CN102260027A - Method for treating papermaking wastewater - Google Patents
Method for treating papermaking wastewater Download PDFInfo
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- CN102260027A CN102260027A CN 201110187863 CN201110187863A CN102260027A CN 102260027 A CN102260027 A CN 102260027A CN 201110187863 CN201110187863 CN 201110187863 CN 201110187863 A CN201110187863 A CN 201110187863A CN 102260027 A CN102260027 A CN 102260027A
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Abstract
The invention discloses a combined treatment method for ensuring papermaking wastewater to reach the high discharge standard. The problem that the papermaking wastewater is difficult to treat is solved. In the technical scheme, the method for treating the papermaking wastewater comprises the following steps that after the papermaking wastewater is subjected to deslagging, the materialization treatment is carried out; after sludge-water separation is carried out, the obtained wastewater is lifted to a PAFR (pulse anaerobic fluidized bed reactor) reactor to perform a hydrolysis acidification reaction; after hydrolysis acidification, effluent automatically flows into an improved oxidation ditch system; after being subjected to sludge-water separation, the effluent in the oxidation ditch is lifted to an advanced oxidation system; the obtained effluent is added with drug to perform a coagulation reaction and then flows into a final sedimentation tank; and supernatant fluid reaches the discharge standard. By the method, after the papermaking wastewater is treated, the CODCr (Chemical Oxygen Demand) of the effluent is less than or equal to 70mg/L and the effluent basically reaches the high industrial wastewater treatment control standard.
Description
Technical field
The present invention relates to a kind of treatment process of trade effluent high standard discharging, particularly a kind of treatment process of paper waste high standard discharging.
Background technology
Paper waste particularly pulping and paper-making factory effluent mainly embathes processing, change machine slurry middle section water, boxboard production process from raw material wood chip (or wheat straw etc.).The characteristics of waste water are that the water yield is big, SS, COD
CrAll higher, waste water B/C is lower, and biodegradability is relatively poor, belongs to one of more unmanageable trade effluent.The pollutant component complexity of waste water, contain the more stable macromolecule contaminant of a large amount of molecular structures, as difficult degradation pollutents such as xylogen, Mierocrystalline cellulose, hemicellulose and a small amount of rosin, and contain other inorganics such as organic impurity, soil particle and a small amount of toxic substance such as muriate of part.Xylogen and derivative thereof, Mierocrystalline cellulose, hemicellulose etc. are to form COD
CrAnd the main component of BOD; The main suspended solid (SS) that forms such as wood chip in small, broken bits, fiber fines, soil particle.
At present, traditional " materialization+biochemistry " treatment process of main both at home and abroad employing is handled paper waste, but its water outlet is difficult to satisfy the emission standard of increasingly stringent.Therefore, provide a kind of treatment process of paper waste high standard discharging, to overcome the shortcoming of prior art.
Summary of the invention
The treatment process that the object of the present invention is to provide that a kind of technology is simple, cost is low, efficient is high, can effectively administer paper waste.
Purpose of the present invention can realize by following technical measures:
A kind of technological process for the treatment of papermaking method, described treatment process comprises the steps:
(1) paper waste carries out the materialization processing after pre-treatment, and flow to equalizing tank certainly after the preliminary sedimentation tank mud-water separation;
(2) equalizing tank waste water is promoted to the pulse anaerobic fluidized-bed reactor acidification reaction that is hydrolyzed, and the water outlet gravity flow enters the improved oxidation ditch system behind the acidication, and the improved oxidation ditch water outlet enters the second pond mud-water separation, and water outlet is from flowing to water collecting basin; Wherein, the combination of described improved oxidation ditch system's employing " ABR reactor+Carrousel oxidation ditch ";
(3) water collecting basin waste water carries out the advanced oxidation processing after promoting, and supernatant liquor can discharge after the final deposition pool mud-water separation.
Described pulse anaerobic fluidized-bed reactor can be provided with the anti-clogging plug water distribution system.
The improved oxidation ditch system adopts the combination of " ABR reactor+Carrousel oxidation ditch ", this system is based on Carrousel oxidation ditch, be aided with the ABR reactor, not only effluent quality is good, and this system has remarkable stability, easy operational administrative and minimum maintenance workload, can effectively prevent the sludge bulking phenomenon simultaneously.
Carrousel) oxidation ditchUltimate principle stem from development to the novelty of common oxidation Ditch Technology.The shape of Carrousel oxidation ditch resembles a stadium of track and field runway, and some roads longitudinal subdivision wall is arranged in the pond.Mixing liquid is by around the surface aerating machine of vertical axes low speed rotation (25-35 rpm) and oxygenation.So fully guaranteed that blended is even, and produced an enough big horizontal flow velocity and certain turbulent flow to guarantee that mud is unlikely to sedimentation in flow process.When sewage flowed around oxidation ditch, microorganism (active sludge) can degradation of organic substances and nitrogenous dirt.When possessing good processing performance,, also can realize the optimum allocation of OXYRATOR surface aerating machine energy aspect oxygenation, plug-flow and mixing three, thereby make Carrousel oxidation ditch possess good hydraulic performance by adopting special-purpose hydraulic model and design.Because the entrance region of Carrousel oxidation ditch has complete blended waterpower fluidised form, and compare with water inlet, the section flow of channel very big (be flooding velocity 20 ~ 50 times) in the ditch, water inlet just can mix with a large amount of water in the pond in very short time fully like this, obtain dilution, thereby oxidation ditch has very strong capacity of resisting impact load, guaranteed stability and reliability that the oxidation ditch operation is handled.This processing for trade effluents such as slurrying/papermaking is particularly important, because the phenomenon of impact load occurs through regular meeting in the discharging of trade effluent.Because this characteristics of Carrousel oxidation ditch, even if under the situation of influent load fluctuation, it still can guarantee stable water flow quality.For reaching maximum flexibility of operation, preferably can regulate the power input according to actual oxygen requirement and loading condiction.And Carrousel oxidation ditch just can be regulated total oxygenation capacity by the rotating speed of regulating aerator.Actual dissolved oxygen (DO) concentration is measured by the dissolved oxygen probe that is located at the downstream, aeration zone.The result who records is sent to robot control system(RCS) (PLC, PID controller etc.), robot control system(RCS) according to DO concentration by the rotating speed of adjusting surface aerating machine the regulating and controlling oxygenation capacity.Adopt this kind mode, realized the coupling of oxygenation capacity and actual oxygen requirement, thereby saved the energy.Under the very low situation of actual oxygen requirement, can import by the part surface aerating machine being closed fully, thereby save the energy with further reduction power.
Carrousel oxidation ditch is to be proved to be a kind of very effective sewage treatment process, compares with other Sewage treatment systems, and it has following advantage: (1) pollutant removal is good; (2) construction and working cost are low, owing to adopt the surface aerating machine OXYRATOR of the inverted umbrella shaped impeller with special shape, its power efficiency of oxygen supply (2.1 ~ 2.4kgO
2/ kWh) be higher than similar surface aerating machine and other surface aeration equipment (as plate-spinning or change brush), thus energy consumption reduced, saved working cost; (3) because OXYRATOR surface aerating machine power is bigger, single device oxygenation capacity height, thereby aeration process is mainly finished by several few equipment of number.The minimizing of number of devices has not only reduced investment, and operational administrative is simple and convenient compares with the blast aeration head that inconvenience is safeguarded, surface aerating machine is sturdy and durable, stable and reliable operation; (4) in conjunction with the use of RHVC, robot control system(RCS) also can be come the regulation system oxygenation capacity by operation platform number and the rotating speed of adjusting surface aerating machine, and itself and summer in winter and the fluctuation of influent load are round the clock adapted.When guaranteeing treatment effect, further reduced energy consumption.
Prevent the sludge bulking reactor)Can solve the problem of sludge bulking effectively.When being applied to Industrial Wastewater Treatment, Carrousel oxidation ditch can obtain good treatment effect and high-quality water outlet, also finds in application process, and is the same with other treatment process, because some singularity of trade effluent, the sludge bulking phenomenon may appear in oxidation ditch.Carrousel oxidation ditch and some are prevented that the measure of sludge bulking from combining, when avoiding sludge bulking, still keep the original various advantages of Carrousel oxidation ditch.
Make discovery from observation, for industrial sewage, the sludge bulking problem is by thread microbial, and these thread funguss are to rely on the readily biodegradable composition in the sewage to survive.Adopt the preaeration of suitably design can prevent such sludge bulking.The principle of work of ABR reactor is in fact very simple.Its running status is equivalent to a complete blended perseveranceization reactor, and its hydraulic detention time (HRT) is 2-14 hour.In ABR, in the waste water easily the COD of degraded be converted into colloidal state exist can free-swimming bacterium.And under this specified conditions and environment, poky thread fungus can't survive, and its growth is subjected to very big compacting.The bacterium that freely moves about in the reactor just becomes the food of the high microorganism (protozoon and metazoan) that exists in the active sludge of follow-up aeration tank (as Carrousel oxidation ditch).One of key point of ABR reactor design is determining of hydraulic detention time (HRT).The setting of system HRT should guarantee that the COD that easily degrades in the water can fully be absorbed by the bacterium that freely moves about and utilize, thereby it can keep the growth that continues and constantly discharge system with water outlet, thread fungus is because specific growth rate is lower simultaneously, and short HRT makes it can't have the sufficient time to breed.If it is proper that HRT selects, thereby thread fungus can't survive in competition and can not cause sludge bulking.In actual motion, as the main function of ABR, it offsets except that the intumescent effect of mud and has obtained sufficient proof.
In sum, for containing a large amount of readily biodegradable COD compositions and causing the industrial technological process for the treatment of papermaking of sludge bulking easily, adopting the combination of ABR reactor+Carrousel is a kind of extraordinary mode.From on the one hand, the employing of ABR reactor can effectively prevent the sludge bulking phenomenon and bring many benefits (as the minimizing of cubic capacity and excess sludge production, and removing sulphur in the sewage effectively) for treatment process; From another point of view, the lot of advantages of Carrousel is all kept, and is strengthened by the employing of ABR.The plurality of advantages of ABR and Carrousel oxidation ditch is added altogether, just formed ABR-Carrousel technology, both advantages bring out the best in each other in this technology, have fully guaranteed good treatment effect.
As the preferred implementation of technological process for the treatment of papermaking method of the present invention, in the described Wastewater Pretreatment, comprise waste water quality, the water yield, pH value and temperature are regulated, and the suspended substance in the removal waste water.
As the preferred implementation of technological process for the treatment of papermaking method of the present invention, the described pulse anaerobic fluidized-bed reactor residence time is 12 ~ 25h, and the improved oxidation ditch system residence time is 12 ~ 22h.
As the more preferably embodiment of technological process for the treatment of papermaking method of the present invention, the described pulse anaerobic fluidized-bed reactor residence time is 18h, and the AB section residence time is 4.2h, and the improved oxidation ditch residence time is 18h.
As the preferred implementation of technological process for the treatment of papermaking method of the present invention, described advanced oxidation processing comprises the adjustment waste water ph, adds Fenton reagent, adds alkali lye, adds polymerize aluminum chloride and polyacrylamide.
As the more preferably embodiment of technological process for the treatment of papermaking method of the present invention, adjusting waste water ph during described advanced oxidation is handled is 4.0 ~ 7.0.As the most preferred embodiment of technological process for the treatment of papermaking method of the present invention, adjusting waste water ph during described advanced oxidation is handled is 5.0.
As the more preferably embodiment of technological process for the treatment of papermaking method of the present invention, add Fenton reagent during described advanced oxidation is handled and be meant by H
2O
2With COD
CrWeight ratio is that 1.25 ~ 3.00:1 adds H
2O
2, and then press H
2O
2/ Fe
2+Mol ratio is that 1:4.5 ~ 15.5 add Fe
2+Solution.As the most preferred embodiment of technological process for the treatment of papermaking method of the present invention, the H that described advanced oxidation adds in handling
2O
2With COD
CrWeight ratio be 2.00:1, H
2O
2/ Fe
2+Mol ratio is 1:6.5.
As the preferred implementation of technological process for the treatment of papermaking method of the present invention, the oxidation time that described advanced oxidation is handled is 2 ~ 8min.As the more preferably embodiment of technological process for the treatment of papermaking method of the present invention, the oxidation time that described advanced oxidation is handled is 4min.
Compare with conventional art, combination treatment method by the discharging of a kind of paper waste high standard of the present invention has solved paper waste and has been difficult to a difficult problem up to standard, and paper waste has reached higher Industrial Wastewater Treatment control criterion after the combination treatment method of described high standard discharging is handled.And paper waste can enter biochemical system and carry out biochemical treatment after materialization is handled, temperature of reaction, nutrilite etc. is not had particular requirement, can not produce by product simultaneously, can not pollute environment.The treatment process that present method is that a kind of cost is low, efficient is high, can effectively administer paper waste.
Description of drawings
The invention will be further described to utilize accompanying drawing, but the embodiment in the accompanying drawing does not constitute any limitation of the invention.
Fig. 1 is the schematic flow sheet of technological process for the treatment of papermaking method of the present invention.
Embodiment
For making the present invention easier to understand, will further set forth specific embodiments of the invention below.
A kind of combination treatment method of paper waste high standard discharging is handled paper waste, and this method may further comprise the steps:
(1) paper waste carries out the materialization processing after pre-treatment, and flow to equalizing tank certainly after the preliminary sedimentation tank mud-water separation;
(2) equalizing tank waste water is promoted to the PAFR reactor acidification reaction that is hydrolyzed, and the water outlet gravity flow enters the improved oxidation ditch system behind the acidication, and the oxidation ditch water outlet enters the second pond mud-water separation, and water outlet is from flowing to water collecting basin;
(3) water collecting basin waste water enters the advanced oxidation system and carries out advanced oxidation and handle after promoting, and supernatant liquor gets final product qualified discharge after the final deposition pool mud-water separation.
In step (1), carry out the materialization processing after the paper waste pre-treatment and be meant that paper waste flows into coagulation reaction tank after pre-treatment, add polymerize aluminum chloride (PAC) and polyacrylamide (PAM), enter preliminary sedimentation tank subsequently and carry out mud-water separation, settling tank water outlet gravity flow enters the adjusting that equalizing tank carries out water quality, the water yield and water temperature etc.
In step (2), described paper waste is promoted to PAFR reactor (pulse anaerobic fluidized-bed reactor) acidification reaction that is hydrolyzed is meant the pulse water distribution device that waste water is promoted to the PAFR reactor head, waste water enters the reaction of PAFR reactor generation acidication through the pulse water distribution.The water outlet of PAFR reactor is handled from flowing into the improved oxidation ditch system, and the improved oxidation ditch system adopts the combination of " ABR reactor+Carrousel oxidation ditch ".The oxidation ditch water outlet enters second pond and carries out mud-water separation, and water outlet is from flowing to water collecting basin.
Contain a large amount of paper pulp fibers in the paper waste, through after the pre-treatment, still can inevitably have tiny fiber of part and bigger impurity to enter the PAFR reactor, as bag film, cloth etc., these impurity cause water distributing pore to stop up easily.Because water distribution system is installed in the PAFR reactor bottom, and the PAFR reactor is a closed structure, and clear and coherent water distribution system need expend bigger human and material resources.For solving this difficult problem, we have improved the structure of water distribution system according to the experience of a plurality of engineerings, increase hydraulic reverse towards Residue extraction pipeline, make water distribution system have good anti-clogging plug function, also can be by easy operation mediation water distributor even if stop up.The anti-clogging plug water distribution system is to sum up improvement according to the PAFR reactor water distribution system running condition of the structure of PAFR reactor, hydraulic model and a plurality of paper waste treatment project to draw.In water distribution system in the past, stop up the end that usually occurs in water distributor, the impurity of obstruction is bag film, cloth etc.We are at the terminal recoil scum pipe that increases of water distributor, during pulse water distribution device pulsing impurity is dashed to scum pipe, open the recoil slag-discharging valve then, utilizing high-order hydraulic pressuring difference that the interior waste water of PAFR reactor is entered in the water distributor by the water distributor water hole recoils, enter the recoil scum pipe subsequently and together impurity is taken out of, finish the recoil tapping process thus.Whole recoil tapping process only needs to carry out the unlatching of valve, very easy of operation, and the recoil deslagging is effective.
Security personnel's screen cloth of anti-clogging plug water distribution system and pulse water distribution device has been formed the anti-clogging plug double insurance of PAFR reactor, has improved the continuous reliability of operation of PAFR reactor greatly.
In step (2), the residence time of PAFR reactor is 18h in the present embodiment; The residence time of Carrousel oxidation ditch is adopted 18h, and the ABR reactor is 1:4.3 with the residence time ratio of Carrousel oxidation ditch, so determine that the residence time of ABR reactor in the present embodiment is 4.2h.
In step (3), water collecting basin waste water enters the advanced oxidation pond after promoting, and to wherein adding Fenton reagent, Fenton reagent is by H after adjusting pH
2O
2And ferrous compound combines H in the finite concentration ratio
2O
2At Fe
2+Katalysis decompose down and produce OH, oxidation operation is resolved into small-molecule substances such as carbonic acid gas and water by approach such as transfer transports, thereby reaches the purpose of removing pollutent in the waste water.Simultaneously, Fe
2+Be oxidized to Fe
3+Produce coagulating sedimentation, and can adsorb the removal large amount of organic.The waste water gravity flow enters final deposition pool, adds alkali lye and polymerize aluminum chloride (PAC), polyacrylamide (PAM) in the pond, forms a large amount of alumen ustum, enter precipitating phase, mud precipitates at this, by the scraping and sucking machine sucking-off, is pumped to the sludge thickener of Waste Water Treatment then.Final deposition pool water outlet qualified discharge.
In step (3), pre-treatment is carried out in water outlet behind the biochemistry, the pH value of promptly adjusting waste water is 4.0 ~ 7.0.
The described Fenton of utilization reagent carries out advanced oxidation to waste water to be handled, and promptly adds Fe in waste water
2+Solution and H
2O
2,Fe wherein
2+Solution is FeSO
4Solution.H
2O
2Concentration be generally 25% ~ 30%, be preferably 27.5%.
Further improvement in the technical proposal is H in the described advanced oxidation reaction
2O
2/ COD
Cr(g/g) (weight ratio) is 1.25-2.25, is preferably 2; H
2O
2/ Fe
2+(mol/mol)=and 1:4.4 ~ 15.5, be preferably 1:6.5.
In the present invention, FeSO
4Solution is used other instead and is contained Fe
2+Solution also can use, but effect is poor slightly.
In the present invention, described pretreated waste water ph scope is 4.0 ~ 7.0, and preferred pH value scope is 5.0 ~ 6.0.
In one embodiment of the invention, further comprise and to detect the step of discharging then through the trade effluent after the combined treatment technical finesse of paper waste high standard discharging, this step mainly is the pollutent index of measuring in the water sample, to check this technology to the processing of described waste water situation up to standard.
In the present invention, all there is certain influence residence time of the water quality of paper waste, the water yield, pH value, temperature and structures etc. to pollutants removal rate in the waste water.Below estimate its corresponding incidence relation by specific embodiment.
Table 1 has characterized the hydraulic detention time of PAFR reactor to COD
CrClearance also has certain influence.Under the normal temperature condition, materialization adds dose before the control, and waste water is raised and enters the PAFR reactor after the preliminary sedimentation tank mud-water separation, measures the pollutent index of PAFR reactor water outlet behind different hydraulic detention times, and the result is as shown in table 1.
The table 1 PAFR reactor waterpower residence time is to COD
CrThe influence of clearance
| PAFR reactor residence time (h) | Water outlet COD Cr mg/L | COD CrClearance |
| 12 | 1177.4 | 21.5% |
| 15 | 1035.1 | 31.0% |
| 18 | 825.0 | 45.0% |
| 20 | 798.8 | 46.7% |
| 22 | 794.2 | 47.1% |
| 25 | 785.9 | 47.6% |
The result shows, along with the increase of PAFR reactor residence time, COD
CrClearance progressively increases, and particularly works as the PAFR reactor residence time and increases to 18h from 12h, COD
CrClearance rises apparent in view, rises to 45.0% from 21.5%; But when the PAFR reactor residence time increases to 18h when above, COD
CrClearance tends towards stability substantially, and therefore, PAFR reactor most optimal retention time is 18h.
Table 2 has characterized the hydraulic detention time of oxidation ditch system to COD
CrClearance also has certain influence.Under the normal temperature condition, materialization adds dose before the control, and the PAFR reactor residence time is 18h, and the water outlet of PAFR reactor enters the improved oxidation ditch system, measures the pollutent index of oxidation ditch system water outlet behind different hydraulic detention times, and the result is as shown in table 2.
Table 2 oxidation ditch hydraulic detention time is to COD
CrThe influence of clearance
| The oxidation ditch residence time (h) | Water outlet COD Cr mg/L | COD CrClearance |
| 12 | 505.1 | 38.8% |
| 15 | 424.6 | 48.5% |
| 18 | 280.3 | 66.0% |
| 20 | 261.7 | 68.3% |
| 22 | 253.9 | 69.2% |
The result shows, along with the increase of the oxidation ditch residence time, COD
CrClearance progressively increases, and particularly increases to 18h from 12h, COD when the residence time
CrClearance rises apparent in view, rises to 66.0% from 38.8%; But increase to 18h when above when the anaerobism residence time, COD
CrClearance tends towards stability substantially, and therefore, the oxidation ditch most optimal retention time is 18h.The AB section mainly is the effect of denitrogenation, dephosphorization, and its most optimal retention time is 4.2h.
Table 3 has characterized the advanced oxidation section H
2O
2Dosage is to COD
CrThe influence of clearance.Work as pH=5.0, normal temperature condition adds H
2O
2/ Fe
2+(mol/mol)=and 1:6.5, react after 4 minutes, measure the COD of water sample
Cr, the result is as shown in table 3.
Table 3 H
2O
2Dosage is to COD
CrThe influence of clearance
| H 2O 2/COD Cr （g/g） | Water outlet COD Cr? mg/L | COD CrClearance |
| 1.25 | 115.5 | 60.2% |
| 1.50 | 89.1 | 69.3% |
| 2.00 | 61.0 | 79.0% |
| 2.50 | 56.8 | 80.4% |
| 3.00 | 52.6 | 81.9% |
This shows, when preparation Fenton reagent, H
2O
2Dosage and COD
CrClearance certain cognation is arranged.Along with H
2O
2/ COD
Cr(g/g) increase of (weight ratio), COD
CrClearance rises apparent in view, rises to 79.0% from 60.2%; But work as H
2O
2/ COD
Cr(g/g) (weight ratio) increases to after 2.00, COD
CrClearance increase beginning slowly, therefore, in most preferred embodiment of the present invention, H
2O
2/ COD
Cr(weight ratio) value is 2.00 for best dosage.
Table 4 has characterized advanced oxidation reactive moieties H
2O
2With Fe
2+Add the comparison COD
CrThe influence of clearance.Work as pH=5.0, under normal temperature condition, add H
2O
2/ COD
Cr(g/g)=2.00, the reaction times is 4 minutes, measures the COD of water sample
Cr, the result is as shown in table 4.
Table 4 Fe
2+Dosage is to COD
CrThe influence of clearance
| H 2O 2/Fe 2+? (mol/mol) | Water outlet COD Crmg/L | COD CrClearance |
| 1:4.5 | 97.5 | 66.4% |
| 1:6.5 | 67.3 | 76.8% |
| 1:8.5 | 62.1 | 78.6% |
| 1:10.5 | 60.8 | 79.0% |
| 1:12.5 | 57.7 | 80.1% |
| 1:15.5 | 56.9 | 80.4% |
This shows, when preparation Fenton reagent, H
2O
2With Fe
2+Add the comparison COD
CrClearance certain cognation is arranged.Work as H
2O
2/ Fe
2+(mol/mol) value is 1:4.5 ~ 6.5, COD
CrClearance rise comparatively fast, rise to 76.8% from 66.4%; But work as H
2O
2/ Fe
2+(mol/mol) value rises to 1:6.5 when above, COD
CrClearance basicly stable.In most preferred embodiment of the present invention, H
2O
2/ Fe
2+(mol/mol) value is that the best adds ratio for 1:6.5.
The pH value of waste water was to COD when table 5 had characterized advanced oxidation
CrThe influence of clearance.Under normal temperature condition, add H
2O
2/ Fe
2+(mol/mol) value is 1:6.5, H
2O
2/ COD
Cr(g/g)=2.00, the reaction times is 4 minutes, measures the COD of water sample
Cr, the result is as shown in table 5.
Table 5 pH value is to COD
CrThe influence of clearance
| The pH value | Water outlet COD Cr? mg/L | COD CrClearance |
| 3.0 | 58.5 | 79.8% |
| 4.0 | 60.5 | 79.1% |
| 5.0 | 63.0 | 78.3% |
| 6.0 | 67.3 | 76.8% |
| 7.0 | 69.8 | 75.9% |
This shows that under these conditions, the pH value is to COD
CrThe influence of clearance is little, in most preferred embodiment of the present invention, considers the problem of pH regulator expense and treatment effect, and getting the best adjusted value of pH is 5.0.
Table 6 has characterized the advanced oxidation reaction times to COD
CrClearance also has certain influence.At pH=5.0, under the condition of normal temperature, add H
2O
2/ Fe
2+(mol/mol) be 1:6.5, H
2O
2/ COD
Cr(g/g)=2.00 o'clock, the different reaction times is measured the COD of water sample down
Cr, the result is as shown in table 6.
Table 6 reaction times is to COD
CrThe influence of clearance
| Time (min) | Water outlet COD Cr mg/L | COD CrClearance |
| 2 | 90.7 | 68.7% |
| 3 | 75.6 | 73.9% |
| 4 | 64.0 | 77.9% |
| 6 | 61.9 | 78.7% |
| 8 | 60.1 | 79.3% |
The result shows, along with the increase in reaction times, COD
CrClearance progressively increases, after being reacted to 4 minutes, and COD
CrClearance tends towards stability substantially, and therefore, optimum reacting time is 4 minutes.
Evaluation temperature changes COD
CrThe influence of clearance.When reaction conditions is: pH=5.0 adds H
2O
2/ Fe
2+(mol/mol) 1:6.5, H
2O
2/ COD
Cr(g/g)=2.00, the COD of water sample is measured in reaction after 4 minutes
Cr, COD as a result
CrClearance fluctuates about 78.5%, and amplitude very little (fluctuation range is in 1%) illustrates that thus temperature variation is to COD
CrThe influence of clearance is very little.Variation of temperature influences not quite the end reaction result, but speed of response is had certain influence.Along with the rising of temperature, speed of response is accelerated gradually, but the range of temperature of considering pending waste water is not obvious to the influence of speed of response about 10 ℃.
Verified that by above embodiment the present invention is a kind of combination treatment method of paper waste high standard discharging, the residence time of each structures of Waste Water Treatment, advanced oxidation water inlet pH value, H
2O
2With Fe
2+Add dose and dosing ratio, reaction times etc. and COD
CrClearance all has certain cognation, below is preferred suitable reaction conditions:
PAFR reactor most optimal retention time is 18h;
AB section most optimal retention time is 4.2h, and the oxidation ditch most optimal retention time is 18h;
H
2O
2/ COD
Cr(weight ratio) value is 2.00 for best dosage;
H
2O
2/ Fe
2+(mol/mol) value is that the best adds ratio for 1:6.5;
PH value=5.0 o'clock, COD
CrThe clearance effect is best;
Optimum reacting time is 4 minutes.
Combination treatment method by described high standard discharging is handled paper waste, and water outlet can reach table 7 standard.And paper waste can enter biochemical system and carry out biochemical treatment after materialization is handled, temperature of reaction, nutrilite etc. is not had particular requirement, can not produce by product simultaneously, can not pollute environment.The treatment process that present method is that a kind of cost is low, efficient is high, can effectively administer paper waste.
Table 7 Passing Criteria (unit: except mg/L pH, the colourity)
| Project | Emission standard | Project | Emission standard |
| COD Cr | ≤70 | Colourity (extension rate) | ≤30 |
| BOD 5 | ≤20 | pH | 6～9 |
| SS | ≤30 | ? | ? |
Last institute should be noted that; above embodiment is only in order to illustrate technical scheme of the present invention but not limiting the scope of the invention; although the present invention has been done detailed description with reference to preferred embodiment; those of ordinary skill in the art is to be understood that; can make amendment or be equal to replacement technical scheme of the present invention, and not break away from the essence and the scope of technical solution of the present invention.
Claims (11)
1. a technological process for the treatment of papermaking method is characterized in that, described treatment process comprises the steps:
(1) paper waste carries out the materialization processing after pre-treatment, and flow to equalizing tank certainly after the preliminary sedimentation tank mud-water separation;
(2) equalizing tank waste water is promoted to the pulse anaerobic fluidized-bed reactor acidification reaction that is hydrolyzed, and the water outlet gravity flow enters the improved oxidation ditch system behind the acidication, and the improved oxidation ditch water outlet enters the second pond mud-water separation, and water outlet is from flowing to water collecting basin; Wherein, the combination of described improved oxidation ditch system's employing " ABR reactor+Carrousel oxidation ditch ";
(3) water collecting basin waste water carries out the advanced oxidation processing after promoting, and supernatant liquor can discharge after the final deposition pool mud-water separation.
2. technological process for the treatment of papermaking method according to claim 1 is characterized in that, in the described Wastewater Pretreatment, comprises waste water quality, the water yield, pH value and temperature regulated, and the suspended substance in the removal waste water.
3. technological process for the treatment of papermaking method according to claim 1 is characterized in that, the described pulse anaerobic fluidized-bed reactor residence time is 12 ~ 25h, and the improved oxidation ditch system residence time is 12 ~ 22h.
4. technological process for the treatment of papermaking method according to claim 3 is characterized in that, the described pulse anaerobic fluidized-bed reactor residence time is 18h, and the AB section residence time is 4.2h, and the improved oxidation ditch residence time is 18h.
5. technological process for the treatment of papermaking method according to claim 1 is characterized in that, described advanced oxidation processing comprises the adjustment waste water ph, adds Fenton reagent, adds alkali lye, adds polymerize aluminum chloride and polyacrylamide.
6. technological process for the treatment of papermaking method according to claim 5 is characterized in that, adjusting waste water ph during described advanced oxidation is handled is 4.0 ~ 7.0.
7. technological process for the treatment of papermaking method according to claim 6 is characterized in that, adjusting waste water ph during described advanced oxidation is handled is 5.0.
8. technological process for the treatment of papermaking method according to claim 5 is characterized in that, adds Fenton reagent during described advanced oxidation is handled and is meant by H
2O
2With COD
CrWeight ratio is that 1.25 ~ 3.00:1 adds H
2O
2, and then press H
2O
2/ Fe
2+Mol ratio is that 1:4.5 ~ 15.5 add Fe
2+Solution.
9. technological process for the treatment of papermaking method according to claim 8 is characterized in that, the H that described advanced oxidation adds in handling
2O
2With COD
CrWeight ratio be 2.00:1, H
2O
2/ Fe
2+Mol ratio is 1:6.5.
10. technological process for the treatment of papermaking method according to claim 5 is characterized in that, the oxidation time that described advanced oxidation is handled is 2 ~ 8min.
11. technological process for the treatment of papermaking method according to claim 10 is characterized in that, the oxidation time that described advanced oxidation is handled is 4min.
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| CN102765849A (en) * | 2011-05-05 | 2012-11-07 | 天津广聚源纸业有限公司 | Deep treatment method of papermaking wastewater |
| CN103183449A (en) * | 2011-12-28 | 2013-07-03 | 王炜 | Technology for processing sulfate method pulping waste water into reclaimed water for reuse |
| CN103214078A (en) * | 2012-12-24 | 2013-07-24 | 华泰集团有限公司 | New use of coal ash in Fenton method sewage process, and papermaking wastewater treatment process adopting the use |
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| CN103183449B (en) * | 2011-12-28 | 2016-05-11 | 上海洗霸科技股份有限公司 | Water reuse treatment process in sulfate pulping waste water |
| CN103214078A (en) * | 2012-12-24 | 2013-07-24 | 华泰集团有限公司 | New use of coal ash in Fenton method sewage process, and papermaking wastewater treatment process adopting the use |
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| CN104556578A (en) * | 2015-02-13 | 2015-04-29 | 山东新时代药业有限公司 | Method for deep treatment of wastewater |
| CN104556578B (en) * | 2015-02-13 | 2019-01-29 | 山东新时代药业有限公司 | A kind of deep treatment method of waste water |
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