CN103523985A - Coke oven discharge water treatment device, and coke oven discharge water treatment method - Google Patents
Coke oven discharge water treatment device, and coke oven discharge water treatment method Download PDFInfo
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- CN103523985A CN103523985A CN201310270463.5A CN201310270463A CN103523985A CN 103523985 A CN103523985 A CN 103523985A CN 201310270463 A CN201310270463 A CN 201310270463A CN 103523985 A CN103523985 A CN 103523985A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 183
- 239000000571 coke Substances 0.000 title claims abstract description 18
- 238000000034 method Methods 0.000 title claims description 55
- 239000010802 sludge Substances 0.000 claims abstract description 83
- 238000000926 separation method Methods 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 244000005700 microbiome Species 0.000 claims abstract description 24
- 239000012528 membrane Substances 0.000 claims description 144
- 238000005276 aerator Methods 0.000 claims description 84
- 238000010790 dilution Methods 0.000 claims description 52
- 239000012895 dilution Substances 0.000 claims description 52
- 239000000203 mixture Substances 0.000 claims description 44
- 230000008569 process Effects 0.000 claims description 43
- 238000012545 processing Methods 0.000 claims description 36
- 230000008595 infiltration Effects 0.000 claims description 22
- 238000001764 infiltration Methods 0.000 claims description 22
- 239000000835 fiber Substances 0.000 claims description 15
- 239000013535 sea water Substances 0.000 claims description 15
- 239000011575 calcium Substances 0.000 claims description 11
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 10
- 229910052791 calcium Inorganic materials 0.000 claims description 10
- 239000012466 permeate Substances 0.000 claims description 7
- 239000011148 porous material Substances 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000007865 diluting Methods 0.000 claims description 3
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 21
- 239000011574 phosphorus Substances 0.000 abstract description 21
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 12
- 238000005273 aeration Methods 0.000 abstract description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 55
- -1 phosphorus compound Chemical class 0.000 description 10
- 239000004576 sand Substances 0.000 description 10
- 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 239000012510 hollow fiber Substances 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 230000035764 nutrition Effects 0.000 description 6
- 235000016709 nutrition Nutrition 0.000 description 6
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 6
- 239000006228 supernatant Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000012716 precipitator Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 238000012851 eutrophication Methods 0.000 description 4
- 238000011049 filling Methods 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- 230000009183 running Effects 0.000 description 3
- 125000005031 thiocyano group Chemical group S(C#N)* 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 230000001580 bacterial effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-DYCDLGHISA-N deuterium hydrogen oxide Chemical compound [2H]O XLYOFNOQVPJJNP-DYCDLGHISA-N 0.000 description 2
- 238000007598 dipping method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 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 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 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
- 229920000297 Rayon Polymers 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
- 230000033228 biological regulation Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
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- 230000007423 decrease Effects 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
- 239000012535 impurity Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 150000003016 phosphoric acids Chemical class 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 1
- ZMZDMBWJUHKJPS-UHFFFAOYSA-N thiocyanic acid Chemical compound SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Images
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
An object of the invention is to reduce COD content and total phosphorus concentration in treating water in activated sludge treatment of coke oven discharge water. A coke oven discharge water treatment device provided by the invention comprises an aeration tank for carrying out biological treatment on the coke oven discharge water by microorganisms in activated sludge; a film separation unit for carrying out solid-liquid separation treatment on the treated water after biological treatment in the aeration tank; and a COD content removing unit for removing COD content in the permeation water permeating the separation film in the film separation unit.
Description
Technical field
The present invention relates to the water treatment device of coke fire grate and the treatment process of coke-fired furnace draining.
Background technology
In the past, the coke-fired furnace draining of being discharged by coke-fired furnace was flowed in drainage treatment equipment, and by active sludge, made it innoxious.
Usually, in coke-fired furnace draining, contain to be derived from the ammonia (NH of coke feed coal
4), cyanogen (CN), thiocyano (SCN), phenol etc. has the composition of bio-toxicity.Therefore,, when coke-fired furnace draining at that time flows in aerator tank, in order to lighten the load, by dilution water, dilute.
For example, in patent documentation 1, recorded a kind of activated sludge treatment method, at Jiang Yuanshui, imported in the method for carrying out continuously active sludge treatment in aerator tank, process water and seawater have been flowed in aerator tank as dilution water.
Prior art document
Patent documentation
Patent documentation 1: Japanese Patent Laid-Open 2005-46697 communique
Summary of the invention
The problem that invention will solve
Yet, in the active sludge treatment of coke-fired furnace draining, conventionally, in aerator tank, treated processing water is sent in settling bath, be separated into mud and supernatant liquor, supernatant liquor is removed impurity at sand tower further, removes the oxidizability material that is scaled COD (chemical oxygen demand (COD)) (be designated as below " COD composition " at activated carbon tower.)。
But, in aerator tank, although the organism that is scaled BOD (biochemical oxygen demand) containing in coke-fired furnace draining (is designated as " BOD composition " below.) major part processed, but in COD composition, also exist untreated and be directly sent to the material in settling bath.And it is excessive that the COD composition comprising in separated supernatant liquor gives the load of gac, therefore need the gac of filling in exchange activity charcoal tower continually in settling bath.So, exist the problem that running management is miscellaneous and operating cost is too high.
In addition, generally also consider following situation: the phosphorus compound (phosphoric acid, phosphoric acid salt etc.) adding as the nutrition source of mud escapes to be processed in water, become the reason of the eutrophication on draining discharge ground.
The object of the invention is to when the active sludge treatment of coke-fired furnace draining, reduce COD composition and the total phosphorus concentration processed in water.
Solve the means of problem
The invention provides the treatment unit of coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment aerator tank, in described aerator tank through the processed water of biological treatment, by separatory membrane implements membrane sepn portion that solid-liquid separation processes, with by permeating the COD composition that COD composition contained in the infiltration water of described membrane sepn portion removes, remove portion.
In addition, the invention provides the treatment process of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment active sludge treatment operation, in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements membrane sepn operation that solid-liquid separation processes, and the COD composition that COD composition contained permeate the infiltration water of described separatory membrane in described membrane sepn operation in is removed remove operation.
That is, the present invention has following mode.
[1] a kind for the treatment of unit of coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment aerator tank, in described aerator tank through the processed water of biological treatment, by separatory membrane implements membrane sepn portion that solid-liquid separation processes, with by permeating the COD composition that COD composition contained in the infiltration water of described separatory membrane removes, remove portion.
[2] a kind for the treatment of unit of coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment aerator tank, in described aerator tank through the processed water of biological treatment, by separatory membrane, implements the membrane sepn portion of solid-liquid separation processing, the gac portion contacting with gac with the infiltration water that makes to permeate described separatory membrane.
[3], according to the treatment unit of the coke-fired furnace draining described [1] or [2] Suo Shu, wherein, described membrane sepn portion is arranged in described aerator tank or outside this aerator tank.
[4], according to the treatment unit of the coke-fired furnace draining described in any one of described [1]～[3], wherein, the calcium concn in described aerator tank is 110mg/L～170mg/L.
[5], according to the treatment unit of the coke-fired furnace draining described in any one of described [1]～[4], wherein, to through diluting water-reducible coke-fired furnace draining, in described aerator tank, by the microorganism in active sludge, implement biological treatment.
[6], according to the treatment unit of the coke-fired furnace draining described [5] Suo Shu, wherein, the volume ratio of described dilution water/described coke-fired furnace draining is in 1/1～4/1 scope.
[7] according to the treatment unit of the coke-fired furnace draining described [5] or [6] Suo Shu, wherein, described dilution water is seawater and/or process water.
[8] according to the treatment unit of the coke-fired furnace draining described in any one of described [1]～[7], wherein, described membrane sepn portion has separating film element, and the member of formation of this separating film element is Porous hollow-fibre membrane.
[9], according to the treatment unit of the coke-fired furnace draining described in any one of described [1]～[8], wherein, in described membrane sepn portion, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
[10], according to the treatment unit of the coke-fired furnace draining described in any one of described [1]～[9], wherein, the mean pore size of described separatory membrane is 0.03 μ m～0.5 μ m.
[11] a kind for the treatment of process of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment active sludge treatment operation, in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements membrane sepn operation that solid-liquid separation processes, with by permeating the COD composition that COD composition contained in the infiltration water of described separatory membrane removes, remove operation.
[12] a kind for the treatment of process of coke-fired furnace draining, it comprises: STRENGTH ON COKE fire grate water, microorganism by active sludge implement biological treatment active sludge treatment operation, in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements the membrane sepn operation of solid-liquid separation processing, the gac contacting with gac with the infiltration water that makes to permeate described separatory membrane contacts operation.
[13] a kind for the treatment of process of coke-fired furnace draining, it comprises: the dilution operation that dilution water is mixed with coke-fired furnace draining, to the water-reducible coke-fired furnace draining of the dilution obtaining through described dilution operation, microorganism by active sludge implement biological treatment active sludge treatment operation, in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements membrane sepn operation that solid-liquid separation processes, with by permeating the COD composition that COD composition contained in the infiltration water of described separatory membrane removes, remove operation.
[14] a kind for the treatment of process of coke-fired furnace draining, it comprises: the dilution operation that dilution water is mixed with coke-fired furnace draining, to the water-reducible coke-fired furnace draining of the dilution obtaining through described dilution operation, microorganism by active sludge implement biological treatment active sludge treatment operation, in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements the membrane sepn operation of solid-liquid separation processing, the gac contacting with gac with the infiltration water that makes to permeate described separatory membrane contacts operation.
[15], according to the treatment process of the coke-fired furnace draining described in any one of described [11]～[14], wherein, described membrane sepn operation, by implementing the aerator tank of described biological treatment or the described separatory membrane of setting this aerator tank outside, carries out solid-liquid separation processing.
[16], according to the treatment unit of the coke-fired furnace draining described in any one of described [11]～[15], wherein, the calcium concn in described aerator tank is 110mg/L～170mg/L.
[17] according to the treatment process of the coke-fired furnace draining described [13] or [14] Suo Shu, wherein, described dilution operation is adjusted into 1/1～4/1 scope by the volume ratio of described dilution water/described coke-fired furnace draining.
[18], according to the treatment process of the coke-fired furnace draining described [17] Suo Shu, wherein, described dilution water is seawater and/or process water.
[19], according to the treatment process of the coke-fired furnace draining described in any one of described [11]～[18], wherein, in described membrane sepn operation, comprise using and take the separating film element that Porous hollow-fibre membrane is member of formation.
[20], according to the treatment process of the coke-fired furnace draining described in any one of described [11]～[19], wherein, in described membrane sepn operation, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
[21], according to the treatment unit of the coke-fired furnace draining described in any one of described [11]～[20], wherein, the mean pore size of described separatory membrane is 0.03 μ m～0.5 μ m.
The effect of invention
According to the present invention, can in processing, coke-fired furnace draining reduce the COD composition of processing in water, extend the gac life-span.
In addition, reduce the total phosphorus concentration of processing in water, prevent the eutrophication on discharge ground.
Accompanying drawing explanation
Fig. 1: be the sketch chart that an example of the treatment unit (film separated activated sludge apparatus) of the coke-fired furnace draining of applicable present embodiment is described.
Fig. 2: be the FB(flow block) that an example of the treatment unit of the coke-fired furnace draining of applicable present embodiment is described.
Fig. 3: be the FB(flow block) that the example of the treatment unit of coke-fired furnace draining is in the past described.
Nomenclature
1... former tank, 2... aerator tank, 3, 9... diffuser, 4, 11... liquid level switch, 5... dissolved oxygen instrument, 6... settling bath, 7... mud gathering machine, 8... membrane sepn groove, 10... membrane sepn portion, 12... process tank, 13... sand tower, 14, 15... activated carbon tower, 21... former water pipe arrangement, 22, 25, 26, 27, 28, 31, 32, 33... pipe arrangement, 23 ... supplying tubing, 24... gas pipe arrangement falls apart, 29, 34... drainage piping, 30, 35... loopback pipe arrangement, 41, 43, 44, 51, 53, 54... pump, 42, 52... air-supply arrangement, 100... treatment unit (film separated activated sludge apparatus), 200... treatment unit (precipitator method activated sludge apparatus), A... coke-fired furnace draining, B... dilution water, C, D... process water
Embodiment
Below, embodiments of the present invention are elaborated.
In addition, the present invention is not limited to following embodiment, can carry out implementing after various distortion within the scope of its aim.That is, only otherwise record especially, aim not delimit the scope of the invention for the size of the component parts that the example of embodiment is recorded, material, shape, its relative configuration etc., only illustrative examples just.
In addition, the figure of use is for an example of present embodiment being described, not representing actual size.The size of the member shown in each figure or position relationship etc., exist in order to make the explanation clear and the situation of exaggeration.
The treatment unit of<coke-fired furnace draining>
Fig. 1 is the sketch chart that an example of the treatment unit 100 (film separated activated sludge apparatus) of the coke-fired furnace draining of applicable present embodiment is described.
Fig. 2 is the FB(flow block) that an example of the treatment unit of the coke-fired furnace draining of applicable present embodiment is described.Fig. 2 (a) is the 1st embodiment, and Fig. 2 (b) is the 2nd embodiment.
In addition, in Fig. 1, recorded in the lump treatment unit 200 in the past (precipitator method activated sludge apparatus).The treatment unit 100 of the coke-fired furnace draining shown in Fig. 1, it possesses: store the coke-fired furnace draining (A) being imported by outside and (be designated as below " former water (A) ".) former tank 1, the aerator tank (activated sludge apparatus) 2 of BOD composition contained in the former water of former tank 1 being carried out a biological disposal upon by the microorganism in active sludge, by 10 pairs, membrane sepn portion in aerator tank 2 through the processed water of biological treatment carry out solid-liquid separation membrane sepn groove 8, with by the activated carbon tower (COD composition is removed portion) 15 that has permeated COD composition absorption contained in the infiltration water of membrane sepn portion 10 by the solid-liquid separation in membrane sepn groove 8 and remove.
In present embodiment, membrane sepn portion 10 consists of separating film module, and separating film module is equipped with a plurality of separating film elements with separatory membrane.
In addition,, in present embodiment, membrane sepn groove 8 is arranged at the outside (the 1st embodiment) of aerator tank 2.
(the 1st embodiment)
Then,, based on Fig. 1 and Fig. 2 (a), the treatment scheme of utilizing the treatment unit 100 of coke-fired furnace draining to carry out is described.
As shown in Figure 1, by former water pipe arrangement 21, former water (A) is directed in former tank 1 and is stored by outside.By pump (P1) 41, be situated between and by pipe arrangement 22, the former water (A) of storing in former tank 1 be supplied in aerator tank (activated sludge apparatus) 2.
By supplying tubing 23, dilution water (B) is added in the former water (A) in aerator tank 2, former water is by (A) dilution.In present embodiment, as dilution water (B), use seawater and process water.
In addition, in present embodiment, by supplying tubing 23, the phosphorus compound of the nutrition source as active sludge (for example, phosphoric acid) is added in aerator tank 2.
In aerator tank 2, to carrying out a biological disposal upon by the microorganism in active sludge through the former water (A) of dilution water (B) dilution, most BOD composition is decomposed.In addition, the amount of COD composition also reduces.
In addition, in aerator tank 2, by being arranged on outside air-supply arrangement (B1) 42, be situated between by loose gas pipe arrangement 24, by diffuser 3 air supplies of aerator tank 2 interior settings.BOD composition by the air being discharged by diffuser 3 by aerobism be oxidized, and be decomposed.In addition, the water level of controlling in aerator tank 2 by liquid level switch 4, by dissolved oxygen instrument 5 monitoring dissolved oxygen contents.
By the pump (P4) 51 of aerator tank 2 interior settings, be situated between, by pipe arrangement 31, the processed water through biological treatment in aerator tank 2 be delivered to membrane sepn groove 8.The processed water that 10 pairs, the membrane sepn portion by membrane sepn groove 8 interior dippings is sent in membrane sepn groove 8 carries out solid-liquid separation processing, by mud from processed water separated (solid-liquid separation).In present embodiment, be situated between by the pipe arrangement 32 being connected with membrane sepn portion 10, by pump (P5) 53, carry out suction strainer.Jie is delivered to the infiltration water that has permeated membrane sepn portion 10 in activated carbon tower (COD composition is removed portion) 15 by pipe arrangement 33.
, as COD composition, remove portion here, can use coagulo sedimen tation tand, activated carbon tower of the condensing agent that has adopted Tai-Ace S 150, PAC, iron(ic) chloride, ferric sulfate, bodied ferric sulfate etc. etc.In present embodiment, as COD composition, remove portion, be not particularly limited, for example, can use the activated carbon tower 15 of having filled gac.
In activated carbon tower 15, it is removed by gac the COD composition absorption containing in infiltration water, then, by the bottom of activated carbon tower 15, is situated between by drainage piping 34, as the processing water (D) that is suitable for discharge or recycling, is expelled to outside system.
In addition, the gac of filling in activated carbon tower 15 is, conventionally using the carbon speciess such as coal, Exocarpium cocois (Cocos nucifera L) as raw material, there is at high temperature the Porous material with minute aperture (diameter 1nm～20nm left and right) producing with gas or reagent react, its shape is not particularly limited, such as suitable fibrous, cellular, cylindric, the broken shape of choice for use, granular, Powdered etc. gac.
In addition, in membrane sepn groove 8, by being arranged on outside air-supply arrangement (B2) 52, be situated between by diffuser 9 air supplies that are arranged in separator tank 8.In addition, by the water level in liquid level switch 11 controlling diaphragm separator tanks 8.Further, the mud of tunicle separated part 10 separation, is used as loopback mud by pump (P6) 54 Jie by loopback pipe arrangement 35 and is recycled in aerator tank 2, and a part of loopback mud is discharged to outside system as excess sludge, processed.
Then, to forming each device of the treatment unit 100 (film separated activated sludge apparatus) of coke-fired furnace draining, describe.
(aerator tank (activated sludge apparatus) 2)
In aerator tank (activated sludge apparatus) 2, implementing provides oxygen to the aerobism microorganism in active sludge, by the biological treatment of the organic substance decomposing in coke-fired furnace draining (former water (A)).
The biological treatment of carrying out with the aerobism microorganism in active sludge, according to mode, for example has for example, conventional actived sludge, long-time aeration, oxidation ditch (OD) method, step aeration, film separated activated sludge method etc.In present embodiment, adopted the biological treatment in aerator tank (activated sludge apparatus) 2 and the film separated activated sludge method combining with the physical treatment that the membrane filtration in membrane sepn groove 8 carries out.
In addition,, in the organic biological treatment in coke-fired furnace draining (former water (A)), preferably use and containing phenol, CN, SCN, NH
4deng coke-fired furnace draining in cultivate the bacterium of (raising and train).As bacterial classification, for example have for example, thiocyano utilizes bacterium (チ オ シ ア ン Capitalization bacterium) etc.
As mentioned above, preferably the middle dilution water (B) that adds of the former water (A) in aerator tank 2 dilutes former water (A).
In present embodiment, because contain the composition that ammonia, cyanogen, thiocyano, phenol etc. have bio-toxicity in coke-fired furnace draining (former water (A)), so preferably, when making it flow into aerator tank 2, dilute by dilution water (B) for lightening the load.
The dilution water (B) using in the dilution of former water (A) and the ratio (volume ratio) of former water are selected for the scope of the scope of (1/1)～(4/1), preferred (2/1)～(3/1) at the ratio (volume ratio) of dilution water (B)/former water (A) conventionally.
In addition, dilution water (B) can be used seawater, process water, river etc.These can use a kind or mix two or more use.
In present embodiment, preferably use seawater and/or process water as dilution water (B).Thus, the calcium concn in aerator tank 2 can be adjusted into the suitableeest scope.
Here, while using seawater and process water as dilution water (B), preferably the ratio (volume ratio) of the seawater/process water in dilution water (B) is the scope of (5/1)～(0.5/1), more preferably (1/1).
In addition,, in present embodiment, during Jiang Yuanshui (A) dilution, preferably the calcium concn in aerator tank 2 is 100mg/L～200mg/L, more preferably 110mg/L～170mg/L, particularly preferably 125mg/L～155mg/L.
Here, want Jiang Yuanshui (A) and be adjusted into as described concentration, preferably use described dilution water (B).Thus, seawater can be 25 capacity %～40 capacity % left and right with respect to the blending ratio of mixed draining.
Here, if calcium concn is too high, the calcium carbonate in aerator tank 2 can be accumulated, and the volume of aerator tank 2 has the tendency of minimizing.
In addition, if calcium concn is too low, the sedimentation speed of mud reduces, and the efficiency of the solid-liquid separation of the membrane sepn portion 10 of membrane sepn groove 8 has the tendency of decline, and further, the pressure reduction of membrane sepn portion 10 has the tendency of increase.
In present embodiment, preferably with the ratio of the BOD composition that comprises in former water (A) and phosphorus compound (P) at (BOD composition: the scope of P)=(100: 0.3)～(100: 1) (weight ratio), is added into the phosphorus compound of the nutrition source as active sludge in former water (A).
In addition, when real-world operation treatment unit 100, if the addition of phosphorus compound is set as higher than above-mentioned ratio, can tackle the organic concentration change comprising in former water (A).But when the addition of phosphorus compound is too much, remaining phosphorus compound can escape to be processed in water, has and causes draining to discharge the tendency of the eutrophication on ground.
In present embodiment, the COD volumetric loading in aerator tank 2 is preferably set to 1kg/ (m
3day)～3kg/ (m
3day) scope of left and right.
In addition preferably 30 ℃～40 ℃ of the water temperatures of aerator tank 2, more preferably 33 ℃～35 ℃.The water temperature of aerator tank 2 is too low or when too high, has the bacterial activity degree in active sludge to reduce, the decomposability of the COD composition comprising in former water (A) or SCN etc. is brought to the tendency of impact.
(membrane sepn groove 8)
Be arranged in the outside membrane sepn groove 8 of aerator tank 2, by the 10 pairs of processed waters of membrane sepn portion that are immersed in membrane sepn groove 8, carry out solid-liquid separation processing.As the separatory membrane being equipped in membrane sepn portion 10, for example there are for example secondary filter film (MF film), ultra-filtration membrane etc.
In addition, the shape of separatory membrane, has the type and the type of using flat film of using hollow-fibre membrane for example.Use the type of hollow-fibre membrane, compare with using the type of flat film, can improve the integration density of film.Especially because have advantages of that membrane filter unit compactness, aeration air capacity are few, so preferably.
Material as forming separatory membrane, for example has the organism such as Mierocrystalline cellulose, polyolefine, polysulfones, polyvinylidene difluoride (PVDF) (PVDF), tetrafluoroethylene (PTFE) for example; The inorganicss such as pottery.
Formation to membrane sepn portion 10 is not particularly limited.In present embodiment, preferably hollow fiber film assembly and loose gas generating unit (diffuser 9, air-supply arrangement (B2) 52) are used in combination, the sheet hollow fibre membrane component that described hollow fiber film assembly is arranged in parallel a plurality of Porous hollow-fibre membranes at grade obtains so that being spaced of needs is a plurality of, and described loose gas generating unit is configured in the below of this hollow fiber film assembly.Hollow fiber film assembly is comprised of a plurality of hollow fibre membrane components, and global shape presents roughly rectangular parallelepiped.
In addition,, from the viewpoint of processing efficiency, the mean pore size of described Porous tubular fibre is 0.03 μ m～0.5 μ m preferably.
In present embodiment, use the hollow fiber film assembly of the Porous hollow fibre membrane component with PVDF system as membrane sepn portion 10.Now, from the run stability of membrane module and the viewpoint of economy, preferably the average daily membrane permeation flow of processed water carries out in the scope of 0.1m/ day～0.6m/ day, more preferably in the scope of 0.2m/ day～0.5m/ day, carry out, further preferably in the scope of 0.25m/ day～0.45m/ day, carry out.
In addition, in order to prevent that mud is attached to Porous hollow-fibre membrane, occurs that film is inaccessible, preferably usually carries out aeration from diffuser 9.
Further, in order to prevent film obturation, preferably use pump (P5) 53 intermittently to carry out suction strainer, particularly, for example, in the mode of suction strainer (7 minutes)-stop (1 minute), carry out.
In addition, when use has the treatment unit 100 of the outside membrane sepn groove 8 that is arranged at aerator tank 2, by the isolated separated sludge of membrane sepn portion 10, preferably with the loopback between aerator tank 2 and membrane sepn groove 8 than 1～5, preferably with 2～3 scope by loopback.
In addition, the active sludge suspended solid of aerator tank 2 (MLSS:Mixed liquor suspended solid) is the scope of 4000mg/L～10000mg/L, preferably the scope of 6000mg/L～8000mg/L.
The MLSS of membrane sepn groove 8 is 5000mg/L～15000mg/L, preferably the scope of 8000mg/L～12000mg/L.
(the 2nd embodiment)
Then,, based on Fig. 2 (b), the 2nd embodiment of the treatment unit of STRENGTH ON COKE fire grate water describes.As shown in Fig. 2 (b), in present embodiment, membrane sepn portion 10 is impregnated in the inside of aerator tank 2 and configures.
In present embodiment, in thering is the identical aerator tank 2 of the diffuser 3 by air-supply arrangement (B1) 42, air delivered in former water (A) and membrane sepn portion 10, implement by the microorganism in active sludge the biological treatment of the organic substance decomposing in former water (A) and process by the solid-liquid separation of membrane sepn portion 10.By using the suction strainer of the pump being connected with membrane sepn portion 10 to carry out solid-liquid separation processing.By pump (P5) 53, the infiltration water that has permeated membrane sepn portion 10 is delivered in activated carbon tower 15.In activated carbon tower 15, by gac, the COD composition absorption containing in infiltration water is removed, then, by the bottom of activated carbon tower 15, be situated between by drainage piping 34, as the processing water (D) that is suitable for discharge or recycling, be expelled to outside system.
In addition, as present embodiment, when membrane sepn portion 10 is impregnated in the inside of aerator tank 2 and configures, the MLSS of aerator tank 2 is preferably the scope of 6000mg/L～15000mg/L.
In the treatment unit 100 of the coke-fired furnace draining of applicable present embodiment, when membrane sepn portion 10 is impregnated, is disposed at and is arranged on the outside membrane sepn groove 8 of aerator tank 2 when interior (the 1st embodiment), the necessary loose device of air of biological treatment in aerator tank 2 (diffuser 3, air-supply arrangement (B1) 42) and washing impregnated in the necessary loose device of air of membrane sepn portion 10 (diffuser 9, air-supply arrangement (B2) 52) in membrane sepn groove 8, can adopt the mode adapting with groove separately.
Under the mode of the MLSS that in addition, can make aerator tank 2 lower than the MLSS of membrane sepn groove 8, turn round.Further, by cooperating with other systems or a plurality of separated part membrane elements being set, can when repairing replacing, the inspection of separated part membrane element ceaselessly carry out solid-liquid separation processing.
In addition,, in the treatment unit 100 of the coke-fired furnace draining of applicable present embodiment, when membrane sepn portion 10 is impregnated while being configured in the inside of aerator tank 2 (the 2nd embodiment), the formation of operation is by simplification.In addition, use can be arranged to aeration that the diffuser 3 of the inside of aerator tank 2 carries out for washing membrane sepn portion 10.
Further, by cooperating with other systems or at a plurality of separated part membrane elements of the inside of aerator tank 2 dipping configuration, in the situation that repairing the running that can not stop aerator tank 2 while changing, the inspection of separated part membrane element carries out solid-liquid separation processing.
In addition, by making treatment unit 100 runnings of the coke-fired furnace draining of applicable present embodiment, the total phosphorus concentration of processing water reduces.Think that to process the reason that the total phosphorus concentration of water reduces as follows.
That is,, in present embodiment, the pH (hydrogen ionexponent) of coke-fired furnace draining (former water (A)), conventionally at alkali side (pH8～pH9.5), contains the ammonia (800mg/L～1000mg/L after mixing) from coke-fired furnace draining.
Now, if there is a certain amount of magnesium (Mg), the phosphorus compound adding as the nutrition source of mud, can with insoluble phosphoric acid magnesium ammonium (following, be called " MAP ".) crystallization.
Therefore, as described above the seawater as dilution water is added in former water (A) with the ratio of regulation, adjust the magnesium (Mg) and/or the amount (Ca) that in coke-fired furnace draining (former water (A)), contain hardly, the crystallization of MAP is separated out as insoluble substance.
Afterwards, by membrane sepn portion 10, insoluble substance MAP is carried out to separation, can obtain having removed the processing water of the most phosphorus compound adding as mud nutrition source.
That is, the treatment unit 100 of the coke-fired furnace draining by applicable present embodiment, can stop to be arranged at the minute sized MAP crystallization that settling bath 6 in treatment unit 200 in the past or sand tower 13 cannot remove and pass through, and prevents the leakage of phosphorus.
Embodiment
Based on embodiment and comparative example, the present invention is carried out to more specific description below.In addition, as long as the present invention is no more than its main idea, by following examples, do not limited.
(embodiment)
Use the treatment unit 100 of the coke-fired furnace draining shown in Fig. 1, by film separated activated sludge method (MBR), the active sludge treatment of carrying out coke-fired furnace draining according to the operating condition shown in following.To (the A: the measurement result of the water quality of processing aquametry processed water) and after processing shows in table 1 described later of the former water before processing.Processed water
(coke-fired furnace draining)
Water flowing flow: 0.1m
3/ h (flow before dilution)
0.3m
3/ h (with the flow after seawater and process water dilution)
(2) treatment condition of aerator tank 2
The adding proportion of marine industry water: coke-fired furnace draining: seawater: process water=1: 1: 1
The capacity of aerator tank 2: 4m
3
Calcium concn in aerator tank 2: 110mg/L～170mg/L
Phosphorus addition: average 10mg-P/L (interpolation phosphoric acid)
COD volumetric loading: average 2.6kg/ (m
3day)
Water temperature: 33 ℃～35 ℃
·MLSS：7000mg/L～8000mg/L
Dissolved oxygen: average 1mg/L
(3) treatment condition of membrane sepn groove 8 (groove external form membrane separation unit)
Membrane sepn portion 10: use membrane area 18m
2hollow fiber film assembly (Mitsubishi Rayon Co., Ltd's system), described hollow fiber film assembly has been used the hollow fibre membrane component that is equipped with PVDF hollow-fibre membrane processed (mean pore size 0.4 μ m).
Common bubble air amount: 10Nm
3/ m
2h～20Nm
3/ m
2h
Process finding time 7 minutes of water, extract stand-by time out 1 minute
Mud loopback ratio by membrane sepn groove 8 to aerator tank 2: 2
The average daily seepage discharge of film (membrane sepn portion 10): 0.4m/ day
(4) treatment condition of activated carbon tower 15 (COD removes portion)
Space velocity: 5 (m
3/ h)/(m
3-AC)
The loading level of gac: 0.06m
3
The floor height of gac: 1900mmH
The size of activated carbon tower 15:
(sectional area 0.031m
2)
Water flowing LV:9.7m/h
COD:60mg/L when activated carbon tower 15 penetrates (Japanese: Po Over)
(comparative example)
Use the treatment unit in the past 200 (precipitator method activated sludge apparatus) of the coke-fired furnace draining shown in Fig. 1, by the precipitator method, the active sludge treatment of carrying out coke-fired furnace draining according to the operating condition shown in following.
Below, based on Fig. 1 and Fig. 3, treatment unit 200 is in the past described.
The treatment unit in the past 200 of the coke-fired furnace draining shown in Fig. 1, the settling bath 6 that the processed water that have former tank 1, aerator tank 2, contains the active sludge overflowing from aerator tank 2 flows into, the processing tank 12 that separated supernatant liquor flows into by active sludge precipitation settling bath 6, sand tower 13, with activated carbon tower 14.
With treatment unit 100 (film separated activated sludge apparatus) similarly, the former water (A) of former tank 1 is supplied in aerator tank 2, by the microorganism in active sludge, carries out a biological disposal upon.Then, the processed water that contains the active sludge overflowing from aerator tank 2 is situated between and is flow in the settling bath 6 with mud gathering machine 7 by pipe arrangement 25, by active sludge, in settling bath 6, precipitates, and is separated into supernatant liquor and mud (mud of loopback).In addition, by pump (P2) 44, loopback mud is situated between and is recycled in aerator tank 2 by loopback pipe arrangement 30, it is outer and processed that a part of loopback mud is expelled to system as excess sludge.
Supernatant liquor Jie separated in settling bath 6 is flowed to and is processed in tank 12 by pipe arrangement 26, then, by pump (P3) 43, Jie is delivered in sand tower 13 by pipe arrangement 27, further be situated between and delivered in activated carbon tower 14 by pipe arrangement 28, from bottom Jie of activated carbon tower 14, by drainage piping 29, as processing water (C), be expelled to system.The measurement result of the water quality that the former water (processed water) by the processing water after use treatment unit 200 is in the past processed and before processing is measured, demonstration in aftermentioned table 1.(1) processed water (coke-fired furnace draining): the treatment condition of identical with embodiment 1 (2) aerator tank 2: identical with embodiment 1
(3) treatment condition of settling bath 6
Surface load: 14.3m/ day
Mud loopback ratio by settling bath 6 to aerator tank 2: 1
(4) treatment condition of sand tower 13
Filter material floor height: hard coal: 1200mmH
Filter sand: 700mmH
The size of sand tower 13: 150mm φ * 3000mmH (sectional area 0.018m
2)
Filter LV:17m/h
(5) treatment condition of activated carbon tower 14: identical with embodiment 1
Table 1
Here, the life-span of obtaining gac as described below.
In embodiment, the processing water of membrane sepn portion 10 is passed in activated carbon tower 15, in comparative example, the processing water of sand tower 13 is passed in activated carbon tower 14, every 12～14 hours, take respectively each activated carbon tower to process water, measure COD.
Activated carbon tower is processed the COD of water, along with water flowing time process, increases, and using the moment of the COD arrival 60% of activated carbon tower inlet water as breakpoint (Japanese: Po Over point), obtains by starting water flowing till break once water flowing number of days a little.
In addition, in embodiment and comparative example, carry out respectively 3 these evaluations, the life-span using the mean value of permeable number of days as gac is evaluated.
Result is as shown in Table 1 known, 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): seawater: process water=1: the dilution proportion of 1: 1, make calcium concn in aerator tank 2 remain on the scope of 110mg/L～170mg/L, and, as the nutrition source of active sludge, add phosphoric acid and be adjusted into phosphorus addition and reach 10mg-P/L, in aerator tank 2, carry out after active sludge treatment, by thering is the membrane sepn portion 10 of PVDF hollow-fibre membrane processed, carried out the processing water (embodiment) that solid-liquid separation is processed, compare with untreated coke-fired furnace draining (former water (A)), COD composition (COD (mg/L)) is reduced to approximately 1.8% left and right (79mg/L) of former water (A), BOD composition (BOD (mg/L)) is reduced to approximately 0.25% left and right (7.6mg/L) of former water (A), the gac life-span of filling in activated carbon tower 15 is extended, needing the number of days of changing is average 16 days.
Further, total phosphorus concentration (T-P (total phosphorus) (mg/L)) is reduced to approximately 0.6% left and right (0.06mg/L) of former water (A).
On the other hand, using treatment unit 200 (precipitator method activated sludge apparatus) in the past when carrying out active sludge treatment with the same coke-fired furnace draining of embodiment (comparative example), result is: the minimizing of COD composition terminates in approximately 2.5% left and right (110mg/L) of former water (A), the minimizing of BOD composition terminates in approximately 1.8% left and right (55mg/L) of former water, the number of days that the needs of the gac of filling in activated carbon tower 14 are changed is compared with embodiment, terminates in average 11 days.
Further, T-P (total phosphorus) is reduced to approximately 7% left and right (0.7mg/L) of former water (A).Above, according to the present invention, by membrane sepn portion 10 is set, replace settling bath 6 and the sand tower 13 of coke-fired furnace drain treatment apparatus in the past, can reduce the COD composition of activated carbon tower 15 entrances, thereby extend the gac life-span.
In addition, by the total phosphorus concentration of processing in water, reduce, can prevent the eutrophication on discharge ground.
Claims (24)
1. a treatment unit for coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, by the microorganism in active sludge implement biological treatment aerator tank,
To in described aerator tank through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn portion,
Remove portion with the COD composition that COD composition contained in the infiltration water of the described separatory membrane of infiltration is removed.
2. a treatment unit for coke-fired furnace draining, it has: STRENGTH ON COKE fire grate water, by the microorganism in active sludge implement biological treatment aerator tank,
To in described aerator tank through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn portion,
The gac portion contacting with gac with the infiltration water that makes to permeate described separatory membrane.
3. the treatment unit of coke-fired furnace draining according to claim 1 and 2, wherein, described membrane sepn portion is arranged in described aerator tank or outside this aerator tank.
4. the treatment unit of coke-fired furnace draining according to claim 1 and 2, wherein, the calcium concn in described aerator tank is 110mg/L～170mg/L.
5. the treatment unit of coke-fired furnace draining according to claim 1 wherein, to through diluting water-reducible coke-fired furnace draining, is implemented biological treatment by the microorganism in active sludge in described aerator tank.
6. the treatment unit of coke-fired furnace draining according to claim 2 wherein, to through diluting water-reducible coke-fired furnace draining, is implemented biological treatment by the microorganism in active sludge in described aerator tank.
7. the treatment unit of coke-fired furnace draining according to claim 5, wherein, the volume ratio of described dilution water/described coke-fired furnace draining is in 1/1～4/1 scope.
8. the treatment unit of coke-fired furnace draining according to claim 6, wherein, the volume ratio of described dilution water/described coke-fired furnace draining is in 1/1～4/1 scope.
9. according to the treatment unit of the coke-fired furnace draining described in any one of claim 5～8, wherein, described dilution water is seawater and/or process water.
10. the treatment unit of coke-fired furnace draining according to claim 1 and 2, wherein, described membrane sepn portion has separating film element, and the member of formation of this separating film element is Porous hollow-fibre membrane.
The treatment unit of 11. coke-fired furnace drainings according to claim 1 and 2, wherein, in described membrane sepn portion, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
The treatment unit of 12. coke-fired furnace drainings according to claim 1 and 2, wherein, the mean pore size of described separatory membrane is 0.03 μ m～0.5 μ m.
The treatment process of 13. 1 kinds of coke-fired furnace drainings, it comprises: STRENGTH ON COKE fire grate water, the active sludge treatment operation of carrying out a biological disposal upon by the microorganism enforcement in active sludge,
To in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn operation,
Remove operation with the COD composition that COD composition contained in the infiltration water of the described separatory membrane of infiltration is removed.
The treatment process of 14. 1 kinds of coke-fired furnace drainings, it comprises: STRENGTH ON COKE fire grate water, the active sludge treatment operation of carrying out a biological disposal upon by the microorganism enforcement in active sludge,
To in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn operation,
The gac contacting with gac with the infiltration water that makes to permeate described separatory membrane contacts operation.
The treatment process of 15. 1 kinds of coke-fired furnace drainings, it comprises: the dilution operation that dilution water is mixed with coke-fired furnace draining,
The coke-fired furnace draining that the dilution water obtaining through described dilution operation is diluted, the active sludge treatment operation of carrying out a biological disposal upon by the microorganism enforcement in active sludge,
To in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn operation,
Remove operation with the COD composition that COD composition contained in the infiltration water of the described separatory membrane of infiltration is removed.
The treatment process of 16. 1 kinds of coke-fired furnace drainings, it comprises: the dilution operation that dilution water is mixed with coke-fired furnace draining,
To the water-reducible coke-fired furnace draining of the dilution obtaining through described dilution operation, the active sludge treatment operation of carrying out a biological disposal upon by the microorganism enforcement in active sludge,
To in described active sludge treatment operation through the processed water of biological treatment, by separatory membrane implements solid-liquid separation processing membrane sepn operation,
The gac contacting with gac with the infiltration water that makes to permeate described separatory membrane contacts operation.
17. according to the treatment process of the coke-fired furnace draining described in any one of claim 13～16, and wherein, described membrane sepn operation, by implementing the aerator tank of described biological treatment or the described separatory membrane of setting this aerator tank outside, carries out solid-liquid separation processing.
18. according to the treatment unit of the coke-fired furnace draining described in any one of claim 13～16, and wherein, the calcium concn in described aerator tank is 110mg/L～170mg/L.
The treatment process of 19. coke-fired furnace drainings according to claim 15, wherein, described dilution operation is adjusted to 1/1～4/1 scope by the volume ratio of described dilution water/described coke-fired furnace draining.
The treatment process of 20. coke-fired furnace drainings according to claim 16, wherein, described dilution operation is adjusted to 1/1～4/1 scope by the volume ratio of described dilution water/described coke-fired furnace draining.
21. according to the treatment process of the coke-fired furnace draining described in claim 19 or 20, and wherein, described dilution water is seawater and/or process water.
22. according to the treatment process of the coke-fired furnace draining described in any one of claim 13～16, wherein, in described membrane sepn operation, uses separating film element, and the member of formation of this separating film element is Porous hollow-fibre membrane.。
23. according to the treatment process of the coke-fired furnace draining described in any one of claim 13～16, and wherein, in described membrane sepn operation, the average daily membrane permeation flow of processed water is 0.1m/ day～0.6m/ day.
24. according to the treatment process of the coke-fired furnace draining described in any one of claim 13～16, and wherein, the mean pore size of described separatory membrane is 0.03 μ m～0.5 μ m.
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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|---|---|---|---|---|
| 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 |
| CN102107996A (en) * | 2004-12-14 | 2011-06-29 | 栗田工业株式会社 | Apparatus and method for treating waste water |
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| 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 |
| 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 (4)
| 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 |
| CN102107996A (en) * | 2004-12-14 | 2011-06-29 | 栗田工业株式会社 | Apparatus and method for treating 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 |
| CN103523985B (en) | 2016-08-10 |
| JP2014028366A (en) | 2014-02-13 |
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Address after: Within Japan Tokyo Chiyoda pill 1 chome 1 No. 1 Co-patentee after: Nippon Rensui Co. Patentee after: MITSUBISHI CHEMICAL Corp. Address before: Within Japan Tokyo Chiyoda pill 1 chome 1 No. 1 Co-patentee before: Nippon Rensui Co. Patentee before: MITSUBISHI RAYON Co.,Ltd. |
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