CN114620852A - Treatment method of wastewater from process for producing rubber vulcanization accelerator CBS by oxidation method - Google Patents
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Abstract
The invention provides a method for treating wastewater from a process for producing a rubber vulcanization accelerator CBS by an oxidation method. The processing method comprises the following steps: step S1, adjusting the pH value of the process wastewater to 5-7, and then sequentially performing flocculation treatment and solid-liquid separation to obtain clear liquid and flocculate; step S2, carrying out adsorption treatment on the clear liquid to obtain adsorbed wastewater; and step S3, filtering the waste water after adsorption to obtain reusable water and concentrated water, wherein the filtering is microfiltration, ultrafiltration or nanofiltration. By applying the technical scheme of the invention, most of flocculate, macromolecular organic matters, colloid and micromolecular organic matters in the wastewater of the oxidation CBS process are effectively removed. The method is easy to implement, and the treatment of each step realizes the synergistic effect, so that the high-efficiency treatment of the wastewater of the oxidation CBS process is realized.
Description
Technical Field
The invention relates to the technical field of treatment of wastewater from a production process of a rubber vulcanization accelerator CBS, in particular to a treatment method of wastewater from a production process of the rubber vulcanization accelerator CBS by an oxidation method.
Background
The synthesis method of the rubber vulcanization accelerator CBS is usually a sodium hypochlorite method, a hydrogen peroxide method and an oxygen oxidation method, and the reaction conditions and environments of different processes are different, so that the composition difference of the generated waste water is large. The existing wastewater treatment technology for synthesizing the rubber vulcanization accelerator CBS mainly aims at wastewater obtained by a sodium hypochlorite CBS process, and the treatment scheme mainly centers on COD removal and brine separation. There is little mature technology for CBS processes synthesized by the hydrogen peroxide method and the oxygen oxidation method.
Meanwhile, the conventional sodium hypochlorite process wastewater treatment has the characteristics of high cost, long route, complex flow and high energy consumption. The main flow technology is sedimentation, clear liquid flocculation treatment and multi-effect evaporation desalination after carbon adsorption, and the technology is not suitable for the process wastewater for preparing CBS by the prior hydrogen peroxide method and the process wastewater for preparing CBS by the oxygen oxidation method.
Disclosure of Invention
The invention mainly aims to provide a method for treating wastewater from a process for producing a rubber vulcanization accelerator CBS by an oxidation method, so as to solve the problem that the wastewater from the process for producing the rubber vulcanization accelerator CBS by the oxidation method in the prior art is difficult to effectively treat.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for treating wastewater from a process for producing a rubber vulcanization accelerator CBS by an oxidation method, the method comprising: step S1, adjusting the pH value of the process wastewater to 5-7, and then sequentially performing flocculation treatment and solid-liquid separation to obtain clear liquid and flocculate; step S2, carrying out adsorption treatment on the clear liquid to obtain adsorbed wastewater; and step S3, filtering the waste water after adsorption to obtain reusable water and concentrated water, wherein the filtering is microfiltration, ultrafiltration or nanofiltration.
Further, in the step S1, the flocculating agent is used for flocculation, preferably, the flocculating agent includes an inorganic flocculating agent and an organic flocculating agent, preferably, the inorganic flocculating agent is selected from one or more of polyaluminum chloride, polyferric sulfate, polyferric silicate, polyaluminum chloride, polyferric chloride, polysilicic acid, polyaluminum ferric silicate, polyferric sulfate, polyaluminum chloride, polyaluminum sulfate, polyaluminum phosphate, polyaluminum chloride, polyferric phosphate, polyferric silicate, polyaluminum phosphate, silicon calcium composite polyferric chloride and biological polyferric, and the organic flocculating agent is polyacrylamide flocculating agent.
Further, the polyacrylamide flocculant is any one of an anionic polyacrylamide flocculant, a nonionic polyacrylamide flocculant, a zwitterionic polyacrylamide flocculant and a cationic polyacrylamide flocculant, the polymerization degree of the nonionic polyacrylamide flocculant, the anionic polyacrylamide flocculant and the zwitterionic polyacrylamide flocculant is preferably 500-2500 ten thousand, and the ion degree of the cationic polyacrylamide flocculant is preferably 20-80%.
Further, the processing method is a batch processing method, and step S1 includes: mixing the process wastewater with the pH value of 5-7 with an inorganic flocculant for primary flocculation to obtain a first mixed system, wherein the inorganic flocculant is calculated by an aqueous solution with the mass content of 2%, and the preferred dosage of the inorganic flocculant is 0.5-50 per mill of the mass of the process wastewater; mixing the first mixed system with an organic flocculant for secondary flocculation to obtain a second mixed system, wherein the organic flocculant is calculated by emulsion with the mass content of 1 per mill, and the preferred dosage of the organic flocculant is 0.5-30 per mill of the mass of the process wastewater; and carrying out solid-liquid separation on the second mixed system to obtain clear liquid and flocculate.
Further, the processing method is a continuous processing method, and step S1 includes: continuously feeding the process wastewater with the pH value of 5-7 into a first flocculation tank, and continuously adding an inorganic flocculant into the first flocculation tank for primary flocculation treatment to obtain a first mixing system, wherein the inorganic flocculant is calculated by an aqueous solution with the mass content of 5%, and the preferred dosage of the inorganic flocculant is 0.5-50 per mill of the mass of the process wastewater; continuously overflowing the first mixed system into a second flocculation tank, and adding an organic flocculant into the second flocculation tank for secondary flocculation treatment when the volume of the first mixed system is half of that of the second flocculation tank to obtain a second mixed system; the organic flocculant is calculated by emulsion with the mass content of 1 per mill, and the dosage of the organic flocculant is 0.5-30 per mill of the mass of the process wastewater; and continuously carrying out solid-liquid separation on the overflowed second mixed system to obtain clear liquid and flocculate.
Further, stirring is carried out in the flocculation treatment process in the step S1, wherein the stirring speed is 80-120 r/min.
Further, in the step S1, the solid-liquid separation is performed by sedimentation or filtration.
Further, in step S2, an adsorption treatment is performed using activated carbon.
Further, the particle size of the above charcoal is 2 to 10mm, and the iodine value is 700 to 1500.
Further, the treatment method also comprises the step of returning the concentrated water to the step S1 to carry out flocculation treatment together with the process wastewater.
By applying the technical scheme of the invention, a solution is provided for the separation pertinence of flocs, macromolecular organic matters, colloids and micromolecular organic matters in the wastewater of the oxidation CBS process. Flocculating flocculate, macromolecular organic matter and colloid, separating flocculated flocculate by solid-liquid separation to eliminate most of macromolecular matter, adsorbing to eliminate small molecular organic matter, microfiltering, ultrafiltering or nanofiltering to purify the adsorbed waste water, and using the clear liquid as reuse water. Not only is easy to implement, but also realizes the synergistic effect of the treatment of each step, thereby realizing the high-efficiency treatment of the wastewater of the oxidation CBS process.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
As analyzed by the background art of the present application, the CBS wastewater treatment process in the prior art mainly aims at the wastewater of the hyponathic CBS process, and because the wastewater of the processes for preparing CBS by the hyponathic process and preparing CBS by the oxidation process have a large difference in composition, the wastewater treatment method in the prior art is not applicable to the wastewater of the processes for preparing CBS by the oxidation process, and therefore, finding a method capable of effectively treating the wastewater of the processes for preparing CBS by the oxidation process becomes an urgent problem to be solved.
The application discloses a treatment method of wastewater from CBS process for producing rubber vulcanization accelerator by oxidation, which comprises the following steps: step S1, adjusting the pH value of the process wastewater to 5-7, and then sequentially carrying out flocculation and solid-liquid separation to obtain clear liquid and flocculate; step S2, carrying out adsorption treatment on the clear liquid to obtain adsorbed wastewater; and step S3, filtering the waste water after adsorption to obtain reusable water and concentrated water, wherein the filtering is microfiltration, ultrafiltration or nanofiltration.
The treatment method provides a solution for separating floccules, macromolecular organic matters, colloids and micromolecular organic matters in the wastewater of the oxidation CBS process. Flocculating flocculated materials, macromolecular organic matters and colloids through flocculation treatment, separating flocculated materials through solid-liquid separation to remove most of macromolecular substances, further performing adsorption treatment to remove small molecular organic matters, and finally performing further purification treatment on the adsorbed wastewater through microfiltration, ultrafiltration or nanofiltration, wherein the obtained clear liquid can be used as reuse water. The method is easy to implement, and the treatment of each step realizes the synergistic effect, thereby realizing the high-efficiency treatment of the wastewater of the oxidation CBS process.
Preferably, the pH adjustment is performed using a conventional acid or base, and in order to avoid the introduction of ions that are difficult to remove during the pH adjustment, one or more of hydrochloric acid, sulfuric acid, sulfurous acid, phosphoric acid, calcium hydroxide, magnesium hydroxide, and sodium hydroxide are preferably used.
Preferably, the step S1 is performed with a flocculating agent, the flocculating agent preferably includes an inorganic flocculating agent and an organic flocculating agent, the inorganic flocculating agent is selected from one or more of polyaluminum chloride (PAC), polyferric sulfate (PFS), Polyaluminum Silicate (PSF), polyaluminum silicate chloride (PASC), polyaluminum chloride (PFC), polysilicic acid (PS), polyaluminum ferric silicate (PSAF), polyaluminum ferric sulfate chloride (PAFCS), polyaluminum ferric chloride (PAFC), polyaluminum sulfate (PAS), polyaluminum phosphate (PAP), Polyaluminum Ferric Chloride (PFC), polyaluminum phosphate (PFP), polyaluminum silicate (PFSs), polyaluminum silicate sulfate (PFSC), Polyaluminum Ferric Chloride (PFCs), polyaluminum silicate (PASI), polyaluminum ferric phosphate (fp), calcium silicate composite polyaluminum ferric chloride (SCPAFC) and Biological Polyferric (BPFC), the organic flocculant is a polyacrylamide flocculant. The inorganic flocculant is utilized to adsorb particulate matters, colloids, macromolecular compounds and substances with characteristic groups such as sulfydryl, sulfonic acid groups and the like in the wastewater to achieve the enrichment and condensation effect, and then the organic flocculant is utilized to adhere small particles formed by the inorganic flocculant to form large particle settlement, so that the flocculation of macromolecular organic matters and colloids is realized as far as possible, and the removal efficiency of the macromolecular organic matters and the colloids is improved.
In order to better exert the flocculation and sedimentation effects of the organic flocculant, the polyacrylamide flocculant is preferably any one of an anionic polyacrylamide flocculant, a nonionic polyacrylamide flocculant, a zwitterionic polyacrylamide flocculant and a cationic polyacrylamide flocculant, the polymerization degree of the polyacrylamide flocculant is preferably 500-2500 ten thousand, and the ion degree is preferably 20-80%.
In one embodiment, the processing method is a batch processing method, and the step S1 includes: mixing the process wastewater with the pH value of 5-7 with an inorganic flocculant for primary flocculation to obtain a first mixed system, wherein the inorganic flocculant is calculated by a water solution with the mass content of 2%, and the preferred dosage of the inorganic flocculant is 5-50 per mill of the mass of the process wastewater; mixing the first mixed system with an organic flocculant for secondary flocculation to obtain a second mixed system, wherein the organic flocculant is calculated by emulsion with the mass content of 1 per mill, and the preferred dosage of the organic flocculant is 1-30 per mill of the mass of the process wastewater; and carrying out solid-liquid separation on the second mixed system to obtain clear liquid and flocculate. The process wastewater is treated in batches by intermittent treatment, which is beneficial to targeted treatment according to the pollutant content of each batch of wastewater and improves the treatment effect of pollutants in the wastewater. In the treatment process, the added flocculating agent is adjusted in the range aiming at the treated object, so that the high-efficiency removal of macromolecular organic matters and colloids in the wastewater is realized, and the consumption of the flocculating agent is saved.
In another embodiment, the processing method is a continuous processing method, and step S1 includes: continuously feeding the process wastewater with the pH value of 5-7 into a first flocculation tank, and continuously adding an inorganic flocculant into the first flocculation tank for primary flocculation treatment to obtain a first mixing system, wherein the inorganic flocculant is calculated by an aqueous solution with the mass content of 5%, and the preferred dosage of the inorganic flocculant is 0.5-50 per mill of the mass of the process wastewater; continuously overflowing the first mixed system into a second flocculation tank, and adding an organic flocculant into the second flocculation tank for secondary flocculation treatment when the volume of the first mixed system is half of that of the second flocculation tank to obtain a second mixed system; the organic flocculant is calculated by emulsion with the mass content of 1 per mill, and the dosage of the organic flocculant is 0.5-30 per mill of the mass of the process wastewater; and continuously carrying out solid-liquid separation on the overflowed second mixed system to obtain clear liquid and flocculate.
The continuous process is adopted to treat the process wastewater, so that the operation mode is simplified, the treatment efficiency is improved, the respective effects are fully exerted through the use amount and the adding time of the decolorizer and the flocculant, and the reagent cost is saved.
The skilled person can select the appropriate dosage within the above range according to the effect of different flocculants to avoid adding too much flocculant to cause waste of reagents and increase of solid waste. Moreover, the flocculant selected by the application has the advantages that the addition of a small amount of flocculant can enable the treated process wastewater to reach the discharge standard, on one hand, new waste solids cannot be added into the industrial wastewater, and on the other hand, the cost is greatly reduced.
In order to improve the flocculation efficiency, stirring is carried out in the flocculation treatment process in the step S1, and the stirring speed is 80-120 r/min.
In the prior art, there are various solid-liquid separation methods, and in order to adapt to the system to be treated of the present application and improve the solid-liquid separation efficiency, the solid-liquid separation in step S1 is sedimentation or filtration.
In one embodiment, the step S2 is performed by using activated carbon. This application utilizes the high adsorptivity of active carbon to carry out adsorption treatment to the clear solution that solid-liquid separation obtained to adsorb micromolecular organic matter wherein, for the adsorption efficiency who improves active carbon, the particle diameter of active carbon is 2 ~ 10, and the specific surface area of active carbon is 700 ~ 1500.
The filtering process of the above step S3 may be any one of microfiltration, ultrafiltration and nanofiltration, and is preferably nanofiltration to improve the removal rate of contaminants. After the filtration treatment, the treatment method preferably further comprises returning the concentrated water to the step S1 to be flocculated together with the process wastewater so as to avoid waste residue discharge.
The following examples are provided to further illustrate the benefits of the present application.
Example 1
5000g of CBS wastewater (COD 18000-. 75g of PAC solution with the mass concentration of 2 percent is added in sequence under the stirring state with the speed of 120r/min, the mass concentration is 1 per mill, the ionicity is 60 percent of cationic PAM 30g, after the flocs are settled, the supernatant is taken and pumped into an activated carbon adsorption column (the particle size of the activated carbon is 5mm, the iodine value is 800, and the retention time is 4 hours) by a metering pump. After the treatment, the COD of the wastewater can be reduced to about 3000, and the color is colorless and transparent. After the absorption, the waste water is filtered by a nanofiltration membrane, and about 4000g of clean water is obtained by recovery (the recovery rate is more than or equal to 80 percent, and the COD is less than 50 percent). And carrying out flocculation treatment on the concentrated water obtained by nanofiltration again, and discharging the concentrated water after the concentrated water passes through a carbon tower.
Example 2
5000g of CBS wastewater (COD18000-20000) was taken, and 7g of hydrochloric acid (35.5%) was added to the CBS wastewater to adjust the pH to about 6. 2.5g of PASC solution with the mass concentration of 2 percent is sequentially added under the stirring state with the speed of 100r/min, the mass concentration is 1 per thousand, 2.5g of anion PAM with the polymerization degree of 2500 ten thousand is added, and after the flocs are settled, the supernatant is taken and pumped into an active carbon adsorption column (the particle size of the active carbon is 2mm, the iodine value is 700, and the retention time is 4 hours) by a metering pump. After the treatment, the COD of the wastewater can be reduced to about 3000, and the color is colorless and transparent. After the absorption, the waste water is filtered by a nanofiltration membrane, and about 4000g of clean water is obtained by recovery (the recovery rate is more than or equal to 80 percent, and the COD is less than 50). And carrying out flocculation treatment on the concentrated water obtained by nanofiltration again, and discharging the concentrated water after the concentrated water passes through a carbon tower.
Example 3
5000g of CBS wastewater (COD 18000-. 25g of PAFP solution with the mass concentration of 2 percent is added in sequence under the stirring state with the speed of 100r/min, the mass concentration is 1 per thousand, 150g of nonionic PAM with the polymerization degree of 500 ten thousand is added, after the flocs are settled, the supernatant is taken and pumped into an activated carbon adsorption column (the particle size of the activated carbon is 10mm, the iodine value is 1500, and the retention time is 4h) by a metering pump. After the treatment, the COD of the wastewater can be reduced to about 3000, and the color is colorless and transparent. After the absorption, the waste water is filtered by a nanofiltration membrane, and about 4000g of clean water is obtained by recovery (the recovery rate is more than or equal to 80 percent, and the COD is less than 50). And carrying out flocculation treatment on the concentrated water obtained by nanofiltration again, and discharging the concentrated water after the concentrated water passes through a carbon tower.
Example 4
5000g of CBS wastewater (COD 18000-. 250g of PAFC solution with the mass concentration of 2 percent is sequentially added under the stirring state with the speed of 100r/min, the mass concentration is 1 per mill, 150g of cationic PAM with the ionicity of 20 percent is added, and after the flocs are settled, the supernatant is taken and pumped into an activated carbon adsorption column (the particle size of the activated carbon is 10mm, the iodine value is 1500, and the retention time is 4 hours) by a metering pump. After the treatment, the COD of the wastewater can be reduced to about 3000, and the color is colorless and transparent. After the absorption, the waste water is filtered by a nanofiltration membrane, and about 4000g of clean water is obtained by recovery (the recovery rate is more than or equal to 80 percent, and the COD is less than 50). And carrying out flocculation treatment on the concentrated water obtained by nanofiltration again, and discharging the concentrated water after the concentrated water passes through a carbon tower.
Example 5
5000g of CBS wastewater (COD 18000-. 75g of BPFC solution with the mass concentration of 2 percent is added in sequence under the stirring state with the speed of 120r/min, the mass concentration is 1 per thousand, 30g of zwitterion with the polymerization degree of 1000 ten thousand is added, and after the flocs are settled, the supernatant is taken and pumped into an activated carbon adsorption column (the particle size of the activated carbon is 5mm, the iodine value is 800, and the retention time is 4 hours) by a metering pump. After the treatment, the COD of the wastewater can be reduced to about 3000, and the color is colorless and transparent. After the absorption, the waste water is filtered by a nanofiltration membrane, and about 4000g of clean water is obtained by recovery (the recovery rate is more than or equal to 80 percent, and the COD is less than 50 percent). And carrying out flocculation treatment on the concentrated water obtained by nanofiltration again, and discharging the concentrated water after the concentrated water passes through a carbon tower.
Example 6
Pumping CBS wastewater (COD is 18000-. Stirring and mixing to agglomerate the flocs, overflowing to a mud-water separation device of a spiral shell stacking machine, continuously feeding the obtained clear liquid into an activated carbon tower for adsorption (the activated carbon is high-strength granular carbon which can be recycled, the carbon loading is 100g, the particle size of the activated carbon is 5mm, and the iodine value is 800), and reducing the COD of the adsorbed wastewater to about 2000. The wastewater after adsorption is continuously treated by a nanofiltration membrane to obtain reuse water with COD of about 50, and the concentrated water obtained after nanofiltration is returned to the first flocculation tank for flocculation treatment.
Example 7
Pumping CBS wastewater (COD is 18000-20000) into a static mixer, adjusting the pH value of NS wastewater for removing tert-butylamine to about 6 by adopting industrial hydrochloric acid, continuously feeding the wastewater after the pH value is adjusted to a first flocculation tank of a spiral shell stacking machine by using a wastewater feed pump, continuously adding a PAC solution with the concentration of 5 percent and the mass of 50 per mill of the wastewater after the wastewater enters the first flocculation tank of the spiral shell stacking machine, continuously overflowing the wastewater into a second flocculation tank of the spiral shell stacking machine under the stirring state of 120r/min, and continuously adding 80 percent cationic PAM emulsion with the concentration of 1 per mill and the mass of 30 per mill of the wastewater into the second flocculation tank by using a PAM feed pump after the water enters a half liquid level. Stirring and mixing to agglomerate the flocs, overflowing to a mud-water separation device of a screw stacking machine, continuously feeding the obtained clear liquid into an activated carbon tower for adsorption (the activated carbon is high-strength granular carbon which can be recycled, the carbon loading is 100g, the particle size of the activated carbon is 5mm, and the iodine value is 800), and reducing the COD of the waste water after adsorption to about 2000. The wastewater after adsorption is continuously treated by a nanofiltration membrane to obtain reuse water with COD of about 50, and the concentrated water obtained after nanofiltration is returned to the first flocculation tank for flocculation treatment.
Example 8
Pumping CBS wastewater (COD is 18000-20000) into a static mixer, adjusting the pH value of NS wastewater subjected to tertiary butylamine removal to about 6 by adopting industrial hydrochloric acid, continuously feeding the wastewater subjected to pH value adjustment to a first flocculation tank of a spiral shell stacking machine by using a wastewater feeding pump, continuously adding a PAC solution with the concentration of 5% and the mass of the wastewater of 0.5 per thousand after the wastewater enters the first flocculation tank of the spiral shell stacking machine, continuously overflowing the wastewater into a second flocculation tank of the spiral shell stacking machine under the stirring state of the speed of 120r/min, and continuously adding anionic PAM emulsion with the concentration of 1 per thousand and the polymerization degree of 1000 ten thousand and the mass of the wastewater of 0.5 per thousand to the second flocculation tank by using a PAM feeding pump after the water reaches a half liquid level. Stirring and mixing to agglomerate the flocs, overflowing to a mud-water separation device of a screw stacking machine, continuously feeding the obtained clear liquid into an activated carbon tower for adsorption (the activated carbon is high-strength granular carbon which can be recycled, the carbon loading is 100g, the particle size of the activated carbon is 5mm, and the iodine value is 800), and reducing the COD of the adsorbed wastewater to about 2000. The wastewater after adsorption is continuously treated by a nanofiltration membrane to obtain reuse water with COD of about 50, and the concentrated water obtained after nanofiltration is returned to the first flocculation tank for flocculation treatment.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the treatment method provides a solution for separating floccules, macromolecular organic matters, colloids and micromolecular organic matters in the wastewater of the oxidation CBS process. Flocculating flocculate, macromolecular organic matter and colloid, separating flocculated flocculate by solid-liquid separation to eliminate most of macromolecular matter, adsorbing to eliminate small molecular organic matter, microfiltering, ultrafiltering or nanofiltering to purify the adsorbed waste water, and using the clear liquid as reuse water. The method is easy to implement, and the treatment of each step realizes the synergistic effect, thereby realizing the high-efficiency treatment of the wastewater of the oxidation CBS process.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made without departing from the spirit and principle of the present invention shall fall within the protection scope of the present invention.
Claims (10)
1. A treatment method for wastewater from a process for producing a rubber vulcanization accelerator CBS by an oxidation method is characterized by comprising the following steps:
step S1, adjusting the pH value of the process wastewater to 5-7, and then sequentially performing flocculation treatment and solid-liquid separation to obtain clear liquid and flocculate;
step S2, carrying out adsorption treatment on the clear liquid to obtain adsorbed wastewater;
and step S3, filtering the waste water after adsorption to obtain reusable water and concentrated water, wherein the filtering is microfiltration, ultrafiltration or nanofiltration.
2. The treatment method according to claim 1, wherein the step S1 is performed by using a flocculating agent, preferably the flocculating agent comprises an inorganic flocculating agent and an organic flocculating agent, preferably the inorganic flocculating agent is selected from any one or more of polyaluminum chloride, polyferric sulfate, polymeric ferric silicate, polyaluminum chloride, polymeric ferric chloride, polysilicic acid, polyaluminum ferric silicate, polymeric ferric sulfate chloride, polymeric aluminum ferric chloride, polymeric aluminum sulfate, polymeric aluminum phosphate, polymeric ferric chloride, polymeric ferric phosphate, polyaluminum ferric silicate sulfate, polymeric aluminum ferric chloride, polymeric ferric aluminum phosphate, silicon calcium composite polyferric chloride and biological polyferric, and the organic flocculating agent is polyacrylamide flocculating agent.
3. The treatment method according to claim 2, wherein the polyacrylamide flocculant is any one of an anionic polyacrylamide flocculant, a nonionic polyacrylamide flocculant, a zwitterionic polyacrylamide flocculant and a cationic polyacrylamide flocculant, preferably the degree of polymerization of the nonionic polyacrylamide flocculant, the anionic polyacrylamide flocculant and the zwitterionic polyacrylamide flocculant is 500 to 2500 ten thousand, and preferably the degree of ionization of the cationic polyacrylamide flocculant is 20 to 80%.
4. The processing method according to claim 2, wherein the processing method is a batch processing method, and the step S1 includes:
mixing the process wastewater with the pH value of 5-7 with the inorganic flocculant for primary flocculation to obtain a first mixed system, wherein the inorganic flocculant is calculated by a 2% aqueous solution by mass, and preferably the use amount of the inorganic flocculant is 0.5-50 per mill of the mass of the process wastewater;
mixing the first mixed system with the organic flocculant for secondary flocculation to obtain a second mixed system, wherein the organic flocculant is an emulsion with the mass content of 1 per mill, and preferably the dosage of the organic flocculant is 0.5-30 per mill of the mass of the process wastewater;
and carrying out solid-liquid separation on the second mixed system to obtain the clear liquid and the flocculate.
5. The processing method according to claim 2, wherein the processing method is a continuous processing method, and the step S1 includes:
continuously feeding the process wastewater with the pH value of 5-7 into a first flocculation tank, and continuously adding the inorganic flocculant into the first flocculation tank for primary flocculation treatment to obtain a first mixing system, wherein the inorganic flocculant is calculated by an aqueous solution with the mass content of 5%, and preferably the use amount of the inorganic flocculant is 0.5-50 per mill of the mass of the process wastewater;
continuously overflowing the first mixed system into a second flocculation tank, and adding the organic flocculant into the second flocculation tank for secondary flocculation treatment when the volume of the first mixed system is one half of that of the second flocculation tank to obtain a second mixed system; the organic flocculant is calculated by emulsion with the mass content of 1 per mill, and the dosage of the organic flocculant is 0.5-30 per mill of the mass of the process wastewater;
and continuously carrying out solid-liquid separation on the overflowed second mixed system to obtain the clear liquid and the flocculate.
6. The treatment method according to any one of claims 1 to 5, wherein stirring is performed during the flocculation treatment in the step S1, and the stirring speed is 80-120 r/min.
7. The process according to any one of claims 1 to 5, wherein in step S1, the solid-liquid separation is sedimentation or filtration.
8. The treatment method according to any one of claims 1 to 5, wherein the step S2 is performed with activated carbon for the adsorption treatment.
9. The method according to claim 8, wherein the activated carbon has a particle size of 2 to 10mm and an iodine value of 700 to 1500.
10. The treatment method according to claim 1, further comprising returning the concentrated water to the step S1 to perform the flocculation treatment together with the process wastewater.
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| CN115057593A (en) * | 2022-08-03 | 2022-09-16 | 广东水清环境治理有限公司 | Combined treatment method for circuit board wastewater |
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| CN102874961A (en) * | 2012-09-25 | 2013-01-16 | 科迈化工股份有限公司 | Method for treating wastewater of rubber vulcanization accelerator N-cyclohexyl-2-benzothiazolylsulfenamide (CBS) |
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| CN102874961A (en) * | 2012-09-25 | 2013-01-16 | 科迈化工股份有限公司 | Method for treating wastewater of rubber vulcanization accelerator N-cyclohexyl-2-benzothiazolylsulfenamide (CBS) |
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| 《天津环境保护丛书》编委会: "《天津环境污染防治》", 北京：中国环境科学出版社, pages: 140 * |
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| CN115057593A (en) * | 2022-08-03 | 2022-09-16 | 广东水清环境治理有限公司 | Combined treatment method for circuit board wastewater |
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