CN203754565U - Device for combined physicochemical treatment and biochemical treatment of flue gas desulfurization wastewater - Google Patents
Device for combined physicochemical treatment and biochemical treatment of flue gas desulfurization wastewater Download PDFInfo
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- CN203754565U CN203754565U CN201420111270.5U CN201420111270U CN203754565U CN 203754565 U CN203754565 U CN 203754565U CN 201420111270 U CN201420111270 U CN 201420111270U CN 203754565 U CN203754565 U CN 203754565U
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- 239000002351 wastewater Substances 0.000 title claims abstract description 104
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 239000003546 flue gas Substances 0.000 title claims abstract description 42
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 41
- 230000023556 desulfurization Effects 0.000 title claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 40
- 239000010802 sludge Substances 0.000 claims description 31
- 239000000126 substance Substances 0.000 claims description 21
- 229910021529 ammonia Inorganic materials 0.000 claims description 20
- 230000003647 oxidation Effects 0.000 claims description 20
- 238000007254 oxidation reaction Methods 0.000 claims description 20
- 238000005189 flocculation Methods 0.000 claims description 17
- 230000016615 flocculation Effects 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 10
- 229910052799 carbon Inorganic materials 0.000 abstract description 10
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 21
- 230000008569 process Effects 0.000 description 20
- 241000894006 Bacteria Species 0.000 description 19
- 238000012545 processing Methods 0.000 description 17
- 241001453382 Nitrosomonadales Species 0.000 description 12
- 238000005352 clarification Methods 0.000 description 12
- 244000005700 microbiome Species 0.000 description 12
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- 230000001580 bacterial effect Effects 0.000 description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 229910052760 oxygen Inorganic materials 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 229910001385 heavy metal Inorganic materials 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 229910052602 gypsum Inorganic materials 0.000 description 7
- 239000010440 gypsum Substances 0.000 description 7
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 6
- 239000000701 coagulant Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 244000144992 flock Species 0.000 description 6
- 238000009413 insulation Methods 0.000 description 6
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- 230000015556 catabolic process Effects 0.000 description 5
- 238000006731 degradation reaction Methods 0.000 description 5
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- 238000001556 precipitation Methods 0.000 description 5
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- 239000002562 thickening agent Substances 0.000 description 5
- 238000005273 aeration Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- 206010002660 Anoxia Diseases 0.000 description 3
- 241000976983 Anoxia Species 0.000 description 3
- 206010021143 Hypoxia Diseases 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 230000007953 anoxia Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 239000011133 lead Substances 0.000 description 3
- 239000011159 matrix material Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000031018 biological processes and functions Effects 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 230000036983 biotransformation Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000012010 growth Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 230000035800 maturation Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229920002401 polyacrylamide Polymers 0.000 description 2
- 239000010801 sewage sludge Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- HRXKRNGNAMMEHJ-UHFFFAOYSA-K trisodium citrate Chemical compound [Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O HRXKRNGNAMMEHJ-UHFFFAOYSA-K 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- 241000108664 Nitrobacteria Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 241000589774 Pseudomonas sp. Species 0.000 description 1
- 241000190932 Rhodopseudomonas Species 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- DWCPARVNWQQOFS-UHFFFAOYSA-N [Na].[Na].[Na].N1=NN=CC=C1.S1SSC=C1 Chemical compound [Na].[Na].[Na].N1=NN=CC=C1.S1SSC=C1 DWCPARVNWQQOFS-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
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- 241001148470 aerobic bacillus Species 0.000 description 1
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- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
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- 229910052731 fluorine Inorganic materials 0.000 description 1
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- 230000015784 hyperosmotic salinity response Effects 0.000 description 1
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- 229910052742 iron Inorganic materials 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
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- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
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Abstract
The utility model belongs to the technical field of flue gas desulfurization wastewater treatment and relates to a device for combined physicochemical treatment and biochemical treatment of flue gas desulfurization wastewater. The device is characterized by comprising a wastewater buffer pool, a physicochemical treatment device, a middle water tank and a biological treatment device, wherein the wastewater effluent outlet of the wastewater buffer pool is communicated with the feed inlet of the physicochemical treatment device by a pipeline; the effluent outlet of the physicochemical treatment device is communicated with the feed inlet of the middle water tank and the effluent outlet of the middle water tank is communicated with the feed inlet of the biological treatment device by a pipeline. The ammonia nitrogen in wastewater can be efficiently removed by the device in the case that no additional carbon sources are applied.
Description
Technical field
The utility model belongs to flue gas desulfurization waste-water processing technology field, is specifically related to a kind of device that adopts physico-chemical process and biochemical process combined treatment flue gas desulfurization waste-water.
Background technology
Along with economic growth and social progress, environment protection is more and more taken seriously, and China has carried out large-scale SO to coal firing boiler
2administer engineering, a large amount of desulfurizers builds up and puts into operation, wherein limestone-gypsum method is current most widely used Wet Flue Gas Desulfurization Technology, its technology maturation, absorption agent wide material sources, by-produced gypsum can utilize, but limestone-gypsum method flue gas desulfurization also exists the emission problem of desulfurization wastewater.
Flue gas desulfurization waste-water principal character is to be slightly acidic, and pH value is variant with desulfurizer flow process difference, but relatively stable, and the pH value of domestic power plant effluent is generally 4～6.5; Suspended substance solid component content is high, and general waste strength is 1%～4%, is mainly Wingdale, gypsum particle and other heavy metal oxides, is easy to bonding, and sedimentation function is good; Heavy metal content is high, mainly contains Ca in waste water
2+, Mg
2+, Fe
2+, Al
3+, other heavy metal ion contents are lower, contain the non-metal contaminants such as the heavy metals such as mercury, lead, nickel, zinc and arsenic, fluorine, because desulfurization wastewater is slightly acidic, therefore many heavy metal ion still have good solubility simultaneously.The method of materialization processing is mainly taked in the processing of flue gas desulfurization waste-water at present, removes suspended substance and heavy metal ion in waste water by materialization means such as neutralization, sedimentation, flocculations, and pH value is transferred to the requirement of emission standard.
The issuing and implementation of new environmental regulation are to NO
xmade more strict regulation, equipment for denitrifying flue gas is extensively implemented, and causes thus containing the nitrogen of escaping from equipment for denitrifying flue gas in a large number in flue gas desulfurization waste-water, causes ammonia nitrogen in waste water to exceed standard.And ammonia nitrogen in waste water cannot by and the materialization means such as flocculation sediment removed, independent materialization treatment system can not meet, and therefore need to after materialization is processed, increase other method and process.
The method of denitrogenation of waste water is a lot, has Physical, chemical method, biological process etc.For various reasons, the application of Physical, chemical method is very restricted, and mainly adopts at present bio-denitrification technology both at home and abroad.At present the principle of conventional biological denitrificaion is to realize by two separate processes of nitrification and denitrification, wherein nitratedly need to consume a large amount of oxygen, and denitrification will carry out under anoxia condition, and needs certain carbon source.
But flue gas desulfurization waste-water water quality is very poor, pollution components is a lot, suspension object height, saltiness, Cl
-, F
-very high concentrations, the B/C(of flue gas desulfurization and denitrification waste water can be biochemical than) be worth low, biodegradability is very poor, adopts common biological treatment to be difficult to Start-up and operating performance, effluent quality after treatment cannot be realized qualified discharge.
Anammox refers to that under anaerobic, anaerobic ammonia oxidizing bacteria is by NH
4 +-N is as electron donor, NO
2 --N is as electron acceptor(EA), the bioprocess that is nitrogen by the nitrogen transformation of these two kinds of forms.A kind for the treatment of process that utilizes autotrophic microorganism degradation of ammonia nitrogen of anaerobic ammonia oxidation process, does not rely on organic carbon source, and B/C(can biochemically be compared) do not require, be therefore suitable for processing the flue gas desulfurization and denitrification waste water of low B/C ratio.
Summary of the invention
The purpose of this utility model is to provide a kind of materialization and biochemical combined treatment device of flue gas desulfurization waste-water, and this device can, the in the situation that of additional carbon not, efficiently be removed the ammonia nitrogen in waste water.
For achieving the above object, technical solution adopted in the utility model is: a kind of materialization of flue gas desulfurization waste-water and biochemical combined treatment device, is characterized in that it comprises waste water Buffer Pool, apparatus for physical Chemical treating, intermediate water tank and biochemical treatment apparatus; The waste water delivery port of waste water Buffer Pool be connected with the input terminus of apparatus for physical Chemical treating by pipeline (described pipeline is provided with valve and pump); The output terminal of apparatus for physical Chemical treating is connected with the input aperture of intermediate water tank, and the delivery port of intermediate water tank is connected with the input terminus of biochemical treatment apparatus by pipeline.
During described apparatus for physical Chemical treating comprises and case, sludge box, flocculation tanks, concentrated/settler; In be connected with the input aperture of case and the waste water delivery port of waste water Buffer Pool; In be connected with the input aperture of sludge box by pipeline with the waste water delivery port of case, the waste water delivery port of sludge box is connected with the input aperture of flocculation tanks by pipeline, the delivery port of flocculation tanks is connected with the input aperture of concentrated/settler by pipeline, concentrated/settler flows automatically to the intermediate water tank of next stage by overflow mode, the mud discharging mouth of concentrated/settler is taken away and sent into sludge treating system by pipeline, pump.
Described biochemical treatment apparatus comprises anaerobic ammonia oxidation reactor, anoxic reacter, aerobic reactor and settling tank; The input aperture of anaerobic ammonia oxidation reactor is connected with the delivery port of intermediate water tank, the delivery port of anaerobic ammonia oxidation reactor is connected with the input aperture of anoxic reacter by pipeline, the delivery port of anoxic reacter is connected with the input aperture of aerobic reactor by pipeline, the delivery port of aerobic reactor is connected with the input aperture of settling tank by pipeline, and settling tank is provided with primary water discharge outlet, activated sludge discharged mouth.
All pipelines are provided with valve, can establish pump.
Device of the present utility model can adopt materialization processing, biochemical treatment two-stage process, step-by-step processing desulfurization wastewater, especially front end is provided with the wastewater treatment of Wingdale-gypsum wet flue gas desulfurizing device of equipment for denitrifying flue gas, can be applicable to electric power, metallurgy, environmental protection and chemical technology field.
Compared with traditional wastewater biochemical processing, the beneficial effects of the utility model are:
1) the utility model is specially adapted to front end and is provided with the wastewater treatment of Wingdale-gypsum wet flue gas desulfurizing device of equipment for denitrifying flue gas.
2) denitrogenation of the present utility model adopts anaerobic ammonia oxidation process, does not need additional organic carbon source, does not need reactor to carry out aeration, can save energy consumption and expense.
3) the biochemical bacterium that the utility model biological process adopts has equally very high biological activity under high salinity environment, still can realize its good denitrification functions, process Cl in water-concentration can reach 20000ppm.
4) in the situation that of additional carbon not, can efficiently remove the ammonia nitrogen in waste water, clearance reaches more than 85%, has efficient feature.
Brief description of the drawings
Fig. 1 is structured flowchart of the present utility model.
Fig. 2 is the structural representation of anaerobic ammonia oxidation reactor.
Fig. 3 is the structural representation of the cover plate of anaerobic ammonia oxidation reactor.
Fig. 4 is the structural representation of the base plate of anaerobic ammonia oxidation reactor.
Fig. 5 is concentrated/settler structural representation of (or claiming: clarification/thickener).
Fig. 6 is the process flow diagram of an embodiment of the utility model.
In Fig. 2-3: 1-venting port, 2-is incubated water, 3-water intake, 4-insulation water water-in, 5-mud discharging mouth, 6-support, 7-wastewater effluent mouth I, 8-wastewater effluent mouth II, 9-wastewater effluent mouth III, 10-wastewater effluent mouth IV, 11-insulation water water outlet, 12-pre-opened hole I, 13-pre-opened hole II, 14-pre-opened hole III, 15-pre-opened hole IV, 16-screw, 17-pre-opened hole V.
In Fig. 5: 18-cylindrical shell, 19-central draft tube, 20-mud scraper, 21-railing, 22-inclined tube, 23-supports.
Embodiment
As shown in Figure 1, a kind of materialization of flue gas desulfurization waste-water and biochemical combined treatment device, it comprises waste water Buffer Pool, apparatus for physical Chemical treating, intermediate water tank (or claiming intermediate pool) and biochemical treatment apparatus, during apparatus for physical Chemical treating comprises and case, sludge box, flocculation tanks, concentrated/settler (or claiming mud concentrating clarifying device), biochemical treatment apparatus comprises anaerobic ammonia oxidation reactor, anoxic reacter (denitrification), aerobic reactor (or claiming aerobic biological processor) and settling tank, the waste water delivery port of waste water Buffer Pool (reception flue gas desulfurization waste-water) by pipeline with in be connected with the input aperture of case, described pipeline is provided with valve and pump, in be connected with the input aperture of sludge box by pipeline with the waste water delivery port of case that (pipeline is provided with valve, on pipeline, can establish pump), the waste water delivery port of sludge box is connected with the input aperture of flocculation tanks by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), the delivery port of flocculation tanks is connected with the input aperture of concentrated/settler by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), concentrated/settler flows automatically to the intermediate water tank of next stage by overflow mode, the mud discharging mouth of concentrated/settler is by pipeline, pump is taken away and is sent into sludge treating system, the delivery port of intermediate water tank is connected with the input aperture of anaerobic ammonia oxidation reactor by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), the delivery port of anaerobic ammonia oxidation reactor is connected with the input aperture of anoxic reacter by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), the delivery port of anoxic reacter is connected with the input aperture of aerobic reactor by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), the delivery port of aerobic reactor is connected with the input aperture of settling tank by pipeline, and (pipeline is provided with valve, on pipeline, can establish pump), settling tank is provided with primary water discharge outlet, activated sludge discharged mouthful.
As shown in Figure 6, a kind of materialization of flue gas desulfurization waste-water and biochemical combined treatment process, comprise the following steps:
1). adopt physicochemical method to carry out pre-treatment to flue gas desulfurization waste-water at leading portion, comprise: flue gas desulfurization waste-water (waste water that flue gas desulfurization (FGD) unit comes) enters waste water Buffer Pool, then concentrate and clarify through neutralization, sedimentation, cohesion, mud and (remove suspended substance, the heavy metal of flue gas desulfurization waste-water, and regulate its pH value, making water quality after treatment meet follow-up biochemical water inlet requires), obtain pretreated flue gas desulfurization waste-water; Detailed process is:
1. during flue gas desulfurization waste-water is introduced into by waste water Buffer Pool and case, in and in case, to add milk of lime be 9～9.5 by pH regulator, make precipitation of hydroxide that most of heavy metal in flue gas desulfurization waste-water forms indissoluble out;
2. in passing through and the waste water of case processing, most heavy metal ion has generated precipitation of hydroxide, and part Pb at this moment
2+, Hg
2+still exist in waste water with ionic forms; In process, enter in sludge box with the waste water of case processing, in sludge box, add organosulfur (TMT-15) solution, make Pb
2+, Hg
2+with the more precipitation of indissoluble of its generation, from waste water, separate;
Described organosulfur solution (or claiming organosulfur liquid) is tri-thiol triazine trisodium salt (TMT-15), and the compound concentration of organosulfur solution is 13wt%～17wt%;
3. enter flocculation tanks through the waste water of sludge box processing, in flocculation tanks, add Polyferric Sulfate and coagulant aids to make that suspended solid flocculates rapidly, sedimentation; The add-on of described Polyferric Sulfate (polyaluminum sulfate iron(ic) chloride) and coagulant aids (anion-polyacrylamide solution, the aqueous solution of 0.1wt% concentration) is respectively 65～85ppm and 2.5～3ppm;
4. enter clarification/thickener (or claiming: concentrate/settler, structure is shown in accompanying drawing 5) through the waste water of flocculation tanks processing, separated with water at this throw out, throw out is deposited in bottom, forms concentrated mud under gravity concentration effect; Mud is taken away and is sent into sludge treating system (after sludge dewatering, mud cake outward transport) by pump by clarification/thickener bottom pipe; The supernatant liquor of clarification/thickener is pretreated flue gas desulfurization waste-water, and pretreated flue gas desulfurization waste-water flows automatically to next stage intermediate water tank (or claiming intermediate pool) by overflow mode;
Clarification/thickener (structure is shown in accompanying drawing 5), it comprises cylindrical shell 18, mud scraper 20, central draft tube 19, inclined tube 22, the bottom of cylindrical shell is fixed with supports 23, in cylindrical shell 18, be provided with mud scraper 20, central draft tube 19, inclined tube 22, waste water, from flocculation tanks overflows, enters into clarification concentrator central tube by action of gravity.On the inlet channel of clarification concentrator, add coagulant aids (being generally the anion-polyacrylamide solution of 0.1wt%).Coagulant aids and waste water enter into clarification concentrator central tube after pipe-line blending.In flocculation tanks, form the suspended substance of cotton-shaped particle, by the complexing action of coagulant aids, formed thick flocs unit solid, that more easily deposit.By the guide functions of central tube, waste water arrives clarification concentrator middle part, and by the promotion of follow-up water inlet, waste water starts rising.Due to from central tube out after, waste water rise sectional area suddenly increase, waste water rise also rapid drawdown of speed.The waste water that has gone out central tube is at clarification concentration basin the inside rising, and the macrobead flock that has reacted generation in waste water relies on action of gravity to start to fall.Flock in the waste water rising and the flock of whereabouts be collision mutually in interting, and becomes larger flock by the effect of coagulant aids, finally loses activity and deposits to the sewage sludge storage district of clarification concentrator.And form suspension zone because the flock of the flock in the waste water constantly entering and whereabouts ceaselessly obtains supplementing in the upper and lower scope of central tube.Waste water upwards flows always, and through inclined tube district, clear water zone, finally covers effluent weir, overflows in water tank by rising pipe.Flocculation is carried and is relied on the sewage sludge storage district of gravity sedimentation to clarification concentrator, is focused in mud-removing bucket by the scraper plate of mud scraper, is regularly expelled to sludge dewatering system dewaters by sludge pump.
2) pretreated flue gas desulfurization waste-water flows automatically in intermediate water tank by overflow mode, injects dilute hydrochloric acid and pH value is adjusted to the requirement that meets follow-up biochemical treatment in intermediate water tank;
Described pH value is 6.5～7.5, and the concentration of described dilute hydrochloric acid is 25wt%～35wt%(massfraction);
3). adopt biochemical method smoke treatment desulfurization wastewater at back segment, comprise: intermediate water tank flue gas desulfurization waste-water after treatment (adopts anaerobic ammonia oxidation process to remove total nitrogen through Anammox, denitrification, aerobe processing, precipitation, the nitric nitrogen again Anammox being produced carries out denitrification denitrogenation, finally process and remove organism by aerobe, make waste water after treatment meet emission request), through primary water qualified discharge or the reuse of settling tank processing; Detailed process is:
1. intermediate water tank flue gas desulfurization waste-water after treatment enters anaerobic ammonia oxidation reactor (its structure is shown in accompanying drawing 2-4), and under anaerobic, anaerobic ammonia oxidizing bacteria is with NH
4 +-N is as electron donor, NO
2 --N, as electron acceptor(EA), is nitrogen by the nitrogen transformation of these two kinds of forms;
Anaerobic ammonia oxidation reactor (its structure is shown in accompanying drawing 2-4), it comprises body, is provided with waste water chamber in body, and water intake 3, wastewater effluent mouth (7,8,9,10) all communicate with waste water chamber, the bottom of body is provided with mud discharging mouth (establishing valve control), and mud discharging mouth communicates with waste water chamber; Outside waste water chamber, be provided with insulation water cavity, insulation water water-in 4, insulation water water outlet 11 all communicate with insulation water cavity;
Anaerobic ammonia oxidation reactor is container or pond airtight, lucifuge; Higher temperature of reaction (15-40 DEG C); Higher influent ammonium concentration (T-N:100～800mg/L); Taking ammonia nitrogen as electron donor, do not need additional organic carbon source; Do not need reactor to carry out aeration;
Anammox reaction conditions is as follows:
Temperature: optimum temps is at 30-35 DEG C;
PH: best pH between 6.8-8.3, water inlet suitable 7.5 left and right that maintain of pH, the highest pH is not suitable for exceeding for a long time more than 8.5;
Hydraulic detention time (HRT): HRT is can be according to the enrichment degree of bacterial classification, and the nitrogen removal performance of reactor is adjusted; HRT can from a couple of days to several h not etc., specifically can simply judge from following two aspects the adjustment of HRT: 1. reactor nitrogen removal performance can or can not be because of the reducing of HRT, and cause matrix to remain in a large number, causes the accumulation (especially nitrite nitrogen) of matrix; 2. whether sludge settling can be because of the reducing of HRT, and causes a large amount of losses of a large amount of active sludge;
Illumination: need lucifuge operation;
Dissolved oxygen (DO): anaerobic ammonia oxidizing bacteria is more responsive to DO, higher DO can cause reactive behavior to be suppressed, and more suitable DO scope is below 0.5mg/L; Higher DO is reversible to the inhibition of reactive behavior, if waste water does not have deoxidation, the nitrobacteria in system (aerobic bacteria) can part breed, and after consuming the DO in reactive system, anaerobic ammonia oxidizing bacteria shows reactive behavior again.(postpone the denitrogenation time, cause denitrogenation slow, Simultaneous Nitrification bacterium competes a part of ammonia nitrogen together with anaerobic ammonia oxidizing bacteria);
Substrate concn: the synchronous removal of ammonia nitrogen and nitrite nitrogen is the feature (Theoretical Mass concentration ratio is 1:1.32) that realizes Anammox, ammonia nitrogen and nitrite nitrogen are the matrix of carrying out Anammox reaction, but in the time of influent ammonia nitrogen and nitrite nitrogen excessive concentration, can suppress the speed of reaction of Anammox; It is generally acknowledged, ammonia nitrogen is less on the impact of reactive system, and more than nitrite nitrogen is not suitable for exceeding 200mg/L, but this inhibition concentration upper limit can increase along with the maturation gradually of the increase of sludge concentration, bacterial classification;
COD: although anaerobic ammonia oxidizing bacteria is chemoautotrophic bacteria, can better realize the synergy (de-COD) with denitrifying bacteria; It is generally acknowledged that COD is little on its system stability impact in 200mg/L left and right;
2. enter anoxic reacter through the waste water of Anammox processing, anti-nitration reaction is to complete at anoxic reacter, it is the biotransformation being completed by denitrifying bacterium, under anoxia condition, the nitrite nitrogen of nitrated generation and nitrate nitrogen are reduced into gaseous nitrogen (N by denitrifying bacterium
2);
Anoxic reacter is airtight container or pond; Under anoxia condition, complete, complete bio-transformation by denitrifying bacterium;
Denitrification bacterial strain (being denitrifying bacterium) source: bacterial strain is taken from ASBR anaerobic ammonia oxidation reactor active sludge, when there is Anammox effect in reactor, NO
3--N accumulating value is extremely low, infers in reactor and exists Anammox effect that denitrification is also occurring simultaneously; Choose a small amount of active sludge, obtain having the denitrification bacterial strain of efficient denitrification carbon elimination ability by separation and purification;
Strain name: order-checking obtains the part 16SrDNA sequence that length is 1408bp to bacterial strain, obtained bacterial strain sequence is committed in GenBank and is retrieved by Blast, application Mega software, grow tree with Neighbor-Joining method drawing system, determine that bacterial strain thinks that part belongs to Rhodopseudomonas (Pseudomonas sp.);
Reaction conditions: the culture condition fundamental sum anaerobic ammonia oxidizing bacteria of denitrifying bacteria is similar, this is also that both can realize better collaborative reason; Difference shows that denitrifying bacteria has stronger avidity to higher COD, oxygen to its restraining effect a little less than compared with anaerobic ammonia oxidizing bacteria many;
4. enter aerobic reactor through anoxic reacter waste water after treatment, in aerobic reactor, by heterotrophic microorganism bacterium degradation of organic substances, make COD meet discharge index and require [discharge index is 100mg/L (GB8978-1996)];
Aerobic biodegradation method is to make good use of oxygen animalcule (comprising aerobic-anaerobic microbe) to carry out biological metabolism with degradation of organic substances under the condition that has oxygen to exist, and makes its stable, innoxious treatment process; Participate in the different oxygen animalcule (heterotrophic microorganism bacterium) of a great variety of this process of aerobic degradation organism;
Aerobic reactor adopts gallery type plug-flow reactor, and reactor is container or pond, and aeration, oxygen supply are set in reactor, passes through heterotrophic microorganism bacterium degradation of organic substances in aerobic reactor;
Aerobic reaction condition is as follows:
The nutritive props of microorganism: to microorganism, carbon, nitrogen, phosphorus nutrition have certain ratio, are generally BOD
5: N:P=100:5:1;
Temperature: the many genus of microorganism (the being heterotrophic microorganism bacterium) mesophilic microorganism in aerobe processing, the optimum temperature range of its growth and breeding is 20-37 DEG C;
PH: the appropriate pH in activated sludge process aeration tank is 6.5-8.5;
Dissolved oxygen (DO): the dissolved oxygen of aerobe processing is generally advisable with 2-3mg/L;
4. enter settling tank through aerobic reaction waste water after treatment, the Main Function of settling tank is that active sludge precipitation is back to aerobic reactor, and residual active sludge is outward transport after dehydration, to ensure the amount of aerobe treating part microorganism;
5. pass through primary water qualified discharge or the reuse of settling tank processing.
In anaerobic ammonia oxidation reactor, adopt anaerobic ammonia oxidizing bacteria, in denitrification reactor, adopt denitrifying bacteria, in aerobe treatment reactor, adopt heterotrophic microorganism bacterium.
Described biochemical treatment section, the biochemical bacterium adopting (being anaerobic ammonia oxidizing bacteria, denitrifying bacteria, heterotrophic microorganism bacterium), can bear high salinity, process Cl in water-concentration be 2000～20000ppm.
Having the Anammox bacterial classification of having a liking for salt characteristic can obtain by following two approach:
1. directly get part ocean bed mud (having a large amount of anaerobic ammonia oxidizing bacterias in seabed);
2. from fresh water environment, get mud, progressively tame anaerobic ammonia oxidizing bacteria by adding salinity, make it have salt tolerance.
We are mainly Anammox bacteriaum KU2 through qualification by the bacterial classification of inoculation at present, are in the anaerobically digested sludge by choosing in certain sewage work, obtain through screening.
This technique is specifically designed to processes desulfurizer waste water, is particularly useful for being provided with at desulfurizer front end the desulfurization wastewater of Wingdale-gypsum system generation of equipment for denitrifying flue gas.
The present invention not additional carbon and table shown in envrionment conditions under, can efficiently remove the ammonia nitrogen in waste water, clearance reaches more than 85%.
Desulfurization wastewater enters water condition
Claims (4)
1. the materialization of flue gas desulfurization waste-water and a biochemical combined treatment device, is characterized in that it comprises waste water Buffer Pool, apparatus for physical Chemical treating, intermediate water tank and biochemical treatment apparatus; The waste water delivery port of waste water Buffer Pool is connected with the input terminus of apparatus for physical Chemical treating by pipeline; The output terminal of apparatus for physical Chemical treating is connected with the input aperture of intermediate water tank, and the delivery port of intermediate water tank is connected with the input terminus of biochemical treatment apparatus by pipeline.
2. the materialization of a kind of flue gas desulfurization waste-water according to claim 1 and biochemical combined treatment device, is characterized in that: during apparatus for physical Chemical treating comprises and case, sludge box, flocculation tanks, concentrated/settler; In be connected with the input aperture of case and the waste water delivery port of waste water Buffer Pool; In be connected with the input aperture of sludge box by pipeline with the waste water delivery port of case, the waste water delivery port of sludge box is connected with the input aperture of flocculation tanks by pipeline, the delivery port of flocculation tanks is connected with the input aperture of concentrated/settler by pipeline, concentrated/settler flows automatically to the intermediate water tank of next stage by overflow mode, the mud discharging mouth of concentrated/settler is taken away and sent into sludge treating system by pipeline, pump.
3. the materialization of a kind of flue gas desulfurization waste-water according to claim 1 and biochemical combined treatment device, is characterized in that: biochemical treatment apparatus comprises anaerobic ammonia oxidation reactor, anoxic reacter, aerobic reactor and settling tank; The input aperture of anaerobic ammonia oxidation reactor is connected with the delivery port of intermediate water tank, the delivery port of anaerobic ammonia oxidation reactor is connected with the input aperture of anoxic reacter by pipeline, the delivery port of anoxic reacter is connected with the input aperture of aerobic reactor by pipeline, the delivery port of aerobic reactor is connected with the input aperture of settling tank by pipeline, and settling tank is provided with primary water discharge outlet, activated sludge discharged mouth.
4. the materialization of a kind of flue gas desulfurization waste-water according to claim 1 and biochemical combined treatment device, is characterized in that: the pipeline being connected with the input terminus of apparatus for physical Chemical treating is provided with valve and pump.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104944635A (en) * | 2015-06-08 | 2015-09-30 | 中国石油集团工程设计有限责任公司 | High-concentration mercury-containing gas field wastewater treatment method |
| CN106630027A (en) * | 2016-12-30 | 2017-05-10 | 华北电力大学（保定） | Method and system for treating high-chlorine desulfurization waste water by electrolytic method and performing flue gas mercury pollution control |
| WO2017133513A1 (en) * | 2016-02-05 | 2017-08-10 | 大唐环境产业集团股份有限公司 | Treatment apparatus and method for softening desulfurization wastewater |
| WO2017133514A1 (en) * | 2016-02-05 | 2017-08-10 | 大唐环境产业集团股份有限公司 | Treatment apparatus and method for softening desulfurization wastewater |
| CN113024011A (en) * | 2019-12-24 | 2021-06-25 | 中冶京诚工程技术有限公司 | Method and device for treating wastewater of activated carbon desulfurization and denitrification system |
-
2014
- 2014-03-12 CN CN201420111270.5U patent/CN203754565U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104944635A (en) * | 2015-06-08 | 2015-09-30 | 中国石油集团工程设计有限责任公司 | High-concentration mercury-containing gas field wastewater treatment method |
| WO2017133513A1 (en) * | 2016-02-05 | 2017-08-10 | 大唐环境产业集团股份有限公司 | Treatment apparatus and method for softening desulfurization wastewater |
| WO2017133514A1 (en) * | 2016-02-05 | 2017-08-10 | 大唐环境产业集团股份有限公司 | Treatment apparatus and method for softening desulfurization wastewater |
| CN106630027A (en) * | 2016-12-30 | 2017-05-10 | 华北电力大学（保定） | Method and system for treating high-chlorine desulfurization waste water by electrolytic method and performing flue gas mercury pollution control |
| CN113024011A (en) * | 2019-12-24 | 2021-06-25 | 中冶京诚工程技术有限公司 | Method and device for treating wastewater of activated carbon desulfurization and denitrification system |
| CN113024011B (en) * | 2019-12-24 | 2024-01-26 | 中冶京诚工程技术有限公司 | Method and device for treating wastewater of active carbon desulfurization and denitrification system |
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