid 1.5-3BV, temperature 52-58 deg.C, cleaning in two steps, half amount of each step, soaking in the first step for not less than 1 hr, stirring with compressed air, and washing with deionized water.
5. The method as claimed in claim 1, wherein the saline alkali + organic cleaning solution is: (2-5) NaOH (8-12) NaCl (20-30) and organic cleaning solution 0.5BV, the temperature is 52-58 ℃, the soaking time is 2 hours, and then the washing is carried out by deionized water.
6. The method of claim 5, wherein the organic cleaning solution is an organic acid, an organic alcohol, or a combination thereof.
7. The method of claim 6, wherein the organic acid is oxalic acid, acetic acid, or citric acid; the organic alcohol is methanol or isopropanol.
8. The method according to claim 1, characterized in that the saline-alkali cleaning is: (2-5) 2-4BV of NaOH + (8-12) wt% NaCl solution at 52-58 ℃, cleaning in three steps, wherein the soaking time in the first step is not less than 2 hours, then washing with deionized water and draining; in the second step, the soaking time is not less than 2 hours, the stirring is carried out by compressed air in the soaking process, and after the soaking is finished, the washing is carried out by deionized water and the water is drained; and thirdly, using two thirds of the dosage, and then washing with deionized water.
9. The method of claim 1, wherein acid wash two is: (2-3) 0.5-1.5BV of hydrochloric acid, normal temperature, and finally washing with deionized water.
10. The method according to claim 1, wherein the elution waste liquid is treated by a wet oxidation process, wherein the wet oxidation process comprises: adjusting pH of the elution waste liquid to 2-4 with sulfuric acid, adding hydrogen peroxide according to the concentration of 2-5%, and mixing uniformly; heating the reaction tower to 145-150 ℃ by using steam, and then sending the prepared stock solution into the reaction tower, wherein the effective retention time of the stock solution in the reaction tower is 1.5-2 h.
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| CN115180750A (en) * | 2022-09-08 | 2022-10-14 | 精华制药集团南通有限公司 | Pharmaceutical industry wastewater purification device and use method thereof |
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| CN114538653B (en) | 2023-04-07 |
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