CN103523985B - The processing means of coke-fired furnace draining, the processing method of coke-fired furnace draining - Google Patents
The processing means of coke-fired furnace draining, the processing method of coke-fired furnace draining Download PDFInfo
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- CN103523985B CN103523985B CN201310270463.5A CN201310270463A CN103523985B CN 103523985 B CN103523985 B CN 103523985B CN 201310270463 A CN201310270463 A CN 201310270463A CN 103523985 B CN103523985 B CN 103523985B
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- coke
- water
- fired furnace
- aeration tank
- draining
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Links
- 238000003672 processing method Methods 0.000 title claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 180
- 238000000926 separation method Methods 0.000 claims abstract description 121
- 238000005273 aeration Methods 0.000 claims abstract description 91
- 239000010802 sludge Substances 0.000 claims abstract description 81
- 239000000203 mixture Substances 0.000 claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 230000008595 infiltration Effects 0.000 claims abstract description 28
- 238000001764 infiltration Methods 0.000 claims abstract description 28
- 244000005700 microbiome Species 0.000 claims abstract description 16
- 239000000571 coke Substances 0.000 claims abstract description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 100
- 238000010790 dilution Methods 0.000 claims description 50
- 239000012895 dilution Substances 0.000 claims description 50
- 238000000034 method Methods 0.000 claims description 41
- 239000012528 membrane Substances 0.000 claims description 33
- 230000008569 process Effects 0.000 claims description 32
- 239000011575 calcium Substances 0.000 claims description 15
- 239000013535 sea water Substances 0.000 claims description 15
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 14
- 229910052791 calcium Inorganic materials 0.000 claims description 14
- 239000000835 fiber Substances 0.000 claims description 13
- 230000000694 effects Effects 0.000 claims description 9
- 239000011148 porous material Substances 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 238000007865 diluting Methods 0.000 claims 2
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 20
- 239000011574 phosphorus Substances 0.000 abstract description 20
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 11
- 238000011946 reduction process Methods 0.000 abstract description 4
- 230000035699 permeability Effects 0.000 abstract 1
- -1 phosphorus compound Chemical class 0.000 description 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 8
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 8
- 239000004576 sand Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000012510 hollow fiber Substances 0.000 description 6
- 235000015097 nutrients Nutrition 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 238000004062 sedimentation Methods 0.000 description 6
- 239000006228 supernatant Substances 0.000 description 6
- 239000003610 charcoal Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000002033 PVDF binder Substances 0.000 description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 238000012851 eutrophication Methods 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 125000005031 thiocyano group Chemical group S(C#N)* 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- XLYOFNOQVPJJNP-DYCDLGHISA-N deuterium hydrogen oxide Chemical compound [2H]O XLYOFNOQVPJJNP-DYCDLGHISA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 238000009287 sand filtration Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 1
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- RRTCFFFUTAGOSG-UHFFFAOYSA-N benzene;phenol Chemical compound C1=CC=CC=C1.OC1=CC=CC=C1 RRTCFFFUTAGOSG-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 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 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000011499 joint compound Substances 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- DJFBJKSMACBYBD-UHFFFAOYSA-N phosphane;hydrate Chemical compound O.P DJFBJKSMACBYBD-UHFFFAOYSA-N 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 229950000845 politef Drugs 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- ZMZDMBWJUHKJPS-UHFFFAOYSA-N thiocyanic acid Chemical compound SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
When it is an object of the invention to the active sludge treatment of coke-fired furnace draining, reduction processes the COD composition in water and total phosphorus concentration.The processing means of the coke-fired furnace draining of the present invention, it has STRENGTH ON COKE fire grate water, by microorganism in activated sludge implement biological treatment aeration tank, in aeration tank through the processed water of biological treatment, implement the membrance separation portion that solid-liquid separation processes and the COD composition removing unit removed by COD composition contained in the infiltration water of permeability and separation film in membrance separation portion by separating film.
Description
Technical field
The present invention relates to water treatment facilities and the processing method of coke-fired furnace draining of coke fire grate.
Background technology
In the past, made the coke-fired furnace draining discharged by coke-fired furnace flow in drainage treatment equipment, made it by activated sludge
Innoxious.
Usually, coke-fired furnace draining contains the ammonia (NH being derived from coke raw material coal4), cyanogen (CN), thiocyano
(SCN), phenol etc. have the composition of bio-toxicity.Therefore, when coke-fired furnace draining at that time flows in aeration tank,
In order to lighten the load, it is diluted by dilution water.
Such as, patent documentation 1 has been recorded a kind of activated sludge treatment method, in Jiang Yuanshui imports to aeration tank
It is carried out continuously in the method for active sludge treatment, water for industrial use is flowed in aeration tank as dilution water with sea water.
Prior art literature
Patent documentation
Patent documentation 1: Japanese Patent Laid-Open 2005-46697 publication
Summary of the invention
The problem that invention is to be solved
But, in the active sludge treatment of coke-fired furnace draining, generally, treated process water quilt in aeration tank
Delivering in stillpot, be separated into mud and supernatant, supernatant removes impurity at sand tower further, in activity
The removing of charcoal tower is scaled the oxidability material of COD (COD) and (is designated as " COD composition " below.).
But, in aeration tank, although contain in coke-fired furnace draining is scaled BOD's (biochemical oxygen demand)
Organic substance (is designated as " BOD composition " below.) major part the most processed, but COD composition there is also not
Process and be directly sent to the material in stillpot.And, the COD comprised in the supernatant separated in stillpot
The load that composition gives activated carbon is excessive, it is therefore desirable to the activated carbon filled in exchange activity charcoal tower continually.So,
There is the problem that running management is miscellaneous and operating cost is too high.
Additionally, typically also allow for situations below: the phosphorus compound that adds as the nutrient source of mud (phosphoric acid,
Phosphate etc.) escape to process in water, become the reason of the eutrophication on draining discharge ground.
It is an object of the invention to when the active sludge treatment of coke-fired furnace draining, reduction processes the COD composition in water
With total phosphorus concentration.
Solve the means of problem
The present invention provides the processing means of coke-fired furnace draining, and it has: STRENGTH ON COKE fire grate water, by activated sludge
Microorganism implement biological treatment aeration tank, in described aeration tank through biological treatment processed water, pass through
Separate film and implement membrance separation portion that solid-liquid separation processes and contained by permeating in the infiltration water in described membrance separation portion
The COD composition removing unit that COD composition removes.
Additionally, the present invention provides the processing method of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, by activity
Microorganism in mud implements the active sludge treatment operation of biological treatment, to warp in described active sludge treatment operation
Cross biological treatment processed water, by separate film implement solid-liquid separation process membrance separation operation with will be described
Membrance separation operation is permeated the COD composition that in the infiltration water of described separation film, contained COD composition removes and removes work
Sequence.
That is, the present invention has in the following manner.
[1] processing means of a kind of coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, micro-by activated sludge
Biology implements the aeration tank of biological treatment, to passing through the processed water carried out a biological disposal upon in described aeration tank, by separation
Film implement membrance separation portion that solid-liquid separation processes, with by COD composition contained in described for the infiltration infiltration water separating film
The COD composition removing unit removed.
[2] processing means of a kind of coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, micro-by activated sludge
Biology implements the aeration tank of biological treatment, to passing through the processed water carried out a biological disposal upon in described aeration tank, by separation
Film is implemented the membrance separation portion of solid-liquid separation process, is contacted with activated carbon with making the described infiltration water separating film of infiltration
Activated carbon portion.
[3] according to the processing means of the coke-fired furnace draining described in described [1] or [2], wherein, described membrance separation portion is set
In described aeration tank or outside this aeration tank.
[4] according to the processing means of the coke-fired furnace draining described in any one of described [1]～[3], wherein, described aeration tank
In calcium concentration be 110mg/L～170mg/L.
[5] according to the processing means of the coke-fired furnace draining described in any one of described [1]～[4], wherein, to through dilution water
The coke-fired furnace draining of dilution, implements biological treatment by the microorganism in activated sludge in described aeration tank.
[6] according to the processing means of the coke-fired furnace draining described in described [5], wherein, described dilution water/described coke fire grate
The Capacity Ratio of water 1/1～4/1 scope.
[7] according to the processing means of the coke-fired furnace draining described in described [5] or [6], wherein, described dilution water be sea water and
/ or water for industrial use.
[8] according to the processing means of the coke-fired furnace draining described in any one of described [1]～[7], wherein, described membrance separation
Portion has separating film element, and the member of formation of this separating film element is Porous hollow-fibre membrane.
[9] according to the processing means of the coke-fired furnace draining described in any one of described [1]～[8], wherein, described membrance separation
In portion, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
[10] according to the processing means of the coke-fired furnace draining described in any one of described [1]～[9], wherein, described separation film
Average pore size be 0.03 μm～0.5 μm.
[11] processing method of a kind of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, micro-by activated sludge
Biology implements the active sludge treatment operation of biological treatment, to passing through biological treatment in described active sludge treatment operation
Processed water, implement membrance separation operation that solid-liquid separation processes by separating film, separate film with by described for infiltration
The COD composition removal step that COD composition contained in infiltration water removes.
[12] processing method of a kind of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, micro-by activated sludge
Biology implements the active sludge treatment operation of biological treatment, to passing through biological treatment in described active sludge treatment operation
Processed water, by separate film implement membrance separation operation that solid-liquid separation processes, with make the described film that separates of infiltration
The activated carbon that infiltration water contacts with activated carbon contacts operation.
[13] processing method of a kind of coke-fired furnace draining, it comprises: the reducers mixed with coke-fired furnace draining by dilution water
Sequence, to the dilution water-reducible coke-fired furnace draining obtained through described dilution operation, by the microorganism in activated sludge
Implement the active sludge treatment operation of biological treatment, to the quilt passing through biological treatment in described active sludge treatment operation
Process water, by separate film implement solid-liquid separation process membrance separation operation, with will permeate the described infiltration separating film
The COD composition removal step that COD composition contained in water removes.
[14] processing method of a kind of coke-fired furnace draining, it comprises: the reducers mixed with coke-fired furnace draining by dilution water
Sequence, to the dilution water-reducible coke-fired furnace draining obtained through described dilution operation, by the microorganism in activated sludge
Implement the active sludge treatment operation of biological treatment, to the quilt passing through biological treatment in described active sludge treatment operation
Process water, by separate film implement solid-liquid separation process membrance separation operation, with make the described infiltration separating film of infiltration
The activated carbon that water contacts with activated carbon contacts operation.
[15] according to the processing method of the coke-fired furnace draining described in any one of described [11]～[14], wherein, described film divides
From operation, by the described separation film arranged in the aeration tank implementing described biological treatment or outside this aeration tank, enter
Row solid-liquid separation processes.
[16] according to the processing means of the coke-fired furnace draining described in any one of described [11]～[15], wherein, described aeration
Calcium concentration in groove is 110mg/L～170mg/L.
[17] according to the processing method of the coke-fired furnace draining described in described [13] or [14], wherein, described dilution operation will
The Capacity Ratio of described dilution water/described coke-fired furnace draining is adjusted to the scope of 1/1～4/1.
[18] according to the processing method of the coke-fired furnace draining described in described [17], wherein, described dilution water be sea water and/
Or water for industrial use.
[19] according to the processing method of the coke-fired furnace draining described in any one of described [11]～[18], wherein, at described film
Separation circuit includes using the separating film element with Porous hollow-fibre membrane as member of formation.
[20] according to the processing method of the coke-fired furnace draining described in any one of described [11]～[19], wherein, described film divides
In operation, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
[21] according to the processing means of the coke-fired furnace draining described in any one of described [11]～[20], wherein, described separation
The average pore size of film is 0.03 μm～0.5 μm.
The effect of invention
According to the present invention it is possible in coke-fired furnace drainage sunk well, reduction processes the COD composition in water, extend activity
The charcoal life-span.
Additionally, reduction processes the total phosphorus concentration in water, prevent the eutrophication on discharge ground.
Accompanying drawing explanation
Fig. 1: be the processing means (film separated activated sludge apparatus) to the coke-fired furnace draining being suitable for present embodiment
The skeleton diagram that illustrates of an example.
Fig. 2: be the flow chart element that illustrates of an example of processing means to the coke-fired furnace draining being suitable for present embodiment
Figure.
Fig. 3: be the FB(flow block) that illustrates of the example of processing means to conventional coke-fired furnace draining.
Symbol description
The most former tank, 2... aeration tank, 3,9... diffuser, 4,11... liquid-level switch, 5... dissolved oxygen instrument, 6...
Stillpot, 7... mud collection machine, 8... membrance separation groove, 10... membrance separation portion, 12... process tank, 13... sand filtration
Tower, 14,15... activated carbon tower, 21... former water pipe arrangement, 22,25,26,27,28,31,32,33... pipe arrangements,
23 ... supplying tubing, 24... dissipate gas pipe arrangement, 29,34... drainage piping, 30,35... loopback pipe arrangement, 41,43,
44,51,53,54... pumps, 42,52... air-supply arrangement, 100... processing means (film separated activated sludge apparatus),
200... processing means (sedimentation method activated sludge apparatus), A... coke-fired furnace draining, B... dilution water, C, D... process
Water
Detailed description of the invention
Below, embodiments of the present invention are described in detail.
It addition, the present invention is not limited to implementation below, after various deformation can being carried out in its teachings
Implement.That is, the size of component parts of example record of embodiment, material, shape, its relative configuration etc.
As long as recording the most especially, objective not delimit the scope of the invention, and is merely illustrative example.
Additionally, the figure used is the example for present embodiment is described, it is not offered as the size of reality.Respectively scheme institute
, there is situation about exaggerating in order to make the explanation clear in the size of the component shown or position relationship etc..
<processing means of coke-fired furnace draining>
Fig. 1 is the processing means 100 (film separated activated sludge apparatus) to the coke-fired furnace draining being suitable for present embodiment
The skeleton diagram that illustrates of an example.
Fig. 2 is the flow chart element that an example of the processing means to the coke-fired furnace draining being suitable for present embodiment illustrates
Figure.Fig. 2 (a) is the 1st embodiment, and Fig. 2 (b) is the 2nd embodiment.
It addition, Fig. 1 describes conventional processing means 200 (sedimentation method activated sludge apparatus) in the lump.Fig. 1 institute
The processing means 100 of the coke-fired furnace draining shown, it possesses: storage imported by outside coke-fired furnace draining (A) (with
Under be designated as " former water (A) ".) former tank 1, by the former water to former tank 1 of the microorganism in activated sludge
In the contained BOD composition aeration tank (activated sludge apparatus) 2, right by membrance separation portion 10 that carries out carrying out a biological disposal upon
In aeration tank 2, the processed water through biological treatment carries out the membrance separation groove 8 of solid-liquid separation and will pass through membrance separation
Solid-liquid separation in groove 8 has permeated the activity that COD composition absorption contained in the infiltration water in membrance separation portion 10 removes
Charcoal tower (COD composition removing unit) 15.
In present embodiment, membrance separation portion 10 is made up of separating film module, and separating film module is equipped multiple to be had point
Separating film element from film.
Additionally, in present embodiment, membrance separation groove 8 is arranged at the outside (the 1st embodiment) of aeration tank 2.
(the 1st embodiment)
Then, based on Fig. 1 and Fig. 2 (a), the process stream that the processing means 100 utilizing coke-fired furnace draining is carried out
Journey illustrates.
As it is shown in figure 1, former water (A) is directed in former tank 1 storage by outside by former water pipe arrangement 21.Logical
Cross pump (P1) 41, via pipe arrangement 22 by former water (A) supply of storage in former tank 1 to aeration tank (activity
Device of sludge) in 2.
Adding in the former water (A) to aeration tank 2 by supplying tubing 23 by dilution water (B), former water is by (A)
Dilution.In present embodiment, use sea water and water for industrial use as dilution water (B).
Additionally, in present embodiment, by supplying tubing 23 using the phosphorus compound (example of the nutrient source as activated sludge
As, phosphoric acid) add to aeration tank 2.
In aeration tank 2, the former water (A) diluted through dilution water (B) is carried out by the microorganism in activated sludge
Biological treatment, by most BOD ingredient breakdown.Additionally, the amount of COD composition also reduces.
It addition, in aeration tank 2, by being arranged on outside air-supply arrangement (B1) 42, via scattered gas pipe arrangement 24, logical
The diffuser 3 arranged in crossing aeration tank 2 supplies air.BOD composition by the air that discharged by diffuser 3 and
Aoxidized by aerobism, and be decomposed.Additionally, control the water level in aeration tank 2 by liquid-level switch 4, pass through
Dissolved oxygen instrument 5 monitors dissolved oxygen content.
By the pump (P4) 51 arranged in aeration tank 2, via pipe arrangement 31 by aeration tank 2 through the quilt of biological treatment
Process water and be delivered to membrance separation groove 8.By the membrance separation portion 10 of dipping in membrance separation groove 8 to being sent to membrance separation groove
Processed water in 8 carries out solid-liquid separation process, and from processed water, mud is separated (solid-liquid separation).This embodiment party
In formula, via the pipe arrangement 32 being connected with membrance separation portion 10, carry out suction strainer by pump (P5) 53.Via pipe arrangement 33
The infiltration water having permeated membrance separation portion 10 is delivered in activated carbon tower (COD composition removing unit) 15.
Here, as COD composition removing unit, it is possible to use have employed aluminum sulfate, PAC, iron chloride, sulphuric acid
The coagulo sedimen tation tand of the coagulating agent of ferrum, bodied ferric sulfate etc., activated carbon tower etc..In present embodiment, as COD
Composition removing unit, is not particularly limited, such as, can use the activated carbon tower 15 being filled with activated carbon.
In activated carbon tower 15, the COD composition absorption contained in infiltration water is removed by it by activated carbon, then,
By the bottom of activated carbon tower 15 via drainage piping 34, as process water (D) row being suitable to discharge or recycling
Go out outside system.
Additionally, in activated carbon tower 15 fill activated carbon be, generally using the carbonizable substance such as coal, Exocarpium cocois (Cocos nucifera L) as raw material,
Have at high temperature produce with gas or reagent reacting to have minute aperture (diameter about 1nm～20nm) many
Hole metallic substance, its shape is not particularly limited, such as can suitably select to use fibrous, cellular, cylindric,
The activated carbon of broken shape, granular, powder etc..
Additionally, in membrance separation groove 8, by being arranged on the air-supply arrangement (B2) 52 of outside via being arranged at separating tank 8
Interior diffuser 9 supplies air.Additionally, control the water level in membrance separation groove 8 by liquid-level switch 11.Further
Ground, the mud that tunicle separated part 10 separates, by pump (P6) 54 via loopback pipe arrangement 35 by as loopback mud
Being recycled in aeration tank 2, a part of loopback mud is discharged to outside system as excess sludge, processed.
Then, each device of the processing means 100 (film separated activated sludge apparatus) constituting coke-fired furnace draining is entered
Row explanation.
(aeration tank (activated sludge apparatus) 2)
In aeration tank (activated sludge apparatus) 2, implement to provide oxygen to the aerobic mierobe in activated sludge, will
The biological treatment that Organic substance in coke-fired furnace draining (former water (A)) decomposes.
The biological treatment carried out with the aerobic mierobe in activated sludge, according to mode, for example there are such as, standard
Activated sludge process, long-time aeration, oxidation ditch (OD) method, step aeration, membrane separation activated sludge process etc..
Present embodiment have employed by the biological treatment in aeration tank (activated sludge apparatus) 2 and with in membrance separation groove 8
The membrane separation activated sludge process that combines of the physical treatment that carries out of membrane filtration.
Additionally, in organic biological treatment in coke-fired furnace draining (former water (A)), be preferably used in containing benzene
Phenol, CN, SCN, NH4Deng coke-fired furnace draining in cultivate (raising and train) antibacterial.As strain, for example there are example
As, thiocyano utilizes bacterium (チ オ シ ア Application bacterium) etc..
As described above, it is preferred to the middle dilution water (B) that adds of former water (A) in aeration tank 2 dilutes former water (A).
In present embodiment, because containing ammonia, cyanogen, thiocyano, phenol etc. in coke-fired furnace draining (former water (A))
There is the composition of bio-toxicity, it is advantageous to when enabling its flow into aeration tank 2, for lightening the load by dilution water (B)
It is diluted.
The dilution water (B) used in the dilution of former water (A) and the ratio (Capacity Ratio) of former water are generally at dilution water
(B) ratio (Capacity Ratio) of/former water (A) is (1/1)～the scope of (4/1), preferred (2/1)～(3/1)
Scope select.
Additionally, dilution water (B) can use sea water, water for industrial use, river etc..These can use a kind or
Mix two or more to use.
In present embodiment, sea water and/or water for industrial use are preferably used as dilution water (B).Thus, it is possible to will expose
Calcium concentration in air drain 2 is adjusted to the suitableeest scope.
Here, when using sea water and water for industrial use as dilution water (B), the preferably sea water in dilution water (B)
The ratio (Capacity Ratio) of/water for industrial use is (5/1)～the scope of (0.5/1), more preferably (1/1).
Additionally, in present embodiment, during Jiang Yuanshui (A) dilution, the preferably calcium concentration in aeration tank 2 is
100mg/L～200mg/L, more preferably 110mg/L～170mg/L, particularly preferred 125mg/L～155mg/L.
Here, want Jiang Yuanshui (A) and be adjusted to as described concentration, described dilution water (B) is preferably used.By
This, sea water can be 25 capacity %～40 capacity about % relative to the mixed proportion of mixed draining.
Here, if calcium concentration is too high, the calcium carbonate in aeration tank 2 can be accumulated, and the volume of aeration tank 2 has and subtracts
Few tendency.
If additionally, calcium concentration is too low, the settling velocity of mud reduces, and the membrance separation portion 10 of membrance separation groove 8 consolidates
The efficiency that liquid separates has the tendency of decline, and further, the pressure reduction in membrance separation portion 10 has the tendency of increase.
In present embodiment, preferably with the BOD composition comprised in former water (A) and the ratio of phosphorus compound (P)
In (BOD composition: P)=(100: 0.3)～the scope of (100: 1) (weight ratio), will be as activated sludge
The phosphorus compound of nutrient source add in former water (A).
It addition, when real-world operation processing means 100, if the addition of phosphorus compound to be set higher than above-mentioned ratio
Rate, then can tackle the organic concentration change comprised in former water (A).But, the addition mistake of phosphorus compound
Time many, remaining phosphorus compound can escape to process in water, has the tendency of the eutrophication causing draining discharge ground.
In present embodiment, the COD volumetric loading in aeration tank 2 is preferably set to 1kg/ (m3Day)～3kg/
(m3Day) left and right scope.
Additionally, the water temperature of aeration tank 2 preferably 30 DEG C～40 DEG C, more preferably 33 DEG C～35 DEG C.The water temperature mistake of aeration tank 2
Low or too high time, bacterial activity degree in active mud reduces, to the COD composition comprised in former water (A)
Or the decomposability of SCN etc. brings the tendency of impact.
(membrance separation groove 8)
In the membrance separation groove 8 of the outside being arranged at aeration tank 2, by the membrance separation portion being immersed in membrance separation groove 8
10 pairs of processed waters carry out solid-liquid separation process.As the separation film being disposed in membrance separation portion 10, for example there are example
As, secondary filter film (MF film), ultrafilter membrane etc..
Additionally, separate the shape of film, for example there are the type using hollow-fibre membrane and the type using flat film.Use
The type of hollow-fibre membrane, compared with the type using flat film, can improve the integration density of film.Especially because tool
There is the advantage that membrane filter unit is compact, aeration air capacity is few, so preferably.
As constituting the material separating film, for example there are such as, cellulose, polyolefin, polysulfones, Kynoar
(PVDF), the Organic substance such as politef (PTFE)；The inorganic matters such as pottery.
To membrance separation portion 10 be constructed without limit especially.In present embodiment, preferably by hollow fiber film assembly with
Dissipating gas generating means (diffuser 9, air-supply arrangement (B2) 52) to be applied in combination, described hollow fiber film assembly is
By lamellar hollow fibre membrane component the most arranged in parallel for multiple Porous hollow-fibre membranes with need between
Multiple and obtain every arrangement, described scattered gas generating means is arranged in the lower section of this hollow fiber film assembly.Hollow is fine
Dimension membrane module is made up of multiple hollow fibre membrane components, and global shape presents approximately parallelepiped body.
Additionally, from the viewpoint for the treatment of effeciency, the average pore size of described Porous doughnut is preferred
0.03 μm～0.5 μm.
In present embodiment, use the hollow fiber film assembly of the Porous hollow fibre membrane component with PVDF
As membrance separation portion 10.Now, from the viewpoint of the run stability and economy of membrane module, preferably located
The average daily membrane permeation flow of the reason water scope in 0.1m/ day～0.6m/ day is carried out, more preferably in 0.2m/ day～0.5m/ day
Scope carry out, the further preferably scope in 0.25m/ day～0.45m/ day is carried out.
Additionally, in order to prevent mud to be attached to Porous hollow-fibre membrane, occur that film is inaccessible, the most usually from scattered gas
Pipe 9 carries out aeration.
Further, inaccessible in order to prevent film, pump (P5) 53 is preferably used and intermittently carries out suction strainer, tool
Body ground, such as, carried out in the way of suction strainer (7 minutes)-stopping (1 minute).
Additionally, when using the processing means 100 of membrance separation groove 8 with the outside being arranged at aeration tank 2, by
The isolated separated sludge in membrance separation portion 10, preferably with the loopback between aeration tank 2 and membrance separation groove 8 than 1～5,
Preferably it is looped back with the scope of 2～3.
Additionally, the activated sludge suspended solid of aeration tank 2 (MLSS:Mixed liquor suspended solid) is
The scope of the scope of 4000mg/L～10000mg/L, preferably 6000mg/L～8000mg/L.
The MLSS of membrance separation groove 8 is the model of 5000mg/L～15000mg/L, preferably 8000mg/L～12000mg/L
Enclose.
(the 2nd embodiment)
Then, based on Fig. 2 (b), the 2nd embodiment of the processing means of STRENGTH ON COKE fire grate water illustrates.As
Shown in Fig. 2 (b), in present embodiment, membrance separation portion 10 is impregnated in the inside of aeration tank 2 and configures.
In present embodiment, there is the diffuser being delivered in former water (A) by air by air-supply arrangement (B1) 42
In 3 aeration tanks 2 identical with membrance separation portion 10, implement former water (A) by the microorganism in activated sludge
In the biological treatment decomposed of Organic substance process with by the solid-liquid separation in membrance separation portion 10.By using and membrance separation
The suction strainer of the pump that portion 10 is connected is to carry out solid-liquid separation process.Membrance separation portion will have been permeated by pump (P5) 53
The infiltration water of 10 is delivered in activated carbon tower 15.In activated carbon tower 15, will infiltration water be contained by activated carbon
The absorption of COD composition removes, then, by the bottom of activated carbon tower 15 via drainage piping 34, as being suitable to discharge
Or the process water (D) of recycling is expelled to outside system.
It addition, such as present embodiment, when membrance separation portion 10 is impregnated in the inside of aeration tank 2 and configures, exposure
The MLSS of air drain 2 is preferably the scope of 6000mg/L～15000mg/L.
In the processing means 100 of the coke-fired furnace draining being suitable for present embodiment, it is configured at when membrance separation portion 10 is impregnated
(the 1st embodiment), the biological treatment in aeration tank 2 time in the membrance separation groove 8 of the outside being arranged on aeration tank 2
Necessary air diffusion apparatus (diffuser 3, air-supply arrangement (B1) 42) and washing impregnated in membrance separation groove 8
Air diffusion apparatus necessary to membrance separation portion 10 (diffuser 9, air-supply arrangement (B2) 52), can use with each
The mode that adapts of groove.
Furthermore, it is possible to make the MLSS of aeration tank 2 operate less than under the mode of the MLSS of membrance separation groove 8.Enter one
Step ground, by cooperating with other systems or arranging multiple separated part membrane component, can be in the inspection of separated part membrane component
Repair and ceaselessly carry out solid-liquid separation process when changing.
Additionally, be suitable in the processing means 100 of the coke-fired furnace draining of present embodiment, when membrance separation portion 10 is impregnated
When being arranged in the inside of aeration tank 2 (the 2nd embodiment), the composition of operation is by simplification.Furthermore, it is possible to will make
The aeration carried out with the diffuser 3 of the inside being arranged at aeration tank 2 is for washing membrance separation portion 10.
Further, by cooperate with other systems or aeration tank 2 impregnated inside configure multiple separated part membrane elements
Part, is carried out in the case of the operating that can not stop aeration tank 2 when checking and repair and change of separated part membrane component
Solid-liquid separation processes.
It addition, by making the processing means 100 being suitable for the coke-fired furnace draining of present embodiment operate, process the total of water
Phosphorus concentration reduces.Think that the reason of the total phosphorus concentration reduction processing water is as follows.
That is, in present embodiment, the pH (hydrogen ionexponent) of coke-fired furnace draining (former water (A)) generally exists
Alkali side (pH8～pH9.5), containing the ammonia (800mg/L～1000mg/L after mixing) from coke-fired furnace draining.
Now, if there is a certain amount of magnesium (Mg), the then phosphorus compound added, meeting as the nutrient source of mud
With slightly solubility ammonium magnesium phosphate (hereinafter referred to as " MAP ".) crystallization.
Therefore, as described above the sea water as dilution water is added in former water (A) with the ratio of regulation, adjust
The magnesium (Mg) being practically free of in coke-fired furnace draining (former water (A)) and/or the amount of (Ca), then the crystallization of MAP is made
Separate out for insoluble substance.
Afterwards, by membrance separation portion 10, insoluble substance MAP is separated, can obtain eliminating major part
The process water of the phosphorus compound added as mud nutrient source.
That is, by being suitable for the processing means 100 of the coke-fired furnace draining of present embodiment, can stop to be arranged at
Toward processing means 200 in stillpot 6 or sand tower 13 cannot remove minute sized MAP crystallization pass through,
Prevent the leakage of phosphorus.
Embodiment
Below based on embodiment and comparative example, the present invention is carried out more specific description.As long as additionally, the present invention is not
Exceed its main idea, do not limited by following example.
(embodiment)
Use the processing means 100 of the coke-fired furnace draining shown in Fig. 1, by membrane separation activated sludge process (MBR),
The active sludge treatment of coke-fired furnace draining is carried out according to following shown operating condition.To former water (A: quilt before treatment
Process water) show in table 1 described later with the measurement result of water quality processing aquametry after processing.Processed water
(coke-fired furnace draining)
Water flowing flow: 0.1m3/ h (flow before dilution)
0.3m3/ h (flow with after sea water and water for industrial use dilution)
(2) treatment conditions of aeration tank 2
The adding proportion of marine industry water: coke-fired furnace draining: sea water: water for industrial use=1: 1: 1
The capacity of aeration tank 2: 4m3
Calcium concentration in aeration tank 2: 110mg/L～170mg/L
Phosphorus addition: average 10mg-P/L (interpolation phosphoric acid)
COD volumetric loading: average 2.6kg/ (m3Day)
Water temperature: 33 DEG C～35 DEG C
MLSS:7000mg/L～8000mg/L
Dissolved oxygen: average 1mg/L
(3) treatment conditions of membrance separation groove 8 (groove external form membrane separation device)
Membrance separation portion 10: use membrane area 18m2Hollow fiber film assembly (Mitsubishi Rayon Co., Ltd's system),
Described hollow fiber film assembly employs the hollow being equipped with PVDF hollow-fibre membrane (average pore size 0.4 μm)
Fibrous membrane element.
Generally bubble air amount: 10Nm3/m2H～20Nm3/m2·h
Process finding time 7 minutes of water, extract dwell time out 1 minute
Compared by the mud loopback of membrance separation groove 8 to aeration tank 2: 2
The average daily seepage discharge of film (membrance separation portion 10): 0.4m/ day
(4) treatment conditions of activated carbon tower 15 (COD removing unit)
Space velocity: 5 (m3/h)/(m3-AC)
The loading of activated carbon: 0.06m3
The floor height of activated carbon: 1900mmH
The size of activated carbon tower 15:(sectional area 0.031m2)
Water flowing LV:9.7m/h
Activated carbon tower 15 penetrates COD:60mg/L time (Japanese: broken)
(comparative example)
Use the conventional processing means 200 (sedimentation method activated sludge apparatus) of the coke-fired furnace draining shown in Fig. 1, logical
Cross the sedimentation method, carry out the active sludge treatment of coke-fired furnace draining according to following shown operating condition.
Hereinafter, based on Fig. 1 and Fig. 3, conventional processing means 200 is illustrated.
The conventional processing means 200 of the coke-fired furnace draining shown in Fig. 1, have former tank 1, aeration tank 2, containing from
Aeration tank 2 overflow activated sludge processed water flow into stillpot 6, by activated sludge in stillpot 6 sink
Process tank 12, sand tower 13 and the activated carbon tower 14 that the supernatant formed sediment and separate flows into.
In the same manner as processing means 100 (film separated activated sludge apparatus), the former water (A) of former tank 1 is supplied to
To aeration tank 2, carried out a biological disposal upon by the microorganism in activated sludge.Then, overflow containing from aeration tank 2
The processed water of the activated sludge gone out is flowed into via pipe arrangement 25 to be had in the stillpot 6 that mud collects machine 7, passes through
Activated sludge precipitates in stillpot 6, is separated into supernatant and mud (mud of loopback).It addition, by pump (P2)
44, loopback mud is recycled in aeration tank 2 via loopback pipe arrangement 30, a part of loopback mud is as excess sludge
The system that is expelled to is outer and is processed.
The supernatant separated in stillpot 6 flows to process in tank 12 via pipe arrangement 26, then, by pump (P3)
43, deliver in sand tower 13 via pipe arrangement 27, deliver in activated carbon tower 14 via pipe arrangement 28 further, from work
Property charcoal tower 14 bottom via drainage piping 29 as process water (C) be expelled to outside system.By conventional to using
The measurement result of the water quality that the process water after processing means 200 process measures with former water (processed water) before treatment,
Aftermentioned table 1 shows.(1) processed water (coke-fired furnace draining): (2) same as in Example 1 aeration tank 2
Treatment conditions: same as in Example 1
(3) treatment conditions of stillpot 6
Surface loading: 14.3m/ day
Compared by the mud loopback of stillpot 6 to aeration tank 2: 1
(4) treatment conditions of sand tower 13
Filter material floor height: anthracite: 1200mmH
Filter sand: 700mmH
The size of sand tower 13: 150mm φ × 3000mmH (sectional area 0.018m2)
Filter LV:17m/h
(5) treatment conditions of activated carbon tower 14: same as in Example 1
Table 1
Here, the life-span obtaining activated carbon as described below.
In embodiment, the process water in membrance separation portion 10 is passed through in activated carbon tower 15, in comparative example, by sand tower
The process water of 13 was passed through in activated carbon tower 14, taked each activated carbon tower to process water respectively every 12～14 hours,
Measure COD.
Activated carbon tower processes the COD of water, passes through along with the water flowing time and increases, by the COD of activated carbon tower inlet water
Arrive moment of 60% as breakpoint (Japanese: breakpoint), obtain by starting water flowing leading to breaking once a little
Water natural law.
Additionally, in embodiment and comparative example, carry out 3 these evaluations respectively, using the meansigma methods of permeable natural law as
The life-span of activated carbon is evaluated.
Result as shown in Table 1 understands, in the active sludge treatment of coke-fired furnace draining, by coke-fired furnace draining (former water
(A)) with coke-fired furnace draining (former water): sea water: water for industrial use=1: the dilution proportion of 1: 1, in making aeration tank 2
Calcium concentration is maintained at the scope of 110mg/L～170mg/L, and, the nutrient source as activated sludge adds phosphoric acid also
It is adjusted to phosphorus addition and reaches 10mg-P/L, after carrying out active sludge treatment in aeration tank 2, by having PVDF
The membrance separation portion 10 of hollow-fibre membrane processed has carried out the process water (embodiment) that solid-liquid separation processes, with untreated
Coke-fired furnace draining (former water (A)) is compared, and COD composition (COD (mg/L)) reduces the pact to former water (A)
About 1.8% (79mg/L), BOD composition (BOD (mg/L)) reduces about about 0.25% to former water (A)
(7.6mg/L), the activated carbon life-span filled in activated carbon tower 15 is extended, and needing the natural law changed is average 16
My god.
Further, total phosphorus concentration (T-P (total phosphorus) (mg/L)) reduces about about 0.6% to former water (A)
(0.06mg/L)。
On the other hand, using conventional processing means 200 (sedimentation method activated sludge apparatus) to same with embodiment
The coke-fired furnace draining of sample carries out during active sludge treatment (comparative example), and result is: the minimizing of COD composition terminates in former
About about 2.5% (110mg/L) of water (A), the minimizing of BOD composition terminates in about about 1.8% (55mg/L) of former water,
The natural law needing to change of the activated carbon filled in activated carbon tower 14, compared with embodiment, terminates in average 11 days.
Further, T-P (total phosphorus) reduces about about 7% (0.7mg/L) to former water (A).Above, according to
The present invention, replaces stillpot 6 and the sand filtration of conventional coke-fired furnace drain treatment apparatus by arranging membrance separation portion 10
Tower 13, it is possible to reduce the COD composition of activated carbon tower 15 entrance, thus extend the activated carbon life-span.
Additionally, reduce by processing the total phosphorus concentration in water, it is possible to prevent the eutrophication on discharge ground.
Claims (20)
1. a processing means for coke-fired furnace draining, it has: to through diluting water-reducible coke-fired furnace draining, dirty by activity
Microorganism in mud implement biological treatment aeration tank,
To described aeration tank passes through the processed water carried out a biological disposal upon, implement, by separating film, the membrance separation that solid-liquid separation processes
Portion,
The COD composition removing unit removed with the COD composition contained by permeating in the described infiltration water separating film,
Calcium concentration in described aeration tank is 110mg/L～170mg/L.
2. a processing means for coke-fired furnace draining, it has: to through diluting water-reducible coke-fired furnace draining, dirty by activity
Microorganism in mud implement biological treatment aeration tank,
To described aeration tank passes through the processed water carried out a biological disposal upon, implement, by separating film, the membrance separation that solid-liquid separation processes
Portion,
With make the described activated carbon portion that contacts with activated carbon of infiltration water separating film of infiltration,
Calcium concentration in described aeration tank is 110mg/L～170mg/L.
The processing means of coke-fired furnace draining the most according to claim 1 and 2, wherein, described membrance separation portion is arranged at
In described aeration tank or outside this aeration tank.
The processing means of coke-fired furnace draining the most according to claim 1, wherein, described dilution water/described coke fire grate
The Capacity Ratio of water 1/1～4/1 scope.
The processing means of coke-fired furnace draining the most according to claim 2, wherein, described dilution water/described coke fire grate
The Capacity Ratio of water 1/1～4/1 scope.
6. according to the processing means of the coke-fired furnace draining described in any one of claim 1,2,4,5, wherein, described dilute
Releasing water is sea water and/or water for industrial use.
The processing means of coke-fired furnace draining the most according to claim 1 and 2, wherein, described membrance separation portion has separation
Membrane component, the member of formation of this separating film element is Porous hollow-fibre membrane.
The processing means of coke-fired furnace draining the most according to claim 1 and 2, wherein, processed in described membrance separation portion
The average daily membrane permeation flow of water is 0.1m/ day～0.6m/ day.
The processing means of coke-fired furnace draining the most according to claim 1 and 2, wherein, the average pore size of described separation film
It is 0.03 μm～0.5 μm.
10. a processing method for coke-fired furnace draining, it comprises:
STRENGTH ON COKE fire grate water, by microorganism in activated sludge implement biological treatment active sludge treatment operation,
To described active sludge treatment operation is passed through the processed water carried out a biological disposal upon, implement solid-liquid separation process by separating film
Membrance separation operation,
The COD composition removal step removed with the COD composition contained by permeating in the described infiltration water separating film,
In described active sludge treatment operation, the calcium concentration in aeration tank is 110mg/L～170mg/L.
The processing method of 11. 1 kinds of coke-fired furnace drainings, it comprises:
STRENGTH ON COKE fire grate water, by microorganism in activated sludge implement biological treatment active sludge treatment operation,
To described active sludge treatment operation is passed through the processed water carried out a biological disposal upon, implement solid-liquid separation process by separating film
Membrance separation operation,
Operation is contacted with the activated carbon making the described infiltration water separating film of infiltration contact with activated carbon,
In described active sludge treatment operation, the calcium concentration in aeration tank is 110mg/L～170mg/L.
The processing method of 12. 1 kinds of coke-fired furnace drainings, it comprises:
Dilution operation that dilution water is mixed with coke-fired furnace draining,
The coke-fired furnace draining being diluted the dilution water obtained through described dilution operation, is implemented by the microorganism in activated sludge
Biological treatment active sludge treatment operation,
To described active sludge treatment operation is passed through the processed water carried out a biological disposal upon, implement solid-liquid separation process by separating film
Membrance separation operation,
The COD composition removal step removed with the COD composition contained by permeating in the described infiltration water separating film,
In described active sludge treatment operation, the calcium concentration in aeration tank is 110mg/L～170mg/L.
The processing method of 13. 1 kinds of coke-fired furnace drainings, it comprises:
Dilution operation that dilution water is mixed with coke-fired furnace draining,
To the dilution water-reducible coke-fired furnace draining obtained through described dilution operation, implemented raw by the microorganism in activated sludge
Thing process active sludge treatment operation,
To described active sludge treatment operation is passed through the processed water carried out a biological disposal upon, implement solid-liquid separation process by separating film
Membrance separation operation,
Operation is contacted with the activated carbon making the described infiltration water separating film of infiltration contact with activated carbon,
In described active sludge treatment operation, the calcium concentration in aeration tank is 110mg/L～170mg/L.
14. according to the processing method of the coke-fired furnace draining described in any one of claim 10～13, and wherein, described film divides
From operation, by the described separation film arranged in the aeration tank implementing described biological treatment or outside this aeration tank, carry out solid-liquid
Separating treatment.
The processing method of 15. coke-fired furnace drainings according to claim 12, wherein, described dilution operation is by described dilution
The scope that the Capacity Ratio of water/described coke-fired furnace draining adjusts to 1/1～4/1.
The processing method of 16. coke-fired furnace drainings according to claim 13, wherein, described dilution operation is by described dilution
The scope that the Capacity Ratio of water/described coke-fired furnace draining adjusts to 1/1～4/1.
17. according to the processing method of the coke-fired furnace draining described in claim 15 or 16, and wherein, described dilution water is sea water
And/or water for industrial use.
18. according to the processing method of the coke-fired furnace draining described in any one of claim 10～13, wherein, described membrance separation
Using separating film element in operation, the member of formation of this separating film element is Porous hollow-fibre membrane.
19. according to the processing method of the coke-fired furnace draining described in any one of claim 10～13, wherein, described membrance separation
In operation, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
20. according to the processing method of the coke-fired furnace draining described in any one of claim 10～13, wherein, described separation film
Average pore size be 0.03 μm～0.5 μm.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2012-147808 | 2012-06-29 | ||
| JP2012147808 | 2012-06-29 |
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| CN201320384809.XU Expired - Fee Related CN203513424U (en) | 2012-06-29 | 2013-06-28 | Treatment device for water discharged by coke oven |
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| CN201320384809.XU Expired - Fee Related CN203513424U (en) | 2012-06-29 | 2013-06-28 | Treatment device for water discharged by coke oven |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003117551A (en) * | 2001-10-10 | 2003-04-22 | Ebara Corp | Method and device for treating dioxins-containing waste water |
| JP2006223921A (en) * | 2005-02-15 | 2006-08-31 | Toray Ind Inc | Water treatment method |
| CN101746923A (en) * | 2009-08-19 | 2010-06-23 | 赵立功 | Coking wastewater deep treatment and reuse process and equipment thereof |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5190757A (en) * | 1975-02-07 | 1976-08-09 | Kookusuroansuino shorihoho | |
| JPH0669555B2 (en) * | 1987-03-25 | 1994-09-07 | 新日本製鐵株式会社 | Wastewater activated sludge treatment method |
| JP2005046697A (en) * | 2003-07-31 | 2005-02-24 | Mitsubishi Chemicals Corp | Activated sludge treatment method |
| TWI449674B (en) * | 2004-12-14 | 2014-08-21 | Kurita Water Ind Ltd | Drainage treatment device and treatment method |
| JP4979519B2 (en) * | 2007-09-06 | 2012-07-18 | 三菱レイヨン株式会社 | Operation method of membrane separation activated sludge treatment equipment |
| US7611632B1 (en) * | 2008-11-07 | 2009-11-03 | General Electric Company | Method of conditioning mixed liquor using a tannin containing polymer |
-
2013
- 2013-06-28 CN CN201310270463.5A patent/CN103523985B/en not_active Expired - Fee Related
- 2013-06-28 CN CN201320384809.XU patent/CN203513424U/en not_active Expired - Fee Related
- 2013-06-28 JP JP2013137260A patent/JP6169907B2/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003117551A (en) * | 2001-10-10 | 2003-04-22 | Ebara Corp | Method and device for treating dioxins-containing waste water |
| JP2006223921A (en) * | 2005-02-15 | 2006-08-31 | Toray Ind Inc | Water treatment method |
| CN101746923A (en) * | 2009-08-19 | 2010-06-23 | 赵立功 | Coking wastewater deep treatment and reuse process and equipment thereof |
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| JP6169907B2 (en) | 2017-07-26 |
| CN203513424U (en) | 2014-04-02 |
| JP2014028366A (en) | 2014-02-13 |
| CN103523985A (en) | 2014-01-22 |
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