CN102329050B - Process and device for efficiently treating wheat straw pulp intermediate wastewater by alkaline method - Google Patents
Process and device for efficiently treating wheat straw pulp intermediate wastewater by alkaline method Download PDFInfo
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- CN102329050B CN102329050B CN 201110248385 CN201110248385A CN102329050B CN 102329050 B CN102329050 B CN 102329050B CN 201110248385 CN201110248385 CN 201110248385 CN 201110248385 A CN201110248385 A CN 201110248385A CN 102329050 B CN102329050 B CN 102329050B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000010902 straw Substances 0.000 title claims abstract description 31
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- 235000021307 Triticum Nutrition 0.000 title claims abstract description 9
- 230000003647 oxidation Effects 0.000 claims abstract description 41
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 41
- 238000004062 sedimentation Methods 0.000 claims abstract description 27
- 230000001112 coagulating effect Effects 0.000 claims abstract description 20
- 239000000126 substance Substances 0.000 claims abstract description 19
- 230000000694 effects Effects 0.000 claims abstract description 12
- 239000010802 sludge Substances 0.000 claims abstract description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000001301 oxygen Substances 0.000 claims abstract description 6
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 238000005189 flocculation Methods 0.000 claims description 24
- 230000016615 flocculation Effects 0.000 claims description 23
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 22
- 238000005516 engineering process Methods 0.000 claims description 20
- 238000005273 aeration Methods 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 16
- 239000000701 coagulant Substances 0.000 claims description 15
- 239000003513 alkali Substances 0.000 claims description 14
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 12
- 229920002401 polyacrylamide Polymers 0.000 claims description 12
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 10
- 230000015556 catabolic process Effects 0.000 claims description 10
- 238000006731 degradation reaction Methods 0.000 claims description 10
- 239000010865 sewage Substances 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 10
- 239000012028 Fenton's reagent Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 230000008021 deposition Effects 0.000 claims description 9
- 238000006386 neutralization reaction Methods 0.000 claims description 9
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 8
- 238000005276 aerator Methods 0.000 claims description 7
- 238000002203 pretreatment Methods 0.000 claims description 7
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 241000196324 Embryophyta Species 0.000 claims description 5
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 5
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 5
- 230000002906 microbiologic effect Effects 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000003153 chemical reaction reagent Substances 0.000 claims description 4
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 4
- 239000011790 ferrous sulphate Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 4
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 4
- 239000002957 persistent organic pollutant Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 3
- 239000003403 water pollutant Substances 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 description 12
- 229920005610 lignin Polymers 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 229920002488 Hemicellulose Polymers 0.000 description 3
- 238000004061 bleaching Methods 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- -1 hydroxyl radical free radical Chemical class 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229920001131 Pulp (paper) Polymers 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
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- 125000003118 aryl group Chemical group 0.000 description 2
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- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
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- 208000032170 Congenital Abnormalities Diseases 0.000 description 1
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Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a process and equipment for efficiently treating wheat straw pulp intermediate wastewater by an alkaline method. The process comprises the following four steps: carrying out pretreatment, pre-oxidation, aerobic biological treatment and coagulating sedimentation on wastewater so that effluent reaching standard is discharged. According to the invention, a combined process comprising pretreatment, Fenton pre-oxidation, aerobic biological treatment and coagulating sedimentation is adopted, the treatment equipment has simple structure, high efficiency and good treatment effect, and is stable to operate; total CODCr (chemical oxygen demand Cr) removal rate is up to 95-97%, and total chroma removal rate reaches 95-99%; cost is low, thus energy is saved by above 40%; and the yield of sludge is less, thereby saving sludge treatment cost. By the treatment with the process and equipment, the final effluent can stably reach the requirement of 'water pollutant emission standard in pulp-producing paper-making industry (GB3544-2008)'.
Description
Technical field
The invention belongs to field of waste water treatment, be specifically related to a kind of technology and device of handling the Straw Pulp middle-stage wastewater.
Background technology
The papermaking material structure of China changed in recent years, and the ratio of lumber fibre and secondary stock is increasing.But according to the practical situation of China, non-wood material is still the important paper making raw material of China in the long time.Quantity with wheat straw and straw in numerous non-wood-fiber resources is maximum, accounts for the 65-75% of non-wood-fiber resource.China's Straw Pulp also adopts the CEH bleaching mostly at present, namely use traditional chlorine bleaching agents such as chlorine, hypochlorite that paper pulp is bleached, lignin chlorination degraded products a large amount of in the bleaching process enter in the waste water, contain a large amount of adsorbable organic chlorides (AOX) that hypertoxicity is arranged in the bleaching effluent to making, water body is caused severe contamination.AOX has carinogenicity, to distortion property, to birth defect, multiple cranial nerve pathology and anxious toxicity.Because these material major parts have not metabolizability, unusual difficult for biological degradation, thereby hazardness is very big." pulp and paper industry pollution discharge standard " promulgation (GB3544-2008) has added sternly the emission limit of the conventional pollutent index of paper-making effluent, has replenished the AOX index.Stipulated in the standard that from July 1st, 2011 enterprises in pulp and paper industry workshop or production facility discharge of wastewater mouth AOX emission limit are 12 mg/L.
Contain a large amount of lignins, hemicellulose, carbohydrate, chlorinated lignin and other leachables (residual alkali, inorganic salt, volatile acid, ammonia, chlorine etc.) in the Straw Pulp middle-stage wastewater, complicated component, and wastewater discharge is big, and every production 1t paper pulp produces 80m approximately
3Waste water.Straw Pulping Middle Stage Waste Water BOD
5/ COD
Cr=0.25 ~ 0.30, biodegradable is relatively poor.
At present, Straw Pulp middle-stage wastewater conventional processing technology mainly is the technology of " materialization+aerobic+advanced treatment ", and namely the Straw Pulp middle-stage wastewater is handled the COD that removes most of SS and non-solubility through materialization after pre-treatment
CrAfter, further remove COD through aerobic biological process for treating
CrAnd BOD
5, remove the COD of difficult degradation then through advanced treatment
CrWith reach discharging standards after the colourity.Because Straw Pulp middle-stage wastewater COD
CrConcentration is higher, generally at 2500 ~ 3500mg/L, handle to very difficult below the 100mg/L of discharging standards requirement, mainly being by adding a large amount of chemical agents and consuming a large amount of power---blast aeration could guarantee that sewage is up to standard, current consumption is big, processing cost is high and produce a large amount of chemical sludges, dispose difficulty, easily cause secondary pollution.Especially AOX concentration is big in the Straw Pulp middle-stage wastewater, about 45 ~ 90mg/L, bio-degradable is poor, and application of active mud method could degrade 30% through 20 days processing, could degrade 45% through 50 days processing, so the clearance of the AOX in the conventional treatment method waste water is extremely low.
" the pulp and paper industry pollution discharge standard " that plays new enforcement July 1 this year is (GB3544-2008) more strict to the requirement of papermaking enterprise water pollutant emission limit.Use conventional process Straw Pulp middle-stage wastewater COD
CrClearance low, the AOX clearance is extremely low, cost is high and energy consumption is high.Therefore a kind of novel process and device that the Straw Pulp middle-stage wastewater is handled that be suitable for need be provided, replace tradition " materialization+aerobic+advanced treatment " technology to improve the COD of system
CrClearance, energy efficient, reduce production costs, make simultaneously that AOX reaches the emission standard requirement in the waste water, realize the reliable standard emission of waste water.
Summary of the invention
The deficiency low at Straw Pulp middle-stage wastewater traditional treatment method CODCr clearance, that the AOX clearance is extremely low, cost is high and energy consumption is high the purpose of this invention is to provide that a kind of running cost is low, energy consumption is low, COD
CrHigh and can remove AOX, waste water treatment process and device that sludge yield is little with chroma removal rate.
The solution of the present invention is: a kind of technology of efficient processing alkaline wheat straw pulp middle-stage wastewater, and step is as follows:
(1) pre-treatment of waste water: than the suspended substance that floats of Da Yi block pumps and pipeline, recovery fully utilizes than macrofiber in the removal waste water;
(2) pre-oxidation treatment: to 3-5, under the effect of Fenton reagent, organism is decomposed pretreated waste water with acid for adjusting pH, and removes most COD
CrAnd colourity, water outlet adds alkali and regulates pH to 6-7, removes the suspended substance in the waste water then under the effect of coagulant aids, finishes the pre-oxidation treatment process after the solid-liquid separation;
(3) aerobe is handled: waste water is removed majority of organic pollutants in the water through absorption, oxidation, the Degradation of aerobic microbiological, and mud-water separation is carried out in water outlet;
(4) coagulating sedimentation is handled: adding flocculation agent and coagulant aids fully mix in the waste water, further remove residual COD
CrBehind SS, carry out solid-liquid separation, the water outlet qualified discharge.
Foregoing technology, preferred scheme is, the described acid of step (2) is the vitriol oil (preferred sulfuric acid concentration is 96-99%, more preferably 98%); Preferably, the described alkali of step (2) is caustic soda; Preferably, step (2) pre-oxidation treatment retention time of sewage is 90 ~ 120min(more preferably 100 ~ 110min).
Foregoing technology, preferred scheme is that the described Fenton reagent of step (2) is by H
2O
2And Fe
2+Form described H
2O
2Dosage is that 80 ~ 120mg/L(preferred mass concentration is 30% H
2O
2), described Fe
2+Adopt ferrous sulfate (to be preferably FeSO
47H
2O reagent, purity are analytical pure), dosage is by 300 ~ 400mg/L.
Foregoing technology, preferred scheme is, described coagulant aids is polyacrylamide, and its dosage is that 1 ~ 2mg/L(is preferred 1.2 ~ 1.8mg/L) in step (2), and its dosage is 2 ~ 3mg/L(preferred 2.5 ~ 2.8mg/L) in step (4).
Foregoing technology, preferred scheme is, the described flocculation agent of step (4) be polymerize aluminum chloride (preferred, dosage be 80 ~ 100mg/L) or bodied ferric sulfate (preferred, dosage is 80 ~ 100mg/L).
The present invention also provides and has realized the efficient device of handling alkaline wheat straw pulp middle-stage wastewater technology, mainly comprise pretreatment unit, Fenton preoxidation device, aerobic treatment device and coagulating sedimentation treatment unit, described pretreatment unit, Fenton preoxidation device, aerobic treatment device are linked to each other by pipeline in turn with the coagulating sedimentation treatment unit.
Foregoing device, preferably scheme is, and described pretreatment unit mainly comprises fine fack, water collecting basin and oblique net, and described fine fack, water collecting basin and oblique net are linked to each other by pipeline in turn.
Foregoing device, preferred scheme is that described Fenton preoxidation device mainly comprises pH regulator pond, Fenton oxidation pond, neutralization tank and the preliminary sedimentation tank that is linked to each other by pipeline in turn.Preferably, described pH regulator pond also links to each other with vitriol oil storage tank, and described Fenton oxidation pond also is connected with FeSO
4Dosing pond and H
2O
2Storage tank, described neutralization tank also link to each other with the alkali lye chemicals dosing plant.
Foregoing device, preferred scheme is, described aerobe treatment unit mainly comprises aeration tank and second pond, described aeration tank and second pond are in turn by pipe connection, be provided with aerator in the described aeration tank, aerator links to each other with gas blower, and (preferred, the technical parameter of described aeration tank control is: MLSS concentration 2.5 ~ 3g/L, dissolved oxygen concentration 2 ~ 4mg/L, sludge loading 0.15 ~ 0.3kgCOD
Cr/ (kgMLSSd).
Foregoing device, preferably scheme is, described coagulating sedimentation device mainly comprises flocculation tank and final deposition pool, and described flocculation tank is linked to each other by pipeline in turn with final deposition pool, described flocculation tank is divided into mixing pit and reaction tank two portions, described mixing pit and reaction tank bottom UNICOM.
The treatment process of a kind of Straw Pulp middle-stage wastewater provided by the invention comprises following step in sequence:
1, pre-treatment: at first the Straw Pulp middle-stage wastewater through fine fack remove than Da Yi block pumps and pipeline float suspended substance after enter water collecting basin, be promoted to oblique net by pump then, reclaim in the waste water than macrofiber, comprehensive utilization.
2, Fenton pre-oxidation treatment: pretreated Straw Pulp middle-stage wastewater enters in the Fenton pre-oxidation treatment device, H
2O
2Oxygenant is at Fe
2+Generate hydroxyl radical free radical OH under the effect of catalyzer, hydroxyl radical free radical OH and organism reaction, make organic matter degradation, simultaneously hydroxyl radical free radical OH can after join on phenyl ring, aromatic nucleus or the heterocycle, phenyl ring, aromatic nucleus or heterogeneous ring compound are degraded into the not too big chain type organic compound of molecular weight, make its readily biodegradable.Therefore Fenton reagent can be the small organic molecule of easily degrading with the oxidation operation of difficult degradations such as lignin, hemicellulose, AOX in the waste water.
Removing most COD in waste water
CrWith colourity and the Fenton pre-oxidation treatment of finishing waste water after improving the biodegradability of waste water.Its principle can be used following chemical formulation:
In addition, as the Fe of catalyzer
2+Finally be oxidized to Fe
3+, under certain pH value, the Fe of generation (OH)
3Colloid is a kind of good flocculation agent, can remove suspended substance in the waste water by throwing out.
3, aerobe is handled: the waste water after the Fenton oxidation enters the aerobe treatment unit, at first in the aeration tank, carry out described aerobe under the acting in conjunction of the oxygen of carrying by the aerobic microbiological in the active sludge and aerator and handle, waste water carries out solid-liquid separation in second pond then.Waste water aerobic sludge after the solid-liquid separation in second pond after aerobe is handled, wherein a part is back to the aeration tank in and proceeds described aerobe processing after waste water after the Fenton preoxidation mixes.MLSS concentration is 2.5 ~ 3.5g/L in the described aeration tank, and dissolved oxygen concentration is 2 ~ 4mg/L, and sludge loading is 0.15 ~ 0.3kgCOD
Cr/ (kgMLSSd).
4, coagulating sedimentation is handled: the second pond water outlet enters the coagulating sedimentation treatment unit and carries out advanced treatment, at first entering flocculation tank, add flocculation agent and coagulant aids and fully mix, residual COD is further removed in effects such as the cloth of beating through charge neutrality, adsorption bridging and the volume of flocculation agent and coagulant aids
CrBehind SS, after entering settling tank and carrying out solid-liquid separation, the water outlet qualified discharge.
Straw Pulp middle-stage wastewater treatment process of the present invention and treatment facility have following advantage:
1. waste water treatment process of the present invention adopts the process integration of " pre-treatment+Fenton preoxidation+aerobe processing+coagulating sedimentation is handled ", and treatment facility is simple in structure, stable, efficient is high, treatment effect is good, COD
CrAlways remove up to 95 ~ 97%, the total clearance of colourity reaches 95 ~ 99%, and cost is low, and sludge yield is few, has saved the sludge treatment expense.
2. waste water treatment process of the present invention is simple to operate, handles the back stable effluent quality, and final outflow water can be stablized and reaches " pulp and paper industry pollution discharge standard " requirement (GB3544-2008), i.e. COD
Cr≤ 100mg/L, BOD
5≤ 20 mg/L, SS≤50 mg/L, colourity≤50 times, AOX≤12mg/L.
3. the Fenton preoxidation device of sewage treatment equipment of the present invention, COD
CrWith the chroma removal rate height, be respectively 50 ~ 60% and 80 ~ 90%.
4. compare with traditional technology, before waste water treatment process of the present invention places aerobe to handle the Fenton oxidation, the Fenton pre-oxidation treatment can be the small organic molecule of easily degrading with the oxidation operation of difficult degradations such as lignin, hemicellulose, AOX, improves the biodegradability of waste water, BOD
5/ COD
Cr〉=0.5, make follow-up aerobe handle COD
CrClearance is increased to more than 85 ~ 90% by 70 ~ 75%.
5. the Fenton pre-oxidation treatment of waste water treatment process of the present invention can be removed the AOX in the Straw Pulp middle-stage wastewater.AOX concentration is about 45 ~ 90mg/L in the Straw Pulp middle-stage wastewater, and the AOX after the Fenton oxidation in the waste water can be down to below the 12mg/L that " pulp and paper industry pollution discharge standard " (GB3544-2008) require.
6. waste water treatment process of the present invention substitutes traditional coagulation-settlement process as the pre-treatment means of aerobic treatment, as the Fe of catalyzer with the Fenton pre-oxidation treatment
2+Finally be oxidized to Fe
3+, the Fe of generation
3+Have good flocculence, can be used as the suspended substance in the flocculation agent removal waste water, saved the dosage of aluminium salt, reduced Al
3+Secondary pollution to water body.
7. the Fenton preoxidation device of sewage treatment equipment of the present invention, waste water after pre-oxidation treatment, COD
CrReduce greatly, alleviated the load of follow-up aerobic treatment device, the operation power consumption reduces greatly, and is energy-conservation more than 40%, saved the running cost of wastewater treatment greatly.
8. the Fenton preoxidation device reaction time of sewage treatment equipment of the present invention weak point has shortened the wastewater treatment time, takes up an area of and lacks device processes ability and the processing efficiency of raising.
Description of drawings
Fig. 1 is the process flow diagram of Straw Pulp middle-stage wastewater treatment process of the present invention.
Wherein: 1-pretreatment unit, 2-Fenton preoxidation device, 3-aerobic treatment device, 4-coagulating sedimentation treatment unit, 5-fine fack, 6-water collecting basin, the oblique net of 7-, 8-vitriol oil storage tank, 9-pH equalizing tank, 10-FeSO
4The dosing pond, 11-H
2O
2Storage tank, 12-Fenton oxidation pond 13-alkali lye chemicals dosing plant, 14-neutralization tank, 15-preliminary sedimentation tank, 16-gas blower, 17-aerator, 18-aeration tank, 19-second pond, 20-mixing pit, 21-flocculation tank, 22-reaction tank, 23-final deposition pool.
Embodiment
Describe technical solution of the present invention in detail with embodiment with reference to the accompanying drawings, but protection domain is not by this restriction.
Embodiment 1: a kind of device of realizing Straw Pulp middle-stage wastewater treatment process by shown in Figure 1, mainly comprises pretreatment unit 1, Fenton preoxidation device 2, aerobic treatment device 3 and coagulating sedimentation treatment unit 4.Described pretreatment unit 1, Fenton preoxidation device 2, aerobic treatment device 3 is linked to each other by pipeline in turn with coagulating sedimentation treatment unit 4.
Described pretreatment unit 1 mainly comprises fine fack 5, water collecting basin 6, oblique net 7.Described fine fack 5, water collecting basin 6, oblique net 7 are linked to each other by pipeline in turn.
Described Fenton preoxidation device 2 mainly comprises vitriol oil storage tank 8, pH regulator pond 9, FeSO
4Dosing pond 10, H
2O
2Storage tank 11, Fenton oxidation pond 12, alkali lye chemicals dosing plant 13, neutralization tank 14 and preliminary sedimentation tank 15.Described pH regulator pond 9, Fenton oxidation pond 12, neutralization tank 14, preliminary sedimentation tank 15 are linked to each other by pipeline in turn; Described dense H
2SO
4Storage tank 8 links to each other with pH regulator pond 9; Described FeSO
4Dosing pond 10 and H
2O
2Storage tank 11 links to each other with Fenton oxidation pond 12, and described alkali lye chemicals dosing plant 13 links to each other with neutralization tank 14.
Described aerobe treatment unit 3 mainly comprises aeration tank 18 and second pond 19.Described aeration tank 18 and second pond 19 are in turn by pipe connection.Be provided with aerator 16 in the described aeration tank 18, link to each other with gas blower 17.
Described coagulating sedimentation device 4 mainly comprises flocculation tank 21 and final deposition pool 23 compositions.Described flocculation tank 21 is linked to each other by pipeline in turn with final deposition pool 23.Described flocculation tank 21 is divided into mixing pit 20 and reaction tank 22 two portions, described mixing pit 20 and reaction tank 22 bottom UNICOMs.
The technology of utilizing said apparatus that the Straw Pulp middle-stage wastewater is handled, its step is as follows:
1, the Straw Pulp middle-stage wastewater at first through fine fack remove than Da Yi block pumps and pipeline float suspended substance after enter water collecting basin, be promoted to oblique net by pump then, reclaim in the waste water than macrofiber, comprehensive utilization.
2, pretreated waste water at first enters the pH regulator pond and regulates pH to 3-5, enters the Fenton oxidation pond then, and the organism of difficult degradation is broken down into the small organic molecule of readily biodegradable in the waste water under the effect of Fenton reagent, and removes most COD
CrAnd colourity.Water outlet enters neutralization tank and adds alkali and regulate pH to neutral 6-7, enters then to finish the pre-oxidation treatment process preliminary sedimentation tank is removed suspended substance solid-liquid separation in the waste water under the effect of coagulant aids after.
3, the waste water after the Fenton pre-oxidation treatment enters the aeration tank, removes majority of organic pollutants in the water through absorption, oxidation, the Degradation of aerobic microbiological.The aeration tank water outlet is carried out mud-water separation from flowing into second pond.
4, the second pond water outlet enters the coagulating sedimentation treatment unit, and flow through successively mixing pit and reaction tank enter final deposition pool after the adding flocculation agent fully mixes and carry out solid-liquid separation, final deposition pool water outlet qualified discharge.
Wherein, the used acid of the described pH regulator of step 2 is that concentration is 98% the vitriol oil, and used alkali is caustic soda.Described Fenton reagent is by H
2O
2And Fe
2+Form.Described H
2O
2Concentration is 30%, and dosage is 80mg/L.Described Fe
2+Adopt ferrous sulfate (FeSO
47H
2O) reagent, purity are analytical pure (AR), and dosage is by being 300mg/L; Described coagulant aids is polyacrylamide (PAM), and its dosage is 1mg/L; The described Fenton pre-oxidation treatment of step 2 retention time of sewage is 90min; Waste water aerobic sludge after the solid-liquid separation in second pond after the described aerobe of step 3 is handled, wherein a part is back to and proceeds described aerobe processing after aerobic reactor waste water interior and after the Fenton preoxidation mixes; MLSS concentration is 2.5g/L in the described aeration tank, and dissolved oxygen concentration is 2mg/L, and sludge loading is 0.15kgCOD
Cr/ (kgMLSSd); It is polymerize aluminum chloride (PAC) that the described coagulating sedimentation of step 4 is handled the flocculation agent that adds, and its dosage is 80mg/L.Described coagulant aids is polyacrylamide (PAM), and its dosage is 2mg/L.
Embodiment 2:Except the flocculation agent that adds in the coagulating sedimentation treatment step is bodied ferric sulfate (PFS), its dosage is 90mg/L.Described coagulant aids is polyacrylamide (PAM), and its dosage is outside the 2.5mg/L, and all the other are identical with embodiment 1.
Embodiment 3:But device is reference example 1 and accompanying drawing 1 still, utilizes it to handle the technology of alkaline wheat straw pulp middle-stage wastewater, and step is as follows:
(1) pre-treatment of waste water: than the suspended substance that floats of Da Yi block pumps and pipeline, recovery fully utilizes than macrofiber in the removal waste water;
(2) pre-oxidation treatment: to 3-5, under the effect of Fenton reagent, organism is decomposed pretreated waste water with acid for adjusting pH, and removes most COD
CrAnd colourity, water outlet adds alkali and regulates pH to 6-7, removes the suspended substance in the waste water then under the effect of coagulant aids, finishes the pre-oxidation treatment process after the solid-liquid separation;
(3) aerobe is handled: waste water is removed majority of organic pollutants in the water through absorption, oxidation, the Degradation of aerobic microbiological, and mud-water separation is carried out in water outlet;
(4) coagulating sedimentation is handled: adding flocculation agent and coagulant aids fully mix in the waste water, further remove residual COD
CrBehind SS, carry out solid-liquid separation, the water outlet qualified discharge.
The described acid of step (2) is the vitriol oil, and concentration is 96; Described alkali is caustic soda; Preferably, step (2) pre-oxidation treatment retention time of sewage is 120min.The described Fenton reagent of step (2) is by H
2O
2And Fe
2+Form described H
2O
2Dosage is 120mg/L, described Fe
2+Adopt FeSO
47H
2O reagent, purity is analytical pure, dosage is pressed 400mg/L.Described coagulant aids is polyacrylamide, and its dosage is 2mg/L in step (2), and its dosage is 3mg/L in step (4).The described flocculant poly ferric sulfate of step (4), dosage is 100mg/L.
Embodiment 4:Be that step (2) pre-oxidation treatment retention time of sewage is 100min with embodiment 3 differences.Described H
2O
2Dosage is 110mg/L, and functional quality concentration is 30% H
2O
2, described FeSO
47H
2The O dosage is pressed 380mg/L.Described polyacrylamide, the dosage in step (2) is 1.8mg/L, its dosage is 2.5mg/L in step (4).Described flocculation agent is polymerize aluminum chloride, and dosage is 100mg/L.
Claims (7)
1. efficient device of handling the alkaline wheat straw pulp middle-stage wastewater, it is characterized in that, mainly comprise pretreatment unit (1), Fenton preoxidation device (2), aerobic treatment device (3) and coagulating sedimentation treatment unit (4), described pretreatment unit (1), Fenton preoxidation device (2), aerobic treatment device (3) is linked to each other by pipeline in turn with coagulating sedimentation treatment unit (4), described Fenton preoxidation device (2) mainly comprises the pH regulator pond (9) that is linked to each other by pipeline in turn, Fenton oxidation pond (12), neutralization tank (14) and preliminary sedimentation tank (15), described pretreatment unit (1) mainly comprises fine fack (5), water collecting basin (6) and oblique net (7), described fine fack (5), water collecting basin (6) is linked to each other by pipeline in turn with oblique net (7), described pH regulator pond (9) also links to each other with vitriol oil storage tank (8), and described Fenton oxidation pond (12) also is connected with FeSO
4Dosing pond (10) and H
2O
2Storage tank (11), described neutralization tank (14) also links to each other with alkali lye chemicals dosing plant (13), described aerobic treatment device (3) mainly comprises aeration tank (18) and second pond (19), described aeration tank (18) and second pond (19) are in turn by pipe connection, be provided with aerator (17) in the described aeration tank (18), aerator (17) links to each other with gas blower (16), described coagulating sedimentation treatment unit (4) mainly comprises flocculation tank (21) and final deposition pool (23), described flocculation tank (21) is linked to each other by pipeline in turn with final deposition pool (23), described flocculation tank (21) is divided into mixing pit (20) and reaction tank (22) two portions, described mixing pit (20) and reaction tank (22) bottom UNICOM.
2. device according to claim 1 is characterized in that, the technical parameter of described aeration tank (18) control is: MLSS concentration 2.5 ~ 3g/L, dissolved oxygen concentration 2 ~ 4mg/L, sludge loading 0.15 ~ 0.3kgCOD
Cr/ (kgMLSSd).
3. device according to claim 1 is handled the technology of alkaline wheat straw pulp middle-stage wastewater, it is characterized in that step is as follows:
(1) pre-treatment of waste water: than the suspended substance that floats of Da Yi block pumps and pipeline, recovery fully utilizes than macrofiber in the removal waste water;
(2) pre-oxidation treatment: to 3-5, under the effect of Fenton reagent, organism is decomposed pretreated waste water with acid for adjusting pH, and removes most COD
CrAnd colourity, water outlet adds alkali and regulates pH to 6-7, removes the suspended substance in the waste water then under the effect of coagulant aids, finishes the pre-oxidation treatment process after the solid-liquid separation; Described acid is the vitriol oil of 96-99% for concentration; Described alkali is caustic soda; Described Fenton reagent is by H
2O
2And Fe
2+Form described H
2O
2Dosage is 80 ~ 120mg/L, described Fe
2+Adopt ferrous sulfate, dosage is by 300 ~ 400mg/L;
(3) aerobe is handled: waste water is removed majority of organic pollutants in the water through absorption, oxidation, the Degradation of aerobic microbiological, and mud-water separation is carried out in water outlet;
(4) coagulating sedimentation is handled: adding flocculation agent and coagulant aids fully mix in the waste water, further remove residual COD
CrBehind SS, carry out solid-liquid separation, the water outlet qualified discharge; Described flocculation agent is polymerize aluminum chloride or bodied ferric sulfate; When selecting polymerize aluminum chloride for use, dosage is 80 ~ 100mg/L, and when selecting bodied ferric sulfate for use, dosage is 80 ~ 100mg/L;
Described coagulant aids is polyacrylamide, and its dosage is 1 ~ 2mg/L in step (2), and its dosage is 2 ~ 3mg/L in step (4); Step (2) pre-oxidation treatment retention time of sewage is 90 ~ 120min, described H
2O
2Be 30% H for mass concentration
2O
2, described ferrous sulfate is FeSO
47H
2O reagent, purity are analytical pure.
4. technology according to claim 3 is characterized in that, the described vitriol oil concentration of step (2) is 98%.
5. technology according to claim 3 is characterized in that, the pre-oxidation treatment retention time of sewage is 100 ~ 110min.
6. technology according to claim 3 is characterized in that, described polyacrylamide dosage in step (2) is 1.2 ~ 1.8mg/L.
7. technology according to claim 3 is characterized in that, described polyacrylamide dosage in step (4) is 2.5 ~ 2.8mg/L.
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| CN103523966A (en) * | 2013-10-31 | 2014-01-22 | 东莞理文造纸厂有限公司 | Advanced wastewater treatment system and treatment method |
| CN104671610A (en) * | 2015-02-13 | 2015-06-03 | 王桂霞 | Deep treatment method of chemical wastewater |
| CN105000718B (en) * | 2015-08-11 | 2017-01-18 | 湛江晨鸣浆纸有限公司 | Pulp paper wastewater treatment process |
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| Title |
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| Fenton-混凝法处理麦草浆中段废水的研究;赵玉柱等;《黑龙江造纸》;20081231(第2期);第6-9,13页 * |
| SBR-混凝法处理制浆中段废水;李文俊等;《工业水处理》;20060430;第26卷(第4期);第34-37页 * |
| 李文俊等.SBR-混凝法处理制浆中段废水.《工业水处理》.2006,第26卷(第4期),第34-37页. |
| 赵玉柱等.Fenton-混凝法处理麦草浆中段废水的研究.《黑龙江造纸》.2008,(第2期),第6-9,13页. |
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