CN102765791B - Modified physical chemical coagulation sewage treatment method - Google Patents
Modified physical chemical coagulation sewage treatment method Download PDFInfo
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- CN102765791B CN102765791B CN2012103022183A CN201210302218A CN102765791B CN 102765791 B CN102765791 B CN 102765791B CN 2012103022183 A CN2012103022183 A CN 2012103022183A CN 201210302218 A CN201210302218 A CN 201210302218A CN 102765791 B CN102765791 B CN 102765791B
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Abstract
Provided is a modified physical chemical coagulation sewage treatment method. Flocculant is respectively and continuously added at least in the initial stage and the later stage of sewage running under a running state of sewage in a pipeline through pumping equipment, the flocculant and the sewage are mixed in a joint running process, and sedimentation and solid-liquid separation are finally carried out. When the flocculant added in the later stage and the sewage in the running state are mixed, flow velocity of the mixed sewage is controlled to be 0.1-1m/s through a buffer cell and maintained for at least 5 minutes, then the mixed sewage is mixed with continuously-added flocculant in a state that the flow velocity is 0.1-0.5m/s to maintain for 10 minutes, and finally the mixed sewage is sent to a sedimentation device for solid-liquid separation. The modified physical chemical coagulation sewage treatment method can shorten settling separation time from 1-2hours to 0.4-0.6 hours, handling ability of a solid-liquid separation device promotes by 2-3 times, content indexes of COD, BOD and the like of purified water are greatly reduced further, SS can be less than 10mg/l and achieve class A discharge standard regulated by national GB18918-2002.
Description
Technical field
The present invention relates to a kind of to the improvement with physical chemistry cohesion mode sewage treatment method.
Background technology
In the Chinese patent of Granted publication CN 1098813C, the present inventor provides a kind of sewage water treatment method in physical chemistry cohesion mode,, sewage is sent into pipeline through pumping equipment, and under running status at least at its initial operating stage stage and later stage, add in a continuous manner respectively flocculation agent, make it realize fully mixing in the common operational process with sewage, make pollutant component form the aggregate particle, finally carry out sedimentation and solid-liquid separation, what obtain recycling purifies waste water.Find in practice, though this mode can be processed sewage more quickly, process the COD(chemical oxygen demand in afterpurification water), BOD (biological oxygen demand (BOD)), the SS(suspended matter) etc. index still can not reach very good degree.Through further going deep into test and study, find, its reason is in above-mentioned treating processes, formed aggregate particle less under the coagulation of flocculation agent, and size is inhomogeneous, in follow-up settlement separate process, the particulate sedimentation that particle diameter is tiny is slow, even is difficult to sedimentation, has affected the further reduction of the indexs such as COD, the BOD of water quality, SS after the processing.Therefore, further shortening under the flocculation agent effect settling time of flocculated particle body, improve the sedimentation ratio, is problem to be solved by this invention.
Summary of the invention
Given this, on the sewage water treatment method basis of the above-mentioned patent of contriver, the invention provides a kind of improved physic and chemical condensation method for treatment of foulwater, can significantly shorten the settling time, improve the sedimentation ratio, significantly improve the water quality standard after processing.
The improved physic and chemical condensation method for treatment of foulwater of the present invention is to have kept, on the basis of the disclosed sewage basic skills of above-mentioned patent documentation, the post-processed mode being improved in early stage.That is, sewage is sent into to pipeline with pumping equipment and under running status, at least initial stage and the later stage in the sewage operation adds respectively said flocculation agent in a continuous manner, and it is mixed in the common operational process with sewage.Wherein, after last adds flocculation agent and sewage in running status mixes, make the combined sewage flow rate control at the 0.1-1 meter per second and at least maintain 5 minutes through buffer cell, then under the state that is 0.1～0.5 meter per second at its flow velocity, after mixing with the flocculation agent added continuously and at least maintaining 10 minutes, send into corresponding solid-liquid separation sedimentation device, carry out sedimentation and solid-liquid separation.
Test-results shows, with pumping mode, the said e Foerderanlage with high-speed mixing function in above-mentioned patent documentation for example, sewage is flowed in the pipeline high speed, be conducive to mix with the flocculation agent Quick uniform, but the turbulent flow running status of this high speed (it is even higher that flow velocity is greater than 1m/s usually) also is difficult for making forming under the flocculation agent effect larger aggregate particle simultaneously, or easily make established larger particles body again be broken into subparticle again, thereby affected the separating effect of posterior settlement, and to the index of correlation after the final processing of sewage.Aforesaid method of the present invention is just for this situation, the last time to after adding flocculation agent to mix in the sewage under running status, by the flow rate control of combined sewage at the 0.1-1 meter per second and maintain appropriate time, make the running status of sewage become laminar flow by turbulent flow, reduce intergranular collision, thereby be conducive to make established tiny aggregate particle to become gradually large.
For improving settling velocity and the sedimentation of flocculated particle body in follow-up settling process, obtain more fully fully, on the basis of above-mentioned coutroi velocity/flow state, further in the operation sewage be controlled under suitable flow velocity, add flocculation agent, make established aggregate particle under " bridge formation " effect of flocculation agent, can further form the granule of more volume on the one hand, can also make on the other hand formed macrobead body more solid.Larger and the more solid not breakable flocs unit particle of this granularity, be easier to sedimentation, guaranteed can complete more rapidly, up hill and dale solid-liquid separation at subsidence stage.
Be appreciated that thus, in aforesaid method, said flocculation agent can comprise various flocculation agents currently reported and/or that use, as polyacrylamide, chitin, causticization starch, Walocel MT 20.000PV, polyoxyethylene, polymine, polyacrylamide sodium etc., can be according to the source of processed sewage, and comprises that the characteristics such as pH value scope therefrom select, to adapt to the particular case of different processed sewage, guarantee treatment effect.Some flocculation agent, such as polyacrylamide, polyacrylamide sodium etc., also can be used as flocculation agent in the treating processes in early stage simultaneously.Test shows, preferably commonly uses flocculation agent and can select polyacrylamide, and chitin, causticization starch etc., can as the sewage that the pH value is 4 ~ 13 scopes, all have adaptability widely to the sewage of multiple source and/or character, obtains good flocculating effect.The consumption of flocculation agent is usually little, and for example processed water per ton is used 1-3g can obtain satisfied effect.
The ultimate principle of aforesaid method according to the present invention, can also be separately on the basis of foregoing or take more following further optimal ways with mutually combining:
Said for controlling the buffer cell of sewage operation flow velocity, preferably be adopted as a diameter be greater than before the volume of sewage in-service pipeline expand target phase, its form and/mode can determine according to practical situation, as vertical, horizontal etc. multi-form in be set to.
Said sewage mixes with flocculation agent, equally also can preferably adopt the volume of sewage in-service pipeline before a diameter is greater than to expand in target phase carries out, its form and/mode can determine according to practical situation equally, as vertical, horizontal etc. multi-form in be set to.
In addition, in the sediment after the sedimentation solid-liquid separation, also have part not yet fully and the flocculation agent of having an effect of the pollutent in sewage, therefore can be by the part sediment after the sedimentation solid-liquid separation, the initial period that returns to again sewage disposal recycles, make the partial agglomeration agent wherein do not played one's part to the full, continue and sewage generation coagulation.On the other hand, it is turbid that these sediments that return can also make sewage control, and increases the cohesion core in sewage, makes it more easily under the flocculation agent effect, complete agglomeration process.Thereby not only can reduce the consumption of flocculation agent, also help the raising of follow-up solid-liquid separation effect.Wherein the said sediment ratio recycled of returning, can consider and select according to the characteristics of sewage, the combined factors balances such as processing power of equipment, generally, usually can select 10 ~ 30% of solid-liquid separation sediment volume total amount.For example, day to process sanitary sewage 10, the sediment of 000m3/d is example, and sediment does not return and 15 (v) % sediment was returned in the sewage initiated process stage, and the flocculation agent consumption comparative test result that sewage disposal is consumed is as shown in table 1.The commercially available unit price of flocculation agent of take is 3200 yuan/tons, and only the saving of flocculation agent can reduce 178.85 ten thousand yuan of year processing costss.
Table 1 sediment returns to the contrast whether use affects the flocculation agent consumption
| The non-return dosage of PAC of sediment (t/y) | Dosage of PAC after sediment returns (t/y) | The dosage of PAC (t/y) of saving |
| 1168 | 657 | 511 |
The comparative test result of being undertaken by the sewage water treatment method before and after the present invention is improved shows, adopt treatment process of the present invention, sewage completes the disengaging time of solid-liquid sedimentation in equipment for separating liquid from solid, can be from improving 1 ~ 2 hour of former method, only significantly shorten to and need 0.4～0.6 hour, the processing power of equipment for separating liquid from solid has improved 2 ~ 3 times, the further decrease of energy is processed an index such as COD, BOD of rear sewage simultaneously, SS wherein can, lower than 10mg/l, reach the first class emission standard of GB18918-2002 national regulation.
Embodiment by the following examples is described in further detail foregoing of the present invention again.But this should be interpreted as to the scope of the above-mentioned theme of the present invention only limits to following example.Without departing from the idea case in the present invention described above, various replacements or the change according to ordinary skill knowledge and customary means, made, all should comprise within the scope of the invention.
Embodiment
embodiment 1
Press the mode of the Chinese patent embodiment 1 of notification number CN 1098813C, after the paper waste gradation moved in transport pipe is added to the flocculation agent aftertreatment, through vertical the first enlarged diameter section arranged, the waste water flow velocity is reduced to 0.8 m/s, after maintaining 6 minutes, send into the same vertical Second bobbin diameter section of expanding arranged through pipeline, under the running status that is 0.4 m/s at flow velocity, add flocculation agent polyacrylamide or causticization starch at its both port of origination place, maintain operation after 12 minutes, send in precipitation apparatus that to carry out solid-liquid settlement separate.0.5 hour settlement separate time.See off after sediment drying after the sedimentation solid-liquid separation, or the part sediment after settlement separate (10-30 (v) %) is returned and recycles, all the other sediment dryings are seen off.The result that adopts the present invention to improve front and back method contrasts as shown in table 2.
According to the result of table 2, with improve before compare, except filtering system, the power consumption of whole treatment unit can reduce 30 ~ 40%.Take the sewage disposal scale as 10000m3/d be example, per hour flow is 417 m3/h, power of motor is 22kw, power consumption every day is 22kw/h * 24h=528kwh, calculates with 365 days/year, 192,720 kwh can economize on electricity.Aspect reduction of discharging:
COD: the CER before improving is (0.525kg/m3-0.2102 kg/m3) * 10000 * 365d=1149.94t, after improving, is (0.525kg/m3-0.0356 kg/m3) * 10000 * 365d=1786.31t;
BOD: the CER before improving is (0.185 kg/m3-0.0836 kg/m3) * 10000 * 365d=370t, after improving, is (0.185 kg/m3-0.0082 kg/m3) * 10000 * 365d=645.3t;
SS: the CER before improving is (0.315 kg/m3-0.0655 kg/m3) * 10000 * 365d=910t, after improving, is (0.315 kg/m3-0.0082 kg/m3) * 10000 * 365d=1119t.
The improvement front and back are more as shown in table 3 to COD, BOD, SS CER.Sewage water treatment method of the present invention after having shown to improve, not only have great economic benefit, also has the environmental benefit of highly significant.
The sewage disposal comparative test result of table 2 embodiment 1
| Detect index | Sewage before processing | Method before improving | The inventive method |
| COD mg/l | 525.0 | 210.2 | 35.6 |
| BOD mg/l | 185.0 | 83.6 | 8.2 |
| SS mg/l | 315.0 | 8.5 | 2.5 |
| The solid-liquid settling time (h) | — | 1.5 | 0.5 |
Table 3 the inventive method and the COD, the BOD that improve front method, the contrast of SS CER
| Detect index | Before improvement (t/y) | The inventive method (t/y) | CER increases (t/y) | CER increases ratio |
| COD | 1149.94 | 1786.31 | 636.37 | 1.55 doubly |
| BOD | 370.0 | 645.3 | 275.3 | 1.74 doubly |
| SS | 910 | 1119.0 | 209 | 1.23 doubly |
embodiment 2
Press the mode of the Chinese patent embodiment 3 of notification number CN 1098813C, after the city domestic sewage gradation moved in transport pipe is added to the flocculation agent aftertreatment, through vertical the first enlarged diameter section arranged, the waste water flow velocity is reduced to 0.8 m/s, after maintaining 6 minutes, send into the same vertical Second bobbin diameter section of expanding arranged through pipeline, under the running status that is 0.4 m/s at flow velocity, add flocculation agent polyacrylamide sodium at its both port of origination place, maintain operation after 12 minutes, send in precipitation apparatus that to carry out solid-liquid settlement separate.0.5 hour settlement separate time.Part sediment after the sedimentation solid-liquid separation (10-30 (v) %) returns and recycles, and all the other sediment dryings are seen off.The result that adopts the present invention to improve front and back method contrasts as shown in table 4.
The sewage disposal comparative test result of table 4 embodiment 2
| Detect index | Sewage before processing | Method before improving | The inventive method |
| COD mg/l | 382 | 68.5 | 21.2 |
| BOD mg/l | 156 | 11.4 | 5.1 |
| SS mg/l | 215 | 3.0 | 2.1 |
| The solid-liquid settling time (h) | — | 1.5 | 0.5 |
embodiment 3
Press the mode of the Chinese patent embodiment 1 of notification number CN 1098813C, after the oil-containing chemical engineering sewage gradation moved in transport pipe is added to the flocculation agent aftertreatment, through vertical the first enlarged diameter section arranged, the waste water flow velocity is reduced to 0.7 m/s, after maintaining 8 minutes, send into the same vertical Second bobbin diameter section of expanding arranged through pipeline, under the running status that is 0.4 m/s at flow velocity, add the flocculation agent Walocel MT 20.000PV at its both port of origination place, maintain operation after 15 minutes, send in precipitation apparatus that to carry out solid-liquid settlement separate.0.5 hour settlement separate time.Part sediment after the sedimentation solid-liquid separation (10-30 (v) %) returns and recycles, and all the other sediment dryings are seen off.The result that adopts the present invention to improve front and back method contrasts as shown in table 5.
The sewage disposal comparative test result of table 5 embodiment 3
| Detect index | Sewage before processing | Method before improving | The inventive method |
| COD mg/l | 860 | 132.1 | 91.2 |
| BOD mg/l | 250 | 35.1 | 8.1 |
| SS mg/l | 150 | 12.3 | 3.2 |
| The solid-liquid settling time (h) | — | 2.0 | 0.5 |
embodiment 4
In the sewage disposal of above-described embodiment 1, add flocculation agent respectively under the different in flow rate condition, investigated and used the impact of flocculation agent on the sewage disposal result under different in flow rate.Flow velocity while having shown to add flocculation agent has obvious impact to the result of sewage.Test-results is as shown in table 6:
Add the impact of flocculation agent on result under table 6 different in flow rate
| Detect index | Sewage before processing | 0.2 water quality after the processing that m/s adds | 0.5 water quality after the processing that m/s adds | 0.8 water quality after the processing that m/s adds |
| COD(mg/l) | 525.0 | 32.6 | 38.5 | 55.0 |
| BOD(mg/l) | 185.0 | 7.5 | 8.8 | 15.6 |
| SS(mg/l) | 315.0 | 2.1 | 3.1 | 12.8 |
embodiment 5
In the sewage disposal of above-described embodiment 1, use respectively different types of flocculation agent, investigate the impact of different flocculation agents on the sewage disposal result.Result shows, in the situation that other condition is constant, changes the kind of flocculation agent, and to net result and do not make significant difference, the water quality after processing can reach basically identical satisfactory result.Test-results is as shown in table 7:
The impact of the different flocculation agents of table 7 on the sewage disposal result
| Detect index | Sewage before processing | After polyacrylamide is processed | After chitin is processed | After causticization starch is processed |
| COD(mg/l) | 525.0 | 35.6 | 48.5 | 42.3 |
| BOD(mg/l) | 185.0 | 8.2 | 9.8 | 9.5 |
| SS(mg/l) | 315.0 | 2.5 | 3.5 | 2.8 |
Claims (6)
1. improved physic and chemical condensation method for treatment of foulwater, under the state that sewage is moved in pipeline through pumping equipment, at least initial stage and the later stage in the sewage operation adds respectively flocculation agent in a continuous manner, make it realize mixing in the common operational process with sewage, and finally carry out sedimentation and solid-liquid separation, it is characterized in that after last adds flocculation agent and sewage in running status mixes, make the combined sewage flow rate control at 0.1 ~ 1 meter per second and at least maintain 5 minutes through buffer cell, then under the state that is 0.1 ~ 0.5 meter per second at flow velocity, after mixing with the flocculation agent added continuously and at least maintaining 10 minutes, send into the sedimentation device of solid-liquid separation.
2. the method for claim 1, is characterized in that said buffer cell is that before a diameter is greater than, the volume of sewage in-service pipeline expands target phase.
3. the method for claim 1, it is characterized in that sewage and flocculation agent be blended in a diameter be greater than before the volume of sewage in-service pipeline expand target phase.
4. the method for claim 1, is characterized in that said flocculation agent comprises polyacrylamide, chitin, causticization starch, Walocel MT 20.000PV, polyoxyethylene, polymine, polyacrylamide sodium.
5. method as described as one of claim 1 to 4, is characterized in that the sediment after solid-liquid separation in said sedimentation device, and the initial period that part is returned to sewage disposal recycles.
6. method as claimed in claim 5, it is characterized in that returning the sediment recycled is 10 ~ 30% of solid-liquid separation sediment volume total amount.
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| CN107473472A (en) * | 2017-09-29 | 2017-12-15 | 项心力 | A kind of method based on physical chemistry coacervation processing sewage |
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| CN1098813C (en) * | 1994-08-13 | 2003-01-15 | 李开春 | Physic and chemical condensation method for treatment of foulwater |
| CN1170779C (en) * | 2000-06-29 | 2004-10-13 | 李黔龙 | Process and equipment for reclaiming waste water from steam-electric power plant |
| JP3888984B2 (en) * | 2003-05-22 | 2007-03-07 | 東京都 | Sewage treatment method and equipment for combined sewers |
| DE202009017790U1 (en) * | 2009-02-27 | 2010-06-17 | Enviplan Ingenieurgesellschaft Mbh | Wastewater treatment plant for the treatment of waste water from oil crops and grain processing |
| CN202265485U (en) * | 2011-10-16 | 2012-06-06 | 杭州高博环保科技有限公司 | Multipoint commonly-cast wastewater coagulating sedimentation reaction device |
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