CN103951107B - A kind of device and method of Treatment of Wastewater in Coking - Google Patents
A kind of device and method of Treatment of Wastewater in Coking Download PDFInfo
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- CN103951107B CN103951107B CN201410173488.8A CN201410173488A CN103951107B CN 103951107 B CN103951107 B CN 103951107B CN 201410173488 A CN201410173488 A CN 201410173488A CN 103951107 B CN103951107 B CN 103951107B
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- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000004939 coking Methods 0.000 title claims abstract description 39
- 239000002351 wastewater Substances 0.000 title claims abstract description 28
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 239000000571 coke Substances 0.000 claims abstract description 25
- 238000004062 sedimentation Methods 0.000 claims abstract description 18
- 238000005189 flocculation Methods 0.000 claims abstract description 15
- 230000016615 flocculation Effects 0.000 claims abstract description 14
- 238000004537 pulping Methods 0.000 claims abstract description 12
- 239000002894 chemical waste Substances 0.000 claims abstract description 11
- 239000003245 coal Substances 0.000 claims abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000005345 coagulation Methods 0.000 claims abstract description 7
- 230000015271 coagulation Effects 0.000 claims abstract description 7
- 239000003814 drug Substances 0.000 claims abstract description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 12
- 239000000701 coagulant Substances 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 10
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 239000000706 filtrate Substances 0.000 claims description 3
- 229920002401 polyacrylamide Polymers 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 2
- 239000008394 flocculating agent Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 8
- 239000002699 waste material Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 3
- 238000006477 desulfuration reaction Methods 0.000 abstract description 3
- 238000005245 sintering Methods 0.000 abstract description 3
- 239000002594 sorbent Substances 0.000 abstract description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 2
- 239000003546 flue gas Substances 0.000 abstract description 2
- 239000010815 organic waste Substances 0.000 abstract description 2
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 230000001112 coagulating effect Effects 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical group [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- ZMZDMBWJUHKJPS-UHFFFAOYSA-M Thiocyanate anion Chemical compound [S-]C#N ZMZDMBWJUHKJPS-UHFFFAOYSA-M 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000010290 biphenyl Nutrition 0.000 description 1
- 239000004305 biphenyl Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
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- ZMZDMBWJUHKJPS-UHFFFAOYSA-N hydrogen thiocyanate Natural products SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- NRADCUWKNUKPHY-UHFFFAOYSA-N oxalonitrile;phenol Chemical compound N#CC#N.OC1=CC=CC=C1 NRADCUWKNUKPHY-UHFFFAOYSA-N 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000005070 ripening Effects 0.000 description 1
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- 239000003403 water pollutant Substances 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The present invention discloses a kind of industrial organic waste water treatment unit and method, the advanced treatment apparatus specifically after a kind of coking chemical waste water biochemistry and method.Treatment unit of the present invention comprises between mixed reaction pond, radial-flow sedimentation tank, bed mud pump house, filter press, activated coke pulping device and medicament addition device; Waste water arrives that mixed reaction pond carries out adsorbing successively, coagulation, flocculation reaction, enter radial-flow sedimentation tank after advanced treatment completes.Feature of the present invention utilizes the by product of the coal based activated burnt system for desulfuration and denitration of flue gas of sintering machine head and coal based activated coke powder end as water outlet after sorbent material advanced treatment on coking wastewater biochemistry, reaches the object of the treatment of wastes with processes of wastes against one another.The present invention has the advantage that treatment effect is good, non-secondary pollution, less investment, floor space are little, running cost is low, good in economic efficiency.
Description
Technical field
The present invention relates to a kind of industrial organic waste water treatment unit and method, the advanced treatment apparatus particularly after coking chemical waste water biochemistry and method.
Background technology
Coking chemical waste water is mainly derived from the dry distillation of coal and coal gas cools and scavenging process, phenol containing high density, prussiate, thiocyanide and ammonia nitrogen, simultaneously also containing being difficult to the poly-ring aromatic compoundses such as heterogeneous ring compound and biphenyl such as biodegradable oils, pyridine, toxicity is large, intractability is large, is the difficult point of coking industry wastewater treatment always.
Existing treatment technology mainly adopts biological denitrificaion and rear coagulating kinetics integrated technique, and water quality treatment cannot reach coking chemistry industrial pollutants discharging standards table 2 requirement of promulgating in 2012.In conventional processing technique, biologic treating technique mainly adopts A/O or A2/O biological denitrification process to come decarburization simultaneously and denitrogenation, large and difficult degradation composition is high based on coking chemical waste water toxicity, the impact resistance of traditional biological denitrification process is poor, the dilution water yield is large, processing cost is high, and removes not the strengthening of hardly degraded organic substance, causes COD and colourity cannot be up to standard.
Because biological treatment water outlet exceeds standard seriously, must carry out advanced treatment, the advanced treatment process of research at present has coagulating sedimentation, charcoal absorption, advanced oxidation, membrane sepn etc.Due to coagulating sedimentation advantage of lower cost, widespread use in coking wastewater deep treatment, but residual organic substances polarity is comparatively strong, many containing chromophoric group, COD and color removal efficiency lower, water outlet is still difficult to up to standard.Major part high-level oxidation technology (as electrochemical oxidation process, photochemical catalysis etc.) processing cost is high, and through engineering approaches difficulty is large; The high-level oxidation technology such as fenton and ozone oxidation ripening degree is high, and technical risk is low, invests little, and treatment effect is good, but the cost adding hydrogen peroxide is higher, adds a large amount of soda acid and introduces a lot of salt and be unfavorable for waste water recycling; Direct ozone oxidation is inadequate based on ozone oxidation ability, and ozone utilization rate is low, and cost is high, and treatment effect is undesirable.In membrane separation technique, nanofiltration and reverse osmosis to salt and organic removal rate higher, can de-salted water be prepared, but it is serious to directly apply to coking chemical waste water fouling membrane, and membrane lifetime is low, investment and processing cost high, must carry out pre-treatment before film, dense water outlet becomes a difficult problem simultaneously.
It is better that conventional plant gac is used for coking chemical waste water aftertreatment adsorption effect, but adsorb saturated after not easily regenerate, cause cost for wastewater treatment too high.
There is secondary pollution, invest the problems such as high, running cost is high in above-mentioned treatment process.
Summary of the invention
The invention provides a kind of by product utilizing the coal based activated burnt system for desulfuration and denitration of flue gas of sintering machine head, namely coal based activated coke powder end, as the device and method of sorbent material advanced treatment on coking wastewater containing phenol and cyanide biochemical system water outlet, reaches the object of the treatment of wastes with processes of wastes against one another.Have the advantages that treatment effect is good, non-secondary pollution, floor space are little, less investment, running cost are low, Sewage Water Emissions concentration limit is stablized and reaches " coking chemistry emission of industrial pollutants standard " (GB16171-2012) table 2 directly emission standard.
The present invention realizes by the following technical solutions:
A kind of device of Treatment of Wastewater in Coking is: comprise between mixed reaction pond, radial-flow sedimentation tank, bed mud pump house, filter press, activated coke pulping device and medicament addition device; Described mixed reaction pond is provided with two, wherein one for subsequent use; Mixed reaction pond comprises distribution reservoir, and every mixed reaction pond is divided into three grid spaces by concrete diaphragm, is provided with a set of whipping appts in every grid space; Radial-flow sedimentation tank is provided with two, is provided with mud scraper in settling tank; Slush pump is provided with in bed mud pump house; Be provided with two cover plate-and-frame filter press between filter press, activated coke pulping device comprises pulping tank and adds pump, and medicament addition device comprises coagulant dosage device and flocculating agent feeding device.
Further, described slush pump is provided with three, and two normally use, and one for subsequent use, and the flow of slush pump is 15m
3/ h, lift is 65m; The filtration area of described plate-and-frame filter press is 150m
2, chamber space is 2.49m
3; Described activated coke pulping tank is of a size of φ 5m × 5m, and adding pumping capacity is 12.5m
3/ h, lift is 20m.
The method of Treatment of Wastewater in Coking provided by the invention, adopts said apparatus Treatment of Wastewater in Coking, comprises the following steps:
(1) water outlet from coking chemical waste water biochemical system second pond flows into mixed reaction pond certainly through mixed reaction pond distribution reservoir;
(2) be respectively equipped with activated coke slurry pool, coagulating agent pond, flocculation agent pond in three grid spaces in every mixed reaction pond, the waste water of mixed reaction pond carry out adsorbing successively, coagulation, flocculation reaction, enter radial-flow sedimentation tank;
(3), after radial-flow sedimentation tank precipitation, water outlet is from flowing into clean water basin reuse, and bed mud enters bed mud pump house;
(4) bed mud in bed mud pump house is through slush pump, and a part returns activated coke pulping tank recycling, and another part enters plate-and-frame filter press dehydration;
(5) plate-and-frame filter press filtrate is back to mixed reaction pond, and mud cake substitutes coking coal and produces for coke oven.
Further, described activated coke slurries, its effective constituent is the by product activated coke powder of the burnt system for desulfuration and denitration of sintering activity, and the concentration that activated coke powder is configured to 15%-25% added, adding concentration is 1-3ppm, and consumption is 20 ton per days.
Described coagulating agent is polymerize aluminum chloride, and concentration is 5%-10%, and adding concentration is 20-100ppm; Described flocculation agent is polyacrylamide, and concentration is 0.1%-0.5%, and adding concentration is 0.5-2ppm.
The residence time of described waste water in mixing reactor is: the residence time is 20-40 minute altogether, and the residence time in activated coke slurry pool, coagulating agent pond, flocculation agent pond is substantially equal; The stirring velocity in three ponds in described mixed reaction pond is respectively: activated coke slurry pool is 120-150rpm, and coagulating agent pond is 120-150rpm, and flocculation agent pond is 20-40rpm.
The residence time of described waste water in radial-flow sedimentation tank is 1.5-3.5 hour, and surface load is 0.6-1.5m
3/ (m
2h).
Compared with existing advanced treatment process, feature of the present invention utilizes coal based activated coke powder end as sorbent material, and water outlet after advanced treatment on coking wastewater biochemistry, reaches the object of the treatment of wastes with processes of wastes against one another.The present invention has following beneficial effect:
1, treatment effect is good---and this technique has good removal effect to the colourity of coking biochemical treatment system water outlet, peculiar smell, COD concentration can be reduced to below 80mg/L by about 150mg/L, ammonia nitrogen, prussiate etc. all have and decline in various degree, (GB16171-2012) table 2 directly emission standard that water conditioning reaches " coking chemistry emission of industrial pollutants standard ".
2, non-secondary pollution---compared with other techniques, the whole process of technique does not produce the more reluctant tail water such as reverse osmosis concentrated salt solution, absorb-elute liquid.
3, less investment, floor space are little---and this technique only needs to increase between mud filter press, activated coke dosing system, and coagulation-flocculation adding of agent system, bed mud pump house, gross investment is less than 2,000,000.Compared with other techniques, save gross investment more than 3,000 ten thousand yuan.
4, running cost is low---and cost consumption is mainly coagulation, flocculation medicament, the electricity consumption such as pump, stirrer, about about 0.3 yuan of ton cost of water treatment, and other technique ton water running costs existing are all in 2-4 unit.
5, good in economic efficiency---mud cake Substitute For Partial coking coal returns coke oven and utilizes, and by utilizing every day 20 tons of useless activated coke powder to calculate, substitutes 7300 tons, coking coal (unit price 1400 yuan/ton) every year, benefit 1,241 ten thousand yuan/year.
Present invention process also coagulation section can be transformed after existing coking chemical waste water biochemical treatment system.Do not need again newly-built mixed reaction pond, radial-flow sedimentation tank, adding of agent system etc.
Below in conjunction with drawings and Examples, the present invention will be further described.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Embodiment:
As shown in Figure 1, the advanced treatment process flow process of coking chemical waste water provided by the invention is:
(1) from the distribution reservoir of the waste water inflow mixed reaction pond of biochemical system second pond, then mixed reaction pond is entered;
(2) mixed reaction pond is separated into three spaces by concrete diaphragm, be respectively activated coke slurry pool, coagulating agent pond, flocculation agent pond, the activated coke slurries that concentration is 15-25% have been added in activated coke slurry pool, adding concentration is 1-3ppm, the polymerize aluminum chloride that concentration is 5%-10% is with the addition of in coagulating agent pond, adding concentration is 20-100ppm, with the addition of the polyacrylamide of concentration 0.1%-0.5% in flocculation agent pond, and adding concentration is 0.5-2ppm; Waste water carries out adsorbing successively, coagulation, flocculation reaction, enter radial-flow sedimentation tank;
(3), after radial-flow sedimentation tank precipitation, water outlet is from flowing into clean water basin reuse, and bed mud enters bed mud pump house;
(4) bed mud in bed mud pump house is through slush pump, and a part returns activated coke pulping tank recycling, and another part enters plate-and-frame filter press dehydration;
(5) plate-and-frame filter press filtrate is back to mixed reaction pond, and mud cake substitutes coking coal and produces for coke oven.
As shown in the table by its water quality detection situation of waste water of the inventive method process:
| Analysis project | pH | SS | Oil | COD | Ammonia nitrogen | Total cyanogen | Phenol | Total phosphorus |
| Unit | — | mg/L | mg/L | mg/L | mg/L | mg/L | mg/L | mg/L |
| Technique is intake | 7.35 | 38 | 6.81 | 145 | 4.94 | 3.08 | 0.028 | 3.26 |
| Process for Effluent | 6.76 | 16 | 0.262 | 78.5 | 2.45 | 0.15 | 0.014 | 0.84 |
| Reference standard | 6-9 | 50 | 2.5 | 80 | 10 | 0.2 | 0.30 | 1.0 |
Can be drawn by upper table, (GB16171-2012) table 2 directly emission standard that water pollutant concentration all reaches " coking chemistry emission of industrial pollutants standard ".
Present invention process also coagulation section can be transformed after existing coking chemical waste water biochemical treatment system.Do not need again newly-built mixed reaction pond, radial-flow sedimentation tank, adding of agent system etc.
Claims (8)
1. a device for Treatment of Wastewater in Coking, is characterized in that: comprise between mixed reaction pond, radial-flow sedimentation tank, bed mud pump house, filter press, activated coke pulping device and medicament addition device; Described mixed reaction pond is provided with two, wherein one for subsequent use; Mixed reaction pond comprises distribution reservoir, and every mixed reaction pond is divided into three grid spaces by concrete diaphragm, is provided with a set of whipping appts in every grid space; Radial-flow sedimentation tank is provided with two, is provided with mud scraper in settling tank; Slush pump is provided with in bed mud pump house; Be provided with two cover plate-and-frame filter press between filter press, activated coke pulping device comprises pulping tank and adds pump, and medicament addition device comprises coagulant dosage device and flocculating agent feeding device.
2. the device of Treatment of Wastewater in Coking according to claim 1, is characterized in that: described slush pump is provided with three, and two normally use, and one for subsequent use, and the flow of slush pump is 15m
3/ h, lift is 65m.
3. the device of Treatment of Wastewater in Coking according to claim 1, is characterized in that: the filtration area of described plate-and-frame filter press is 150m
2, chamber space is 2.49m
3.
4. the device of Treatment of Wastewater in Coking according to claim 1, is characterized in that: described activated coke pulping tank is of a size of φ 5m × 5m, and adding pumping capacity is 12.5m
3/ h, lift is 20m.
5. adopt a method for the device Treatment of Wastewater in Coking described in any one of claim 1 ~ 4, it is characterized in that: comprise the following steps:
(1) water outlet from coking chemical waste water biochemical system second pond flows into mixed reaction pond certainly through mixed reaction pond distribution reservoir;
(2) be respectively equipped with activated coke slurry pool, coagulating agent pond, flocculation agent pond in three grid spaces in every mixed reaction pond, the waste water of mixed reaction pond carry out adsorbing successively, coagulation, flocculation reaction, enter radial-flow sedimentation tank;
Described activated coke slurries are: concentration activated coke powder being configured to 15%-25%, and adding concentration is 1-3ppm, and consumption is 15-20 ton per day;
Described coagulating agent is polymerize aluminum chloride, and concentration is 5%-10%, and adding concentration is 20-100ppm; Described flocculation agent is polyacrylamide, and concentration is 0.1%-0.5%, and adding concentration is 0.5-2ppm;
(3), after radial-flow sedimentation tank precipitation, water outlet is from flowing into clean water basin reuse, and bed mud enters bed mud pump house;
(4) bed mud in bed mud pump house is through slush pump, and a part returns activated coke pulping tank recycling, and another part enters plate-and-frame filter press dehydration;
(5) plate-and-frame filter press filtrate is back to mixed reaction pond, and mud cake substitutes coking coal and produces for coke oven.
6. the method for Treatment of Wastewater in Coking according to claim 5, is characterized in that: the altogether residence time of described waste water in mixing reactor is 20-40 minute.
7. the method for Treatment of Wastewater in Coking according to claim 5, it is characterized in that: the stirring velocity in three ponds in described mixed reaction pond is respectively: activated coke slurry pool is 120-150rpm, coagulating agent pond is 120-150rpm, and flocculation agent pond is 20-40rpm.
8. the method for Treatment of Wastewater in Coking according to claim 5, is characterized in that: the residence time of described waste water in radial-flow sedimentation tank is 1.5-3.5 hour, and surface load is 0.6-1.5m
3/ (m
2h).
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| CN103723853B (en) * | 2013-12-04 | 2015-08-26 | 江苏双净净化科技有限公司 | Gas generating station intermittent type total system and treatment process thereof |
| CN104192966B (en) * | 2014-09-25 | 2016-03-09 | 余柏林 | Utilize processing method and the device of coke powder advanced treatment on coking biochemical waste water |
| CN104355458A (en) * | 2014-11-21 | 2015-02-18 | 中冶赛迪工程技术股份有限公司 | Deep treatment method of coking wastewater |
| CN107089739A (en) * | 2017-06-19 | 2017-08-25 | 北京中科康仑环境科技研究院有限公司 | The enhanced coagulation technique and its device of a kind of biochemical postindustrial waste water |
| CN108083497A (en) * | 2017-12-21 | 2018-05-29 | 上海万狮环保科技有限公司 | A kind of application of coking wastewater deep treatment composite drug |
| CN109179551B (en) * | 2018-09-07 | 2021-09-28 | 湖南华菱涟源钢铁有限公司 | Phenol-cyanogen wastewater treatment method |
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| CN1958486A (en) * | 2006-11-10 | 2007-05-09 | 哈尔滨工业大学 | Advanced treatment method for carbonization wastewater |
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| CN1958486A (en) * | 2006-11-10 | 2007-05-09 | 哈尔滨工业大学 | Advanced treatment method for carbonization wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 混凝吸附法深度处理焦化废水;金文杰等;《环境工程》;20090228;第27卷(第1期);第3-4、25页 * |
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