CN104355450A - High-salinity wastewater grading recycling process - Google Patents
High-salinity wastewater grading recycling process Download PDFInfo
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- CN104355450A CN104355450A CN201410632676.2A CN201410632676A CN104355450A CN 104355450 A CN104355450 A CN 104355450A CN 201410632676 A CN201410632676 A CN 201410632676A CN 104355450 A CN104355450 A CN 104355450A
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Abstract
The invention discloses a high-salinity wastewater grading recycling process. The process comprises the following steps: adding medium-strong base, strong base or CO2 to high-salinity wastewater, carrying out flocculation and sedimentation, sequentially filtering a supernatant liquid obtained from flocculation and sedimentation by virtue of a multi-media filter and a cartridge filter, adsorbing positive ions of filtrate by virtue of cationic resin, adsorbing the filtrate through anionic resin or electro-dialysis, and filtering with a reverse osmosis (RO) membrane. By virtue of the recycling process disclosed by the invention, the treated high-salinity wastewater can reach standards of industrial circulating cooling water and steam boiling water, and more than 90% of water of regenerating cationic resin and anionic resin can be recycled and retreated in a regulating tank, so as to save water resources, reduce the sewage discharge capacity, lower the investment, reduce the operating expense and enhance the treatment effect; sewage from the electro-dialysis can enter an airing tank or spray fly ash to realize zero discharge of enterprise sewage; by virtue of cationic resin bed and electro-dialysis, the effluent rate can reach more than 95%, thus greatly saving water resources and realizing zero discharge of enterprises.
Description
Technical field
After the present invention relates to sewage disposal, high-salt wastewater reprocessing becomes to produce the separate-recycling technique of reuse water.
Background technology
Current industrial high-salt wastewater flocculation sediment after highly basic, highly basic in adding, supernatant liquor after flocculation sediment is filtered, directly by reverse osmosis membrane after filtering, by separation and Extraction, the purifying of film and concentrate the object reaching deep desalting, producing water ratio reaches about 80%.The feature of this method is energy-conservation, compares distillation technique energy consumption and is only 1/40, but only remove suspension at strainer, and the water after filtration is easy to film to block by film, and it is high to change film rate, and running cost is high, and the high dense water yield is large.Thus improve water quality after filtering, increase producing water ratio, reduce running cost and become problem demanding prompt solution.
Summary of the invention
According to the difference of saltiness in sewage after process, the invention provides and a kind ofly salinity in water is removed the separate-recycling technique reaching production reuse.
For realizing the object of the invention, this high-salt wastewater separate-recycling technique comprises the following steps:
One, for the treatment process of hardness in water after sewage disposal lower than 1500mg/L
A., in adding in high-salt wastewater under whipped state after highly basic and highly basic, stir 20 ~ 50 minutes flocculation sediments, the mass ratio of described high-salt wastewater, middle highly basic, highly basic is 1000: 1 ~ 10: 1 ~ 10;
B. the supernatant liquor after flocculation sediment after intermediate pool stabilizing water quality, enter more medium filter successively and cartridge filter filters, and the press filtration after concentrated of the mud after flocculation sediment, goes out the waste back-cycling systemic circulation process of more medium filter;
C. the filtrate going out cartridge filter is stimulated the menstrual flow after resin cation (R.C.) absorption, through electrodialysis or resin anion(R.A) absorption, then reverse osmosis membrane filtration is entered, the waste water retrieval system circular treatment respectively of cation regenerant resin and resin anion(R.A), the waste water going out reverse osmosis membrane enters resin cation (R.C.) or retrieval system circular treatment.
Described middle highly basic adopts calcium hydroxide and sodium carbonate, and described highly basic adopts sodium hydroxide.
Supernatant liquor after described flocculation sediment flows through and passes into CO
2reaction tank after, then through intermediate pool stabilizing water quality, then enter more medium filter successively and cartridge filter filters.
In described step c after electrodialysis, experience a resin cation (R.C.) Liquidity limit and electrodialysis absorption at least again, then enter reverse osmosis membrane filtration.
The technical progress that the present invention obtains:
Adopt the present invention can reach the object of the zero release standard implementation haline water separate-recycling of haline water, overcome the drawback that prior art exists.
Present invention process process high-salt wastewater is flocculation sediment after calcium carbonate in alkaline cleaning removal water and magnesium hydroxide hardness, supernatant liquor after flocculation sediment removes zwitterion through positive resin and negative resin bed after more medium filter and cartridge filter process remove suspended substance can remove most of molecular substance in water, rear electrodialysis and film excessively.The running cost of electrodialysis and film can be saved after negative and positive bed, water rate is high, the dense water of electrodialysis and film can return equalizing tank circular treatment, reduces concentrated water drainage high-volume, and the waste water more than 90% of cation regenerant resin and resin anion(R.A) is recyclable carries out reprocessing to equalizing tank, water resources can be saved, reduce blowdown flow rate, less investment, working cost is low, treatment effect is good, and the high-salt wastewater after process can be made to reach industrial cooling circulating water and steam boiler water supply standard.
Accompanying drawing explanation
Fig. 1 is that hardness is lower than 1500mg/L high-salt wastewater separate-recycling process flow diagram.
Fig. 2 is that hardness is higher than 1500mg/L high-salt wastewater separate-recycling process flow diagram.
Fig. 3 is that the present invention adopts highly basic and CO
2process high-salt wastewater process flow diagram.
Embodiment
Embodiment 1: as shown in Figure 1, certain factory's high-salt wastewater water quality: hardness 1360mg/L, TDS (total dissolved solid): 2130mg/L, pH:8.5, sulfate ion 652mg/L, chlorion 280mg/L.
As follows to above-mentioned high-salt wastewater separate-recycling technique:
A. high-salt wastewater enter after equalizing tank 1 homogenizes reaction tank 2 add calcium hydroxide, sodium carbonate flocculation, the mass ratio of high-salt wastewater, calcium hydroxide and sodium carbonate is 1000: 1 ~ 10: 1 ~ 10, stir and pass into horizontal sedimentation tank 3 flocculation sediment after 20 ~ 50 minutes, after flocculation sediment, water quality is TDS (total dissolved solid): 3060mg/L, pH:8.5 ~ 12, hardness: 10 ~ 800mg/L;
B. the supernatant liquor after precipitation enters more medium filter 6 and (is produced by Shenzhen Water Management Equipment Ltd. of HTC after intermediate pool 4 stabilizing water quality, model: Φ 1000) filter, then intermediate water tank 7 stabilizing water quality is entered, (produced by Shenzhen Water Management Equipment Ltd. of HTC through cartridge filter 8 again, model: Φ 500) filter, and then enter hydrogen form cation resin bed 9 Liquidity limit and acidulous anion resin bed 10 adsorpting anion successively, the press filtration after sludge thickener 5 is concentrated of mud after flocculation sediment, equalizing tank 1 circular treatment is returned after filtrate desliming after press filtration, waste back-cycling equalizing tank 1 circular treatment of backwash more medium filter 6, effluent quality: TDS:628mg/L, pH:6.5, hardness: 5 ~ 45mg/L, sulfate radical 60 ~ 180mg/L, chlorine root 80 ~ 200mg/L after filtering, water outlet reaches refrigeration cycle water quality standard, and the waste water of regeneration Hydrogen resin cation (R.C.) bed 9 and acidulous anion resin bed 10 returns equalizing tank 1 circular treatment respectively,
C. the water outlet after acidulous anion resin bed 10 adsorpting anion enters RO film 11 and filters, RO film 11 filters rear effluent quality TDS:20 ~ 60mg/L, pH:6.5, hardness: 0 ~ 10mg/L, sulfate ion 0 ~ 50mg/L, chlorion 0 ~ 60mg/L, RO film 11 water outlet reaches the requirement of steam boiler water, and the waste water going out RO film 11 returns equalizing tank 1 circular treatment.
In the present embodiment:
(1) after adopting hydrogen form cation resin bed 9 and acidulous anion resin bed 10 to adsorb zwitterion, water outlet can directly reach refrigeration cycle water quality standard, can reach steam boiler water supply standard, can realize supplying water in different qualities after RO film 11.
(2) the dense water of RO film 11 blowdown enters equalizing tank 1 and recycles, and saves water resources.
(3) waste water regenerating the waste water 1% ~ 10% of Hydrogen resin cation (R.C.) bed 9 and acidulous anion resin bed 10 can enter airing pond or water powder coal ash, thus realizes the zero release of enterprise.
Embodiment 2: be illustrated in figure 2 for the high-salt wastewater separate-recycling technical process of hardness in water after sewage disposal higher than 1500mg/L, certain factory's haline water water quality: hardness 5640mg/L, TDS:3890mg/L, pH:8.5, sulfate ion 1737mg/L, chlorion 360mg/L.Its separate-recycling technological process is as follows:
A. high-salt wastewater regulates to enter reaction tank 2 after water and add calcium hydroxide, sodium carbonate flocculation through equalizing tank 1, the mass ratio of high-salt wastewater, calcium hydroxide and sodium carbonate is 1000: 1 ~ 10: 1 ~ 10, stir and pass into horizontal sedimentation tank 3 flocculation sediment after 20 ~ 50 minutes, after flocculation sediment, water quality is TDS:4850mg/L, pH:8.5 ~ 12, hardness: 10 ~ 1500mg/L;
B. the supernatant liquor after precipitation filters through more medium filter 6 after intermediate pool 4 stabilizing water quality, after entering intermediate water tank 7 stabilizing water quality again, filter and hydrogen form cation resin bed 9 Liquidity limit through cartridge filter 8 successively, the press filtration after sludge thickener 5 is concentrated of mud after flocculation sediment, equalizing tank 1 circular treatment is returned, waste back-cycling equalizing tank 1 circular treatment of backwash more medium filter 6 after filtrate desliming after press filtration;
C. after resin cation (R.C.) bed 9 adsorbs, through one-level electrodialysis 12, dense water is through one-level resin cation (R.C.) bed 91, add after Scale inhibitors again and fresh water after secondary electrodialysis 13, dense water is through secondary resin cation (R.C.) bed 92, go out together with fresh water with secondary electrodialysis 13 after adding Scale inhibitors and filter through three-stage electrodialysis 14, then enter reverse osmosis membrane 11 to filter, the waste water wherein regenerating Hydrogen resin cation (R.C.) bed 9 returns equalizing tank 1 circular treatment, and the waste water of backwash reverse osmosis membrane 11 enters hydrogen form cation resin bed 9 and recycles.Reach through three-stage electrodialysis, secondary positive resin bed 92 water softener effluent quality: TDS:580mg/L, pH:6.5, hardness: 0 ~ 45mg/L, sulfate ion 60 ~ 180mg/L, chlorion 80 ~ 200mg/L, through the producing water ratio 90% ~ 95% of three-stage electrodialysis, water outlet reaches refrigeration cycle water quality standard, and third stage electrodialysis 14 sewer is to airing pond or water powder coal ash.RO film 11 effluent quality TDS:20 ~ 60mg/L, pH:6.5, hardness: 0 ~ 10mg/L, sulfate ion 0 ~ 50mg/L, chlorion 0 ~ 80mg/L, water outlet reaches steam boiler water supply standard.
In the present embodiment:
(1) form magnesium hydroxide after adding calcium hydroxide, sodium carbonate in reaction tank 2, precipitation of calcium carbonate to remove most water hardness, thus is conducive to electrodialysis safe and stable operation.
(2) add resin cation (R.C.) bed 9 before one-level electrodialysis 12 and prevent human operational error, be conducive to electrodialytic safe and stable operation.
(3) two, enter resin cation (R.C.) bed 91,92 before three-stage electrodialysis 13,14 and add slow-release scale inhibitor, fouling in electrodialysis can be prevented, ensure that electrodialytic safe operation, can water rate be improved simultaneously.
(4) water rate of existing electrodialysis process is 70% ~ 75%, present invention process is through three-stage electrodialysis, three grades of resin cation (R.C.) beds after adding slow-release scale inhibitor, water rate can reach more than 90% ~ 95%, thus has greatly saved water resources, significantly reduces quantity of wastewater effluent.
(5) electrodialysis water outlet is better than national refrigeration cycle water quality standard, and after RO film 11, be better than steam boiler water supply standard, less investment, working cost is low, and treatment effect is good.
(6) reuse water 90% ~ 99% of resin cation (R.C.) bed 9 is recycled to equalizing tank 1 and carries out reprocessing, can save water resources, reduces blowdown flow rate.
(7) achieve supplying water in different qualities, the dense water of RO film 11 blowdown returns positive resin bed 9 and recycles, and saves water resources, and the sewer of electrodialysis 14 enters airing pond or waters the sewage zero-discharge that powder coal ash achieves enterprise.
Embodiment 3:
Be illustrated in figure 3 and adopt highly basic and CO
2the technical process of process high-salt wastewater, certain factory's haline water water quality: hardness 4970mg/L, TDS:3650mg/L, pH:8.5, sulfate ion 1524mg/L, chlorion 360mg/L.Its separate-recycling technological process is as follows:
A. high-salt wastewater regulates to enter reaction tank 2 after water and add sodium hydroxide flocculation through equalizing tank 1, and stir after 20 ~ 50 minutes, through horizontal sedimentation tank 3 flocculation sediment, the supernatant liquor after flocculation sediment enters CO
2reaction tank 15, to CO
2reaction tank 15 passes into CO
2after enter horizontal sedimentation tank 31 and flocculate, high-salt wastewater, sodium hydroxide and CO
2between mass ratio be 1000: 1 ~ 10: 1 ~ 10, after horizontal sedimentation tank 31 flocculation sediment, water quality is TDS:4520mg/L, pH:8.5 ~ 12.6, hardness: 10 ~ 1500mg/L;
B. the supernatant liquor after flocculation sediment enters more medium filter 6 and filters after intermediate pool 4 stabilizing water quality, then enters intermediate water tank 7 stabilizing water quality, then enters hydrogen form cation resin bed 9 Liquidity limit after cartridge filter 8 filters; The press filtration after sludge thickener 5 is concentrated of mud after flocculation sediment, returns equalizing tank 1 circular treatment, waste back-cycling equalizing tank 1 circular treatment of backwash more medium filter 6 after the filtrate desliming after press filtration:
C. the filtrate after hydrogen form cation resin bed 9 Liquidity limit after one-level electrodialysis 12 dense water through one-level resin cation (R.C.) bed 91 Liquidity limit, dense water is gone out through secondary resin cation (R.C.) bed 92 Liquidity limit with fresh water through secondary electrodialysis 13 after adding Scale inhibitors again, then go out with secondary electrodialysis 13 after adding Scale inhibitors together with fresh water to enter reverse osmosis membrane 11 and filter after three-stage electrodialysis 14 filters, the waste water 90% ~ 99% wherein regenerating Hydrogen resin cation (R.C.) bed 9 returns equalizing tank 1 circular treatment, the waste water going out reverse osmosis membrane 11 enters hydrogen form cation resin bed 9 circular treatment.Can reach through three-stage electrodialysis and secondary positive resin bed water softener effluent quality: TDS:580mg/L, pH:6.5, hardness: 0 ~ 45mg/L, sulfate ion 60 ~ 180mg/L, chlorion 80 ~ 200mg/L; Through the producing water ratio 90% ~ 95% of three-stage electrodialysis, water outlet reaches refrigeration cycle water quality standard, and third stage electrodialysis 14 sewer is to airing pond or water powder coal ash.RO film 11 effluent quality TDS:20 ~ 60mg/L, pH:6.5, hardness: 0 ~ 10mg/L, sulfate ion 0 ~ 50mg/L, chlorion 0 ~ 60mg/L, water outlet reaches steam boiler water supply standard, and the waste water of regeneration Hydrogen resin cation (R.C.) bed 9 returns equalizing tank 1 circular treatment, and RO film 11 sewer returns and enters Hydrogen positive resin bed 9 circular treatment.
In the present embodiment:
(1) add after sodium hydroxide makes it to form magnesium hydrate precipitate removal unit using different water hardness in reaction tank 2, at CO
2reaction tank 15 adds CO again
2make it to form precipitation of calcium carbonate and remove the most of water hardness of residue, achieve the recycling of carbonic acid gas, turn waste into wealth, decrease carbon emission, and to acid adding in water, stiffening effect in water need not be removed good.
(2) enter resin cation (R.C.) bed 9 before one-level electrodialysis 12 and prevent human operational error, be conducive to electrodialytic safe and stable operation simultaneously.
(3) two, enter resin cation (R.C.) bed 91,92 before three-stage electrodialysis 13,14 and add slow-release scale inhibitor, fouling in electrodialysis can be prevented, ensure that electrodialytic safe operation, can water rate be improved simultaneously.
(4) water rate of existing electrodialysis process is 70% ~ 75%, present invention process is through three-stage electrodialysis, three grades of resin cation (R.C.) beds after adding slow-release scale inhibitor, water rate can reach more than 90% ~ 95%, thus has greatly saved water resources, significantly reduces quantity of wastewater effluent.
(5) electrodialysis water outlet is better than national refrigeration cycle water quality standard, and after RO film, be better than steam boiler water supply standard, less investment, working cost is low, and treatment effect is good.
(6) reuse water 90% ~ 99% of resin cation (R.C.) bed 9 is recycled to equalizing tank 1 and carries out reprocessing, can save water resources, reduces blowdown flow rate.
(7) supplying water in different qualities is achieved, the dense water of RO film 11 blowdown returns positive resin bed 9 circular treatment, save water resources, precipitating sludge filtrate after press filtration returns equalizing tank circular treatment, and the sewer of electrodialysis 14 enters airing pond or waters the zero release that powder coal ash achieves enterprise.
Claims (4)
1. a high-salt wastewater separate-recycling technique, is characterized in that it comprises following technological process:
A., in adding in high-salt wastewater under whipped state after highly basic and highly basic, stir 20 ~ 50 minutes flocculation sediments, the mass ratio of described high-salt wastewater, middle highly basic, highly basic is 1000: 1 ~ 10: 1 ~ 10;
B. the supernatant liquor after flocculation sediment after intermediate pool stabilizing water quality, enter more medium filter successively and cartridge filter filters, and the press filtration after concentrated of the mud after flocculation sediment, goes out the waste back-cycling systemic circulation process of more medium filter;
C. the filtrate going out cartridge filter is stimulated the menstrual flow after resin cation (R.C.) absorption, through electrodialysis or resin anion(R.A) absorption, then reverse osmosis membrane filtration is entered, the waste water retrieval system circular treatment respectively of cation regenerant resin and resin anion(R.A), the waste water going out reverse osmosis membrane enters resin cation (R.C.) or retrieval system circular treatment.
2. high-salt wastewater separate-recycling technique according to claim 1, it is characterized in that described middle highly basic adopts calcium hydroxide and sodium carbonate, described highly basic adopts sodium hydroxide.
3. high-salt wastewater separate-recycling technique according to claim 1, is characterized in that the supernatant liquor after described flocculation sediment flows through and passes into CO
2reaction tank after, then through intermediate pool stabilizing water quality, then enter more medium filter successively and cartridge filter filters.
4. high-salt wastewater separate-recycling technique according to claim 1, is characterized in that in described step c after electrodialysis, experiences a resin cation (R.C.) and electrodialysis absorption at least again, then enters reverse osmosis membrane filtration.
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| CN105585221A (en) * | 2016-01-27 | 2016-05-18 | 山东省环保产业股份有限公司 | Pretreatment method of phosphatizing wastewater for automobile painting |
| CN106082501A (en) * | 2016-08-11 | 2016-11-09 | 上海洗霸科技股份有限公司 | Boiler blowdown water recovery processing technique based on ion exchange with chemical precipitation |
| CN107098526A (en) * | 2016-02-22 | 2017-08-29 | 麦王环境技术股份有限公司 | The film concentrator and handling process of strong brine zero-emission sub-prime crystallization |
| CN108069546A (en) * | 2016-11-15 | 2018-05-25 | 广州达意隆包装机械股份有限公司 | Silver in waste recovery system and silver in waste recovery method |
| CN109650835A (en) * | 2018-12-26 | 2019-04-19 | 国电新能源技术研究院有限公司 | A kind for the treatment of method for high-salinity wastewater |
| CN111592148A (en) * | 2020-06-08 | 2020-08-28 | 导洁(北京)环境科技有限公司 | Process method for converting high-salinity wastewater into NaOH solution |
| CN116395903A (en) * | 2023-05-17 | 2023-07-07 | 连云港中星能源有限公司 | Preparation process of desalted raw water for industrial steam |
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| CN111592148A (en) * | 2020-06-08 | 2020-08-28 | 导洁(北京)环境科技有限公司 | Process method for converting high-salinity wastewater into NaOH solution |
| CN116395903A (en) * | 2023-05-17 | 2023-07-07 | 连云港中星能源有限公司 | Preparation process of desalted raw water for industrial steam |
| CN116395903B (en) * | 2023-05-17 | 2023-08-29 | 连云港中星能源有限公司 | Preparation process of desalted raw water for industrial steam |
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Application publication date: 20150218 |