CN106746226A - A kind of processing method and processing device of F- T synthesis waste water - Google Patents
A kind of processing method and processing device of F- T synthesis waste water Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 74
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 46
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 43
- 238000003672 processing method Methods 0.000 title claims abstract description 32
- 238000012545 processing Methods 0.000 title claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 103
- 238000011282 treatment Methods 0.000 claims abstract description 90
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 42
- 239000012528 membrane Substances 0.000 claims abstract description 38
- 230000003647 oxidation Effects 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 238000000034 method Methods 0.000 claims abstract description 30
- 230000001112 coagulating effect Effects 0.000 claims abstract description 22
- 238000005345 coagulation Methods 0.000 claims abstract description 21
- 230000015271 coagulation Effects 0.000 claims abstract description 21
- 230000008569 process Effects 0.000 claims abstract description 19
- 238000005188 flotation Methods 0.000 claims abstract description 10
- 238000007667 floating Methods 0.000 claims abstract description 8
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 6
- 230000033228 biological regulation Effects 0.000 claims description 6
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 6
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical group O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 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
- 239000002033 PVDF binder Substances 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 239000004411 aluminium Substances 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052593 corundum Inorganic materials 0.000 claims description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 239000002131 composite material Substances 0.000 claims description 2
- 239000003814 drug Substances 0.000 claims description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 claims 1
- 239000003610 charcoal Substances 0.000 claims 1
- 239000003921 oil Substances 0.000 description 33
- 239000005416 organic matter Substances 0.000 description 20
- 239000000725 suspension Substances 0.000 description 20
- 238000006243 chemical reaction Methods 0.000 description 19
- 239000000126 substance Substances 0.000 description 18
- 239000010802 sludge Substances 0.000 description 17
- 239000003208 petroleum Substances 0.000 description 15
- 241000196324 Embryophyta Species 0.000 description 13
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 11
- 238000005842 biochemical reaction Methods 0.000 description 11
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 230000008859 change Effects 0.000 description 6
- 238000006396 nitration reaction Methods 0.000 description 6
- 230000020477 pH reduction Effects 0.000 description 6
- 238000004220 aggregation Methods 0.000 description 5
- 230000002776 aggregation Effects 0.000 description 5
- 239000000839 emulsion Substances 0.000 description 5
- 229920002521 macromolecule Polymers 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 150000003384 small molecules Chemical class 0.000 description 5
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 229920002401 polyacrylamide Polymers 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 241000372132 Hydrometridae Species 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004308 accommodation Effects 0.000 description 1
- 230000000703 anti-shock Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses a kind of processing method and processing device of F- T synthesis waste water.The treating method comprises following steps：(1) pre-process：Carry out stripping treatment or stripping treatment, the first coagulating treatment and air-flotation process successively to F- T synthesis waste water, collect the first water outlet；(2) biochemical treatment：Carry out Anaerobic Treatment and A/O biological contact oxidization treatments successively to first water outlet, collect the second water outlet；(3) advanced treating：Second coagulating treatment and membrane separation are carried out successively to second water outlet, water outlet up to standard is obtained.Described device includes the stripper plant or stripping device, the first coagulation device, air-floating apparatus, anaerobic processing device, A/O biological contact oxidation plants, the second coagulation device and membrane separation device that are sequentially communicated.By above-mentioned treating method and apparatus, the effluent quality and capacity of resisting impact load of F- T synthesis waste water are improve, while processing cost is low.
Description
Technical field
The invention belongs to technical field of waste water processing, and in particular to a kind of processing method and processing device of F- T synthesis waste water.
Background technology
In China's energy resources distribution, petroleum resources are relatively fewer, and the solid fuel resource such as coal or biomass is richer
Richness, in order to reduce the degree of dependence to foreign oil market, the solid fuel such as resourceful coal or biomass resource is turned
It is one of important channel of solution China's oil scarcity of resources to turn to liquid fuel.In above-mentioned conversion process, F- T synthesis are anti-
Should be core reaction therein, the various organic oxygen-containing compounds of association in course of reaction, while often producing one ton of oil will be about companion
Raw water more than one ton, the water can neither directly as discharge of wastewater, can not direct circulation utilize, it is necessary to it is processed.
Therefore, how to purify, recycle this part water, either from the angle of saving water resource, or from environmental protection
Angle is set out, and is all had very important significance.
At present, the processing method of F- T synthesis waste water essentially consists in recovery high value organic matter, but not high to reclaiming
Waste water after value organic matter is further processed, it is difficult to reach the purpose for reclaiming completely and utilizing of resource.On overcoming
Defect is stated, prior art employs to separate F- T synthesis waste water is processed with the group technology of oxidation, such as Chinese patent text
Offer CN101190821A and disclose a kind of processing method of F-T synthesis reaction water.The processing method first passes through cohesion or air supporting
Oil removing, realizes the water-oil separating in reaction water, and oil phase is reclaimed；The reaction water after point oil is divided into by multiple-effect evaporation technology again poor
Low concentration of water containing organic matter and the high concentration water rich in organic matter；Then low concentration of water passes through membrane separation technique or biochemical treatment
To remove organic matter therein, water can reuse；Finally, high concentration water passes through cohesion or oil removal by air bubbling to realize water-oil separating, oil
Mutually recyclable, water mutually can carry out biochemical treatment or for synthesis gas production technology.Above-mentioned processing method can be by F-T synthesis reaction
Most of organic matter in waste water can be carried out trans-utilization or directly recovery by Water circulation in production, realize the resource of waste
Utilize.
When above-mentioned technology carries out low concentration of water and high concentration water's separation to Fischer-Tropsch synthesis reaction water, multiple-effect evaporation skill is employed
Art, the operation energy consumption is big, high cost.Furthermore, only by membrane separation technique or biochemical treatment, high concentration water only passes through low concentration of water
Water-oil separating, biochemical treatment, it is difficult to which hardly degraded organic substance therein of degrading, effluent quality is poor.Meanwhile, above-mentioned technology uses profit
The group technology of separation, multiple-effect evaporation, biochemical treatment and UF membrane, in face of the larger F- T synthesis waste water of change of water quality
When, its capacity of resisting impact load is poor.
The content of the invention
Therefore, to be solved by this invention is that the processing method of F- T synthesis waste water has effluent quality and shock resistance is negative
The defect of lotus ability, and then the Fischer-Tropsch good there is provided a kind of effluent quality, capacity of resisting impact load is strong and processing cost is low
The processing method and processing device of synthetic wastewater.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：
The processing method of F- T synthesis waste water provided by the present invention, comprises the following steps：
(1) pre-process：Carry out stripping treatment or stripping treatment, the first coagulating treatment and air supporting successively to F- T synthesis waste water
Treatment, collects the first water outlet；
(2) biochemical treatment：Carry out Anaerobic Treatment and A/O biological contact oxidization treatments successively to first water outlet, collect
Second water outlet；
(3) advanced treating：Second coagulating treatment and membrane separation are carried out successively to second water outlet, obtain it is up to standard go out
Water.
Preferably, in step (2), the Anaerobic Treatment is carried out in anaerobic combined reactor.
Preferably, in step (3), the membrane separation is membrane bioreactor (MBR) treatment.
Further, in step (1), before first coagulating treatment, also including entering to the F- T synthesis waste water
The step of row homogeneous measures regulation.
Preferably, in step (3), after second water outlet carries out second coagulating treatment, at the UF membrane
Before reason, also including carrying out ozone Oxidation Treatment to second water outlet the step of.
Preferably, in step (1), also including collecting the stripping treatment or stripping treatment with air-flotation process gained oil
The step of phase；
In step (2), also including reclaiming the Anaerobic Treatment gained biogas the step of.
Further, when first coagulating treatment and second coagulating treatment is carried out, the medicament for being added is poly-
Close at least one in aluminium chloride, polyaluminium sulfate, poly-ferric chloride, bodied ferric sulfate and polyacrylamide；
When the ozone Oxidation Treatment is carried out, catalyst is additionally added, the catalyst is MnO2、Al2O3、Fe2O3、TiO2
With at least one in activated carbon.
Present invention also offers the processing unit for above-mentioned processing method, it is characterised in that including the vapour being sequentially communicated
Carry device or stripping device, the first coagulation device, air-floating apparatus, anaerobic processing device, A/O biological contact oxidation plants, second
Coagulation device and membrane separation device.
Preferably, the anaerobic processing device is anaerobic combined reactor；
The membrane separation device is membrane bioreactor.
Further, also including ozone Oxidation Treatment device, its water inlet and delivery port are filled with second coagulation respectively
The delivery port put is connected with the water inlet of the membrane separation device；
Regulating reservoir, the delivery port of the regulating reservoir is connected with the water inlet of the stripper plant or the stripping device；
The membrane bioreactor uses the Flat Membrane MBR of PVDF materials.
Compared with prior art, the present invention has the advantages that：
(1) processing method of the F- T synthesis waste water that the embodiment of the present invention is provided, first carries out vapour to F- T synthesis waste water
Treatment or stripping treatment are proposed, the stronger lower alcohol of part volatility, acid is taken away, breaks F- T synthesis waste water original flat
Weighing apparatus state, can effectively realize the separation for dissolving oily substance contained in water, beneficial to being smoothed out for subsequent technique, while stripping
Or stripping reclaim lower alcohol, acid can be directly entered subsequent biochemical treatment in；The first coagulating treatment is carried out to it again, is made
Organic matter aggregation therein；Oils therein (such as oil slick and oil emulsion) and suspension are isolated by air-flotation process again, is collected
First water outlet.First water outlet carries out Anaerobic Treatment and A/O biological contact oxidization treatments successively, by the decomposition of anaerobic bacteria with
And the biochemical reaction of a series of complex, by difficult degradation macromolecule organic therein be converted into small molecule VFA and
Methane, removes most of organic matter therein, then carries out A/O biological contact oxidization treatments, by A ponds bio-contact oxidation,
Acidification hydrolization and nitration denitrification are carried out, continues to reduce wherein organic concentration, remove part ammonia nitrogen；By O ponds biological
There is aerobic biochemical reaction, most organic pollutions are degraded by biological oxidation, absorption, are collected second and are gone out for oxidation
Water.Second water outlet carries out the second coagulating treatment and membrane separation successively, while removing oil removal, removes COD and ammonia nitrogen, obtains
Arrival marks water.Above-mentioned processing method, by pretreatment, biochemical treatment and advanced treating, cooperates and acts between three,
Improve effluent quality.Furthermore, pretreatment uses the first coagulating treatment and air-flotation process, and biochemical treatment uses Anaerobic Treatment and A/
O biological contact oxidization treatments, advanced treating use the second coagulating treatment and membrane separation, can effectively water quality treatment change greatly
F- T synthesis waste water, with strong capacity of resisting impact load, while using evaporation or need not distill, reduce that energy consumption is big and place
Reason cost, after tested, the pH of effluent quality is 6-9, COD≤50mg/L, BOD≤5mg/L, and petroleum substance≤5mg/L suspends
Thing≤1mg/L.
(2) processing method of the F- T synthesis waste water that the embodiment of the present invention is provided, before the first coagulating treatment, to taking
Support synthetic wastewater carries out homogeneous and measures regulation, stabilizes influent quality, further increases the anti-shock loading of the processing method
Ability；Before membrane separation is carried out, ozone Oxidation Treatment is carried out to the second water outlet, by the oxidation of difficult degradation larger molecular organicses
It is biochemical small organic molecule, improves the biodegradability of the second water outlet.
(3) processing method of the F- T synthesis waste water that the embodiment of the present invention is provided, can tackle the big amplitude variation of influent quality
Change, such as COD rises violently or rapid drawdown in influent quality, can be run well under excess load or underload, be not in system crash or
Effluent quality situation not up to standard, after testing, its influent quality COD accommodations can reach 8500-45000mg/L, in short-term
Between maximum can reach 70000mg/L.
(4) processing method of the F- T synthesis waste water that the embodiment of the present invention is provided, has reclaimed stripping, air-flotation process gained
Oil phase, has reclaimed Anaerobic Treatment gained biogas, has reclaimed volatile component, has obtained water outlet up to standard, and water outlet up to standard can also be returned
With realizing the recycling of resource.
(5) processing method of the F- T synthesis waste water that the embodiment of the present invention is provided, Anaerobic Treatment is in anaerobic composite bed
Carried out in reactor, improve the effect of Anaerobic Treatment；Membrane separation uses the flat board of PVDF materials using MBR treatment, MBR
Film MBR, overcomes the fracture of wire problem of doughnut MBR, and safety and reliability is higher, while having effluent quality excellent steady again
Fixed, floor space is small, simple operation and other advantages.
(6) processing unit of the F- T synthesis waste water that the embodiment of the present invention is provided, outlet effect simple with device
Well, the characteristics of capacity of resisting impact load is strong, can effectively process Fischer-Tropsch synthetic wastewater, and the effluent quality after treatment is good.
Brief description of the drawings
In order to illustrate more clearly of the specific embodiment of the invention or technical scheme of the prior art, below will be to specific
The accompanying drawing to be used needed for implementation method or description of the prior art is briefly described, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the processing unit of F- T synthesis waste water in the embodiment of the present invention.
Reference：
1- regulating reservoirs；2- is stripped or stripping device；The coagulation devices of 3- first；4- air-floating apparatus；5- anaerobic processing devices；6-
A/O biological contact oxidation plants；The coagulation devices of 7- second；8- ozone Oxidation Treatment devices；9- membrane separation devices.
Specific embodiment
In order to the object, technical solutions and advantages of the present invention are better described, below in conjunction with specific embodiment to this hair
It is bright to be described further.The present invention can be embodied in many different forms, and should not be construed as limited to set forth herein
Embodiment.Conversely, there is provided these embodiments so that the disclosure will be thorough and complete, and will it is of the invention design fill
Divide and convey to those skilled in the art, the present invention will only be defined by the appended claims.
Embodiment 1
Present embodiments provide a kind of processing method of F- T synthesis waste water.The treating method comprises following steps：
(1) F- T synthesis waste water removes volatile component into stripping treatment is carried out in stripper plant；First is entered back into mix
In solidifying device, the dosage of aluminium polychloride therein is 250mg/L, assembles organic matter therein, after aggregation terminates, then
Transfer them to and carry out in air-floating apparatus air-flotation process, the oils in separation and recovery waste water, such as oil slick and oil emulsion, and suspend
Thing, collects the first water outlet, controls pneumatically supported dissolved-air pressure 0.4MPa, flow 0.3L/min, wherein residence time 30min, Fischer-Tropsch
The pH of synthetic wastewater is that 4.5, COD is that 32000mg/L, BOD are that 5300mg/L, petroleum substance are that 360mg/L, suspension are
230mg/L, after measured, the COD of the first water outlet is that 1590mg/L, petroleum substance are 36mg/L, suspend for 8490mg/L, BOD
Thing is 20mg/L；
(2) first water outlets into carrying out anaerobic reaction in anaerobic processing device, the organic matter in the first water outlet and anaerobism
Grain sludge is fully contacted, and is decomposed by anaerobic bacteria and utilized, and by the biochemical reaction of a series of complex, macromolecule organic is converted into
The VFA and methane of small molecule, remove most of organic matter therein, and the biogas produced during anaerobic reaction can
To recycle, wherein, anaerobic reaction state modulator hydraulic detention time 64h, sludge concentration 5000mg/L；
The first water outlet after Anaerobic Treatment into A/O biological contact oxidation plants carrying out at A/O bio-contact oxidations
Reason, what it was introduced into is A ponds, carries out acidification hydrolization and nitration denitrification, reduces organic concentration, removes part ammonia nitrogen, waste water
Hydraulic detention time wherein is 27h；Flowing into O ponds again carries out aerobic biochemical reaction, waste water hydraulic detention time wherein
It is 78h, by biological oxidation and Adsorption overwhelming majority organic pollution, collects the second water outlet, after measured, the second water outlet
COD be 1100mg/L, BOD be 100mg/L, petroleum substance be 20mg/L, suspension be 20mg/L；
(3) to enter the second coagulation device in the second water outlet in add polyaluminium sulfate and poly-ferric chloride, dosage
Respectively 20mg/L and 15mg/L, further removes oil removal after coagulating sedimentation；Enter back into and carry out depth in membrane separation device
Biochemical treatment, waste water hydraulic detention time wherein is 30h, and sludge concentration is 8000mg/L, removal COD, ammonia nitrogen and suspension
Thing, obtains water outlet up to standard, and after measured, the pH of water outlet up to standard is that 47mg/L, BOD are that 3mg/L, petroleum substance are for 7.2, COD
3.5mg/L, suspension are 0mg/L.
Embodiment 2
Present embodiments provide a kind of processing method of F- T synthesis waste water.The treating method comprises following steps：
(1) F- T synthesis waste water measures regulation into carrying out homogeneous in regulating reservoir；Subsequently enter and carry out vapour in stripper plant
Treatment is proposed, volatile component is removed, stripping gas flow is 0.3m in controlling stripping to process3/L；Enter back into the first coagulation device
In, the dosage of aluminium polychloride therein is 200mg/L, the dosage of polyacrylamide is 4mg/L, is made organic in waste water
Thing is assembled, and after aggregation terminates, then transfers them to and carry out in air-floating apparatus air-flotation process, controls pneumatically supported dissolved-air pressure
0.3MPa, flow 0.2L/min, residence time 30min, the oils in separation and recovery waste water, such as oil slick and oil emulsion, and it is outstanding
Float, collects the first water outlet, and the wherein pH of F- T synthesis waste water is that 4, COD is that 45000mg/L, BOD are 5800mg/L, petroleum-type
Material is 400mg/L, suspension is 250mg/L, and after measured, the COD of the first water outlet is that 9585mg/L, BOD are 1880mg/L, stone
Oily substance is 40mg/L, suspension is 25mg/L；
(2) first water outlets into carrying out anaerobic reaction in anaerobic processing device, the organic matter in the first water outlet and anaerobism
Grain sludge is fully contacted, and is decomposed by anaerobic bacteria and utilized, and by the biochemical reaction of a series of complex, macromolecule organic is converted into
The VFA and methane of small molecule, remove most of organic matter therein, and the biogas produced during anaerobic reaction can
To recycle, wherein, anaerobic reaction state modulator hydraulic detention time 66h, sludge concentration 4000mg/L；
The first water outlet after Anaerobic Treatment into A/O biological contact oxidation plants carrying out at A/O bio-contact oxidations
Reason, what it was introduced into is A ponds, carries out acidification hydrolization and nitration denitrification, reduces organic concentration, removes part ammonia nitrogen, waste water
Hydraulic detention time wherein is 25h；Flowing into O ponds again carries out aerobic biochemical reaction, waste water hydraulic detention time wherein
It is 80h, by biological oxidation and Adsorption overwhelming majority organic pollution, collects the second water outlet, sludge is dense in A ponds and O ponds
Degree 4000mg/L, after measured, the COD of the second water outlet is that 276mg/L, petroleum substance are 22mg/L, outstanding for 1500mg/L, BOD
Float is 25mg/L；
Into oxidation processes are carried out in ozone Oxidation Treatment device, the dosage of ozone is 40mg/L for (3) second water outlets, and
It has been added to MnO2, catalytic action is played, difficult degradation larger molecular organicses are oxidized to by biochemical small point by ozone
Sub- organic matter, improves the biodegradability of waste water；In subsequently entering the second coagulation device, wherein there is the polymerization that dosage is 10mg/L
The poly-ferric chloride of ferric sulfate and 6mg/L；Oil removal is further removed after coagulating sedimentation；Enter back into and carry out in membrane separation device
Deep biochemical treatment, waste water hydraulic detention time wherein be 27h, sludge concentration is 7000mg/L, removal COD, ammonia nitrogen and
Suspension, obtains water outlet up to standard, and after measured, the pH of water outlet up to standard is that 7.0, COD is that 40mg/L, BOD are 1mg/L, petroleum-type thing
Matter is 2mg/L, suspension is 0mg/L.
Embodiment 3
Present embodiments provide a kind of processing method of F- T synthesis waste water.The treating method comprises following steps：
(1) F- T synthesis waste water measures regulation into carrying out homogeneous in regulating reservoir；Subsequently enter and blown in stripping device
De- treatment, removes volatile component, in entering back into the first coagulation device, the dosage of aluminium polychloride therein is 150mg/L,
The dosage of polyacrylamide is 3mg/L, assembles the organic matter in waste water, after aggregation terminates, then transfers them to air supporting
Air-flotation process is carried out in device, pneumatically supported dissolved-air pressure 0.4MPa, flow 0.2L/min, residence time 25min is controlled, separated back
The oils in waste water, such as oil slick and oil emulsion, and suspension are received, the first water outlet is collected, the pH of wherein F- T synthesis waste water is
5th, COD be 8500mg/L, BOD be 2000mg/L, petroleum substance be 80mg/L, suspension be 50mg/L, after measured, first goes out
The COD of water be 5440mg/L, BOD be 1070mg/L, petroleum substance be 16mg/L, suspension be 15mg/L；
(2) first water outlets into carrying out anaerobic reaction in anaerobic processing device, the organic matter in the first water outlet and anaerobism
Grain sludge is fully contacted, and is decomposed by anaerobic bacteria and utilized, and by the biochemical reaction of a series of complex, macromolecule organic is converted into
The VFA and methane of small molecule, remove most of organic matter therein, and the biogas produced during anaerobic reaction can
To recycle, wherein, anaerobic reaction state modulator hydraulic detention time 68h, sludge concentration 3500mg/L；
The first water outlet after Anaerobic Treatment into A/O biological contact oxidation plants carrying out at A/O bio-contact oxidations
Reason, what it was introduced into is A ponds, carries out acidification hydrolization and nitration denitrification, reduces organic concentration, removes part ammonia nitrogen, waste water
Hydraulic detention time wherein is 26h；Flowing into O ponds again carries out aerobic biochemical reaction, waste water hydraulic detention time wherein
It is 82h, by biological oxidation and Adsorption overwhelming majority organic pollution, collects the second water outlet, sludge is dense in A ponds and O ponds
Degree 5000mg/L, after measured, the COD of the second water outlet is that 30mg/L, petroleum substance are 12mg/L, suspension for 50mg/L, BOD
It is 15mg/L；
(3) second water outlets enter in the second coagulation device, wherein having bodied ferric sulfate and 2mg/ that dosage is 180mg/L
The poly-ferric chloride of L；Oil removal is further removed after coagulating sedimentation；Enter back into and carry out at deep biochemical in membrane separation device
Reason, waste water hydraulic detention time wherein is 25h, and sludge concentration is 6000mg/L, removal COD, ammonia nitrogen and suspension, is obtained
Water outlet up to standard, after measured, the pH of water outlet up to standard is that 16mg/L, BOD are that 6mg/L, petroleum substance are 1mg/L, outstanding for 7.5, COD
Float is 0mg/L.
Embodiment 4
Present embodiments provide a kind of processing method of F- T synthesis waste water.The treating method comprises following steps：
(1) F- T synthesis waste water measures regulation into carrying out homogeneous in regulating reservoir；Subsequently enter and carry out vapour in stripper plant
Treatment is proposed, volatile component is removed, stripping gas flow is 0.3m in controlling stripping to process3/L；Enter back into the first coagulation device
In, the dosage of bodied ferric sulfate therein is 250mg/L, the dosage of polyacrylamide is 6mg/L, is made organic in waste water
Thing is assembled, and after aggregation terminates, then transfers them to and carry out in air-floating apparatus air-flotation process, controls pneumatically supported dissolved-air pressure
0.2MPa, flow 0.4L/min, residence time 25min, the oils in separation and recovery waste water, such as oil slick and oil emulsion, and it is outstanding
Float, collects the first water outlet, and the wherein pH of F- T synthesis waste water is that 3, COD is that 25000mg/L, BOD are 3200mg/L, petroleum-type
Material is 225mg/L, suspension is 140mg/L, and after measured, the COD of the first water outlet is that 4120mg/L, BOD are 770mg/L, stone
Oily substance is 25mg/L, suspension is 15mg/L；
(2) first water outlets into carrying out anaerobic reaction in anaerobic processing device, the organic matter in the first water outlet and anaerobism
Grain sludge is fully contacted, and is decomposed by anaerobic bacteria and utilized, and by the biochemical reaction of a series of complex, macromolecule organic is converted into
The VFA and methane of small molecule, remove most of organic matter therein, and the biogas produced during anaerobic reaction can
To recycle, wherein, anaerobic reaction state modulator hydraulic detention time 68h, sludge concentration 3500mg/L；
The first water outlet after Anaerobic Treatment into A/O biological contact oxidation plants carrying out at A/O bio-contact oxidations
Reason, what it was introduced into is A ponds, carries out acidification hydrolization and nitration denitrification, reduces organic concentration, removes part ammonia nitrogen, waste water
Hydraulic detention time wherein is 22h；Flowing into O ponds again carries out aerobic biochemical reaction, waste water hydraulic detention time wherein
It is 78h, by biological oxidation and Adsorption overwhelming majority organic pollution, collects the second water outlet, sludge is dense in A ponds and O ponds
Degree 4000mg/L, after measured, the COD of the second water outlet is that 150mg/L, petroleum substance are 20mg/L, suspend for 800mg/L, BOD
Thing is 15mg/L；
Into oxidation processes are carried out in ozone Oxidation Treatment device, the dosage of ozone is 35mg/L for (3) second water outlets, and
It has been added to Al2O3, catalytic action is played, difficult degradation larger molecular organicses are oxidized to by biochemical small point by ozone
Sub- organic matter, improves the biodegradability of waste water；In subsequently entering the second coagulation device, wherein there is the polymerization that dosage is 5mg/L
Iron chloride；Oil removal is further removed after coagulating sedimentation；Enter back into and carry out deep biochemical treatment in membrane separation device, waste water exists
Hydraulic detention time therein is 20h, and sludge concentration is 6500mg/L, removal COD, ammonia nitrogen and suspension, obtains water outlet up to standard,
After measured, the pH of water outlet up to standard is that 7.2, COD is that 42mg/L, BOD are that 2mg/L, petroleum substance are that 2mg/L, suspension are
0mg/L。
Embodiment 5
Present embodiments provide a kind of processing unit of F- T synthesis waste water.As shown in figure 1, it includes the vapour being sequentially communicated
Carry device 2 or stripping device, the first coagulation device 3, air-floating apparatus 4, anaerobic processing device 5, A/O biological contact oxidation plants 6,
Second coagulation device 7 and membrane separation device 9, in the present embodiment, anaerobic processing device 5 is anaerobic combined reactor, film point
It is membrane bioreactor from device 9.
Above-mentioned processing unit, simple structure, capacity of resisting impact load is strong, Fischer-Tropsch synthetic wastewater can be effectively processed, after treatment
Effluent quality it is good.
On the basis of above-mentioned technical proposal, also including ozone Oxidation Treatment device 8, its water inlet and delivery port respectively with
The delivery port of the second coagulation device 7 is connected with the water inlet of membrane separation device 9；
Regulating reservoir 1, the delivery port of regulating reservoir 1 is connected with the water inlet of stripper plant 2 or stripping device；
Preferably, membrane bioreactor uses the Flat Membrane MBR of PVDF materials.
Comparative example 1
This comparative example provides a kind of processing method of F- T synthesis waste water.The treating method comprises following steps：
(1) F- T synthesis waste water is into carrying out anaerobic reaction in anaerobic processing device, wherein, anaerobic reaction state modulator water
Power residence time 58h, sludge concentration 5000mg/L；
Waste water after Anaerobic Treatment into A/O biological contact oxidation plants to carry out A/O biological contact oxidization treatments, its
What is be introduced into is A ponds, carries out acidification hydrolization and nitration denitrification, reduces organic concentration, removes part ammonia nitrogen, and waste water is wherein
Hydraulic detention time be 30h；Flowing into O ponds again carries out aerobic biochemical reaction, and waste water hydraulic detention time wherein is 75h,
Water outlet is collected, the wherein pH of F- T synthesis waste water is that 4.5, COD is that 32000mg/L, BOD are that 5300mg/L, petroleum substance are
360mg/L, suspension are 230mg/L；
(2) to polyaluminium sulfate and poly-ferric chloride is added in the waste water entered in coagulation device, dosage is respectively
220mg/L and 15mg/L；Enter back into and carry out deep biochemical treatment in membrane separation device, waste water hydraulic detention time wherein is
30h, sludge concentration is 8000mg/L, obtains water outlet, after measured, the pH of water outlet for 5, COD be 500mg/L, BOD be 90mg/L,
Petroleum substance is 130mg/L, suspension is 120mg/L.
Obviously, above-described embodiment is only intended to clearly illustrate example, and not to the restriction of implementation method.It is right
For those of ordinary skill in the art, can also make on the basis of the above description other multi-forms change or
Change.There is no need and unable to be exhaustive to all of implementation method.And the obvious change thus extended out or
Among changing still in the protection domain of the invention.
Claims (10)
1. a kind of processing method of F- T synthesis waste water, comprises the following steps：
(1) pre-process：F- T synthesis waste water is carried out successively at stripping treatment or stripping treatment, the first coagulating treatment and air supporting
Reason, collects the first water outlet；
(2) biochemical treatment：Carry out Anaerobic Treatment and A/O biological contact oxidization treatments successively to first water outlet, collect second
Water outlet；
(3) advanced treating：Second coagulating treatment and membrane separation are carried out successively to second water outlet, water outlet up to standard is obtained.
2. processing method according to claim 1, it is characterised in that in step (2), the Anaerobic Treatment is multiple in anaerobism
Carried out in conjunction bed reactor.
3. processing method according to claim 1 and 2, it is characterised in that in step (3), the membrane separation is MBR
Treatment.
4. the processing method according to any one of claim 1-3, it is characterised in that in step (1), it is mixed described first
Before solidifying treatment, the step of also measure regulation including carrying out homogeneous to the F- T synthesis waste water.
5. the processing method according to any one of claim 1-4, it is characterised in that in step (3), go out described second
Water is carried out after second coagulating treatment, before the membrane separation, also including carrying out ozone oxygen to second water outlet
The step of changing treatment.
6. the processing method according to any one of claim 1-5, it is characterised in that in step (1), also including collecting institute
The step of stripping treatment or stripping treatment are stated with air-flotation process gained oil phase；
In step (2), also including reclaiming the Anaerobic Treatment gained biogas the step of.
7. the processing method according to claim 5 or 6, it is characterised in that carrying out first coagulating treatment and described
During the second coagulating treatment, the medicament for being added is aluminium polychloride, polyaluminium sulfate, poly-ferric chloride, bodied ferric sulfate and gathers
At least one in acrylamide；
When the ozone Oxidation Treatment is carried out, catalyst is additionally added, the catalyst is MnO2、Al2O3、Fe2O3、TiO2And work
At least one in property charcoal.
8. the processing unit of the processing method being used for any one of right 1-7, it is characterised in that including the vapour being sequentially communicated
Carry device or stripping device (2), the first coagulation device (3), air-floating apparatus (4), anaerobic processing device (5), A/O biological contact oxidations
(6), the second coagulation device (7) and membrane separation device (9) are put in makeup.
9. processing unit according to claim 8, it is characterised in that the anaerobic processing device (5) is anaerobic composite bed
Reactor；
The membrane separation device (9) is membrane bioreactor.
10. the processing unit according to claim 7 or 8, it is characterised in that also including ozone Oxidation Treatment device (8), its
Water inlet and delivery port connect with the delivery port of second coagulation device (7) and the water inlet of the membrane separation device (9) respectively
It is logical；
Regulating reservoir (1), the delivery port of the regulating reservoir (1) connects with the water inlet of the stripper plant (2) or the stripping device
It is logical；
The membrane bioreactor uses the flat board MBR of PVDF materials.
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