CN104418472A - Treatment device and treatment method of wastewater containing organic matters - Google Patents
Treatment device and treatment method of wastewater containing organic matters Download PDFInfo
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- CN104418472A CN104418472A CN201310413803.5A CN201310413803A CN104418472A CN 104418472 A CN104418472 A CN 104418472A CN 201310413803 A CN201310413803 A CN 201310413803A CN 104418472 A CN104418472 A CN 104418472A
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- 238000000034 method Methods 0.000 title claims abstract description 54
- 239000002351 wastewater Substances 0.000 title abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 162
- 239000012528 membrane Substances 0.000 claims abstract description 138
- 239000007788 liquid Substances 0.000 claims abstract description 95
- 238000000926 separation method Methods 0.000 claims abstract description 88
- 238000001704 evaporation Methods 0.000 claims abstract description 57
- 230000008020 evaporation Effects 0.000 claims abstract description 57
- 238000001471 micro-filtration Methods 0.000 claims abstract description 46
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 46
- 238000001728 nano-filtration Methods 0.000 claims abstract description 40
- 238000011033 desalting Methods 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims description 73
- 239000010865 sewage Substances 0.000 claims description 53
- 230000008569 process Effects 0.000 claims description 50
- 239000003513 alkali Substances 0.000 claims description 44
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 42
- 239000002253 acid Substances 0.000 claims description 19
- 238000001914 filtration Methods 0.000 claims description 18
- 238000005342 ion exchange Methods 0.000 claims description 17
- 238000005406 washing Methods 0.000 claims description 17
- 239000003814 drug Substances 0.000 claims description 16
- 238000002347 injection Methods 0.000 claims description 15
- 239000007924 injection Substances 0.000 claims description 15
- 238000002791 soaking Methods 0.000 claims description 13
- 239000012141 concentrate Substances 0.000 claims description 7
- 238000011084 recovery Methods 0.000 abstract description 6
- 238000001223 reverse osmosis Methods 0.000 abstract description 4
- 238000005374 membrane filtration Methods 0.000 abstract 3
- 239000000706 filtrate Substances 0.000 abstract 1
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 8
- 239000007787 solid Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 230000008676 import Effects 0.000 description 7
- 229920002401 polyacrylamide Polymers 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 238000009299 dissolved gas flotation Methods 0.000 description 4
- 230000003472 neutralizing effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 229910052681 coesite Inorganic materials 0.000 description 3
- 229910052906 cristobalite Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005189 flocculation Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- 238000005188 flotation Methods 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 235000012239 silicon dioxide Nutrition 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 229910052682 stishovite Inorganic materials 0.000 description 3
- 229910052905 tridymite Inorganic materials 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 240000006909 Tilia x europaea Species 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 241001253206 Andrias Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 238000007738 vacuum evaporation Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2673—Evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention provides a treatment device and a treatment method of wastewater containing organic matters. The treatment device comprises an aerobic tank, a microfiltration or ultrafiltration membrane separating device, a reverse osmosis membrane or nanofiltration membrane separating device and an evaporation and concentration device, wherein the aerobic tank is used for carrying out aerobic treatment on the wastewater containing organic matters under an aerobic condition; the microfiltration or ultrafiltration membrane separating device is used for carrying out solid-liquid separation on treating water of the aerobic tank; the reverse osmosis membrane or nanofiltration membrane separating device is used for carrying out desalting treatment on filtrate of the microfiltration or ultrafiltration membrane separating device; and the evaporation and concentration device is used for carrying out further concentration on concentrated water of the reverse osmosis membrane or nanofiltration membrane separating device. According to the treatment device and the treatment method, the organic matters can be effectively removed; the processing amount of the evaporation and concentration device is reduced; and the pure water recovery rate of the overall system is greatly improved.
Description
Technical field
The present invention relates to a kind for the treatment of unit containing organism sewage and treatment process.
Background technology
In the prior art, there will be a known a kind for the treatment of process of waste water, processed waste water is supplied in NF film unit, be separated into through water and non-through water, and should through water supply in RO film unit, be separated into through water and non-through water, and this is non-ly concentrated through in water supply to evaporation concentration device.(patent documentation 1)
Patent documentation 1: Japanese Patent Laid-Open 2007-789
But, in above-mentioned treatment process, if be present in organism in waste water, then effectively by organic matter removal, and can not can reduce the pure water rate of recovery of NF film unit and RO film unit, increase the weight of the treatment capacity of evaporation concentration device.
Summary of the invention
In view of the above-mentioned problems, the invention provides a kind for the treatment of unit containing organism sewage and treatment process, effectively by organic matter removal, the treatment capacity of evaporation concentration device can be alleviated, and greatly improve the pure water rate of recovery of whole system.
Technical scheme 1 of the present invention is, a kind for the treatment of unit containing organism sewage, has: under aerobic conditions, aerobic treatment is containing the aerobic slot of organism sewage; The process water of described aerobic slot is carried out to micro-filtration or the ultrafiltration membrane separating device of solid-liquid separation; The counter of desalting treatment is carried out to the filtered liquid of described micro-filtration or ultrafiltration membrane separating device and soaks into film or nanofiltration membrane separation device; And evaporation concentration device concentrated is further carried out to described anti-condensed water of soaking into film or nanofiltration membrane separation device.
Technical scheme 2 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 1, also have: ion exchange unit, instead soak into before film or nanofiltration membrane separation device carry out desalting treatment to described filtered liquid described, described ion exchange unit carries out ion-exchange to described filtered liquid.
Technical scheme 3 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 2, also have: alkali adding set, before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water.
Technical scheme 4 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 2, also have: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
Technical scheme 5 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 2, also have: alkali adding set, before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water; And condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
Technical scheme 6 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 1, also have: alkali adding set, before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water.
Technical scheme 7 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 6, also have: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
Technical scheme 8 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 1, also have: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
Technical scheme 9 of the present invention is, a kind for the treatment of process containing organism sewage, has: utilize aerobic slot aerobic treatment under aerobic conditions to contain the aerobic treatment operation of organism sewage; Micro-filtration or the process water of ultrafiltration membrane separating device to described aerobic slot is utilized to carry out the solid-liquid separation process of solid-liquid separation; Utilize and instead soak into the desalting treatment operation that film or the nanofiltration membrane separation device filtered liquid to described micro-filtration or ultrafiltration membrane separating device carries out desalting treatment; And utilize evaporation concentration device to carry out evaporation concentration operation concentrated further to described anti-condensed water of soaking into film or nanofiltration membrane separation device.
Technical scheme 10 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 9, also has: before described desalting treatment operation, utilize ion exchange unit to carry out the ion-exchange process of ion-exchange to described filtered liquid.
Technical scheme 11 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 10, also has: before described evaporation concentration operation, utilizes alkali adding set to add operation to the alkali that described condensed water adds alkali.
Technical scheme 12 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 10, also has: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
Technical scheme 13 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 10, also has: before described evaporation concentration operation, utilizes alkali adding set to add operation to the alkali that described condensed water adds alkali; And condensing the obtained condensing water of the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is transported to the condensing water conveying operation of described aerobic slot.
Technical scheme 14 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 9, also has: before described evaporation concentration operation, utilizes alkali adding set to add operation to the alkali that described condensed water adds alkali.
Technical scheme 15 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 14, also has: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
Technical scheme 16 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 9, also has: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
Technical scheme 17 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 9, also have: under the state stopping described solid-liquid separation process, wash operation to the medicine that the filtering membrane of the film separation unit of described micro-filtration or ultrafiltration membrane separating device cleans, this medicine is washed operation and is had: liquid is injected the film separation unit of described micro-filtration or ultrafiltration membrane separating device to clean the liquid injection process of described filtering membrane; When described film separation unit has been filled with liquid, the aeration making described micro-filtration or ultrafiltration membrane separating device keep utilizing aeration tube to carry out has run the placement operation of the state stopped; Described micro-filtration or ultrafiltration membrane separating device is made to carry out the empty aeration operation of described aeration operation; Water is injected the film separation unit of described micro-filtration or ultrafiltration membrane separating device to wash the washing step of described filtering membrane; And make the water after washing be discharged to the discharge operation of the membrane sepn groove of described micro-filtration or ultrafiltration membrane separating device by described aeration tube from described film separation unit.
Technical scheme 18 of the present invention is, the treatment unit containing organism sewage as described in technical scheme 17, described liquid is hypochlorite liquid.
Technical scheme 19 of the present invention is, as described in technical scheme 18 containing the treatment unit of organism sewage, then carry out once described medicine and wash operation, after medicine once wash in operation, described liquid is acid liquid.
The effect of invention
Adopt technique scheme of the present invention, effectively by organic matter removal, the treatment capacity of evaporation concentration device can be alleviated, and greatly improve the pure water rate of recovery of whole system.
Utilize ion exchange unit and operation, the divalent ion composition in filtered liquid can be removed, prevent from soaking into fouling in film or nanofiltration membrane separation device and evaporation concentration device counter.
Utilize alkali adding set and operation, chlorine corrosion evaporation concentration device can be prevented.
Utilize condensing water transfer unit and operation, can the heat that evaporation concentration device produces is supplied in aerobic slot, make the activity of activated sludge in aerobic slot, improve process, filtration efficiency.
Utilize washing step and discharge operation, in the filtered liquid that the materials such as hypochlorite, acid, active interface agent can be avoided to be mixed in high concentration after film separation unit filters, preventing from soaking into film or nanofiltration membrane separation device generation detrimentally affect to counter.
Accompanying drawing explanation
Fig. 1 is the synoptic diagram of the treatment unit containing organism sewage of the present invention.
Fig. 2 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of hypochlorite liquid injection process.
Fig. 3 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of placement operation.
Fig. 4 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of empty aeration operation.
Fig. 5 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of washing step.
Fig. 6 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of discharge operation.
Fig. 7 is the synoptic diagram of aerobic slot of the present invention and micro-filtration or ultrafiltration membrane separating device part, for illustration of acid liquid injection process.
Nomenclature
4 aerobic slots
5 micro-filtrations or ultrafiltration membrane separating device
6 water softeners
7 instead soak into film or nanofiltration membrane separation device
8 alkali adding sets
9 evaporation concentration devices
10 concentrated former water tanks
11 concentrated tanks
12 transfer limes
Embodiment
With reference to figure 1-7, the specific embodiment of the present invention is described in detail.
As shown in Figure 1, the treatment unit containing organism sewage mainly comprises: aerobic slot 4, micro-filtration or ultrafiltration membrane separating device 5, as the water softener 6 of ion exchange unit, instead soaks into film or nanofiltration membrane separation device 7, alkali adding set 8 and evaporation concentration device 9.
First be directed in aerobic slot 4 as the former water containing organism sewage.In aerobic slot 4, the former water of aerobic treatment under aerobic conditions.That is, be provided with aeration tube 41 in aerobic slot 4, use blower B 1, after air being imported to aeration tube 41, carry out aeration by aeration tube 41, utilize the microorganism needing oxygen in aerobic slot 4, the organism in former water is decomposed.
Micro-filtration or ultrafiltration membrane separating device 5 carry out solid-liquid separation to the process water after aerobic slot 4 processes.This micro-filtration or ultrafiltration membrane separating device 5 comprise membrane sepn groove 51, aeration tube 52 and film separation unit 53.Film separation unit 53 uses microfiltration membrane (MF film) or ultra-filtration membrane (UF film), and be arranged in membrane sepn groove 51, aeration tube 52 is arranged on the below of film separation unit 53.
Process water after aerobic slot 4 processes is directed in membrane sepn groove 51.Film separation unit 53 is utilized to carry out solid-liquid separation to process water.And use blower B 1, air is imported in aeration tube 52, make it in membrane sepn groove 51, carry out aeration, utilize aeration stream that the filtering membrane of film separation unit 53 is vibrated, prevent the Pore Blocking of filtering membrane.Microfiltration membrane (MF film) or the ultra-filtration membrane (UF film) of film separation unit 53 can be flat films, tubular film, any one of hollow-fibre membrane etc.
Filtered liquid after solid-liquid separation is through water softener 6, and water softener 6 pairs of filtered liquids carry out ion-exchange, is removed by the divalent ion composition such as the Ca ion in filtered liquid, Mg ion, prevents from soaking into fouling in film or nanofiltration membrane separation device and evaporation concentration device counter.
Instead soak into film or nanofiltration membrane separation device 7 pairs of filtered liquids carry out desalting treatment, comprise filtered liquid tank 71, the first step is counter soaks into that film or nanofiltration membrane component 72 and the second stage are counter soaks into film or nanofiltration membrane component 73.
Anti-film or the nanofiltration membrane separation device 7 of soaking into can coagulation, also can second-stage treatment.Counter soak into film or nanofiltration membrane separation device 7 reverse osmosis membrane (RO film) or nanofiltration membrane (NF film) can be flat film, tubular film, any one of hollow-fibre membrane, spiral type etc.
After filtered liquid after ion-exchange is imported into filtered liquid tank 71, be fed into that the first step is counter soaks into film or nanofiltration membrane component 72, through the first step counter soak into film or nanofiltration membrane component 72 filter after first step process water be imported into that the second stage is counter soaks into film or nanofiltration membrane component 73, the part that the first step is counter soaks into the first step condensed water produced in film or nanofiltration membrane component 72 is directed in concentrated former water tank 10, and another part mixes with filtered liquid and again imported to that the first step is counter soaks into film or nanofiltration membrane component 72.Through the second stage counter soak into film or nanofiltration membrane component 73 filter after second stage process water be recovered utilization, the anti-part of soaking into the second stage condensed water produced in film or nanofiltration membrane component 73 in the second stage is got back in filtered liquid tank 71, and another part mixes with first step process water and again imported to that the second stage is counter to be soaked in film or nanofiltration membrane component 73.
Before first step condensed water is directed to concentrated former water tank 10, utilizes alkali adding set 8 pairs of first step condensed water to add the alkali such as such as NaOH, chlorine corrosion evaporation concentration device 9 can be prevented.
First step condensed water in concentrated former water tank 10 is imported in evaporation concentration device 9.In evaporation concentration device 9, first step condensed water is heated, under the state of decompression, make it evaporate and concentrate further.Condensed water after concentrating further is imported in concentrated tank 11, discards as industrial waste.
The condensing water that the moisture that evaporation concentration device 9 evaporates is condensing obtained is transported in aerobic slot 4 by the transfer lime 12 as condensing water transfer unit.Thus, the heat produced from evaporation concentration device 9 is also supplied to aerobic slot 4 thereupon, makes the activity of activated sludge in aerobic slot 4, improves process, filtration efficiency.
Then, with reference to figure 2-7, illustrate that the filtering membrane to micro-filtration or ultrafiltration membrane separating device of the present invention carries out the medicine that medicine washes and washes operation.
Operation washed by medicine is stop under the state processing water solid-liquid separation at micro-filtration or ultrafiltration membrane separating device 5, to the operation that the filtering membrane of film separation unit 53 cleans, and carry out according to the order of hypochlorite liquid injection process, placement operation, empty aeration operation, washing step, discharge operation, acid liquid injection process, placement operation, empty aeration operation, washing step, discharge operation.
In hypochlorite liquid injection process, hypochlorite liquid medicine injection is entered the cleaned filter membrane of film separation unit 53 of micro-filtration or ultrafiltration membrane separating device 5.
Namely, as described in Figure 2, pump P1 runs, by after film separation unit 53 filters, the filtered liquid be stored in aqua storage tank 12 imports to film separation unit 53, pump P2 runs, imported to film separation unit 53 by the hypochlorite liquid be stored in hypochlorite chemical liquid groove 13, filtered liquid and hypochlorite liquid together import in film separation unit 53 after A place mixes, and clean the filtering membrane of film separation unit 53.Hypochlorite liquid can add NaClO, Ca (ClO) in process water
2or ClKO etc. and being formed.
Meanwhile, pump P3 is out of service, and the acid liquid be stored in acid chemical liquid groove 14 stops importing to film separation unit 53.
Meanwhile, blower B 1 is out of service, and air stops importing to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 stop aeration.
Meanwhile, pump P4 is out of service, and filtered liquid stops outwards deriving from film separation unit 53.
In placement operation, micro-filtration or ultrafiltration membrane separating device 5 is made to keep aeration to run the state stopped when film separation unit 53 has been filled with hypochlorite liquid.
That is, as shown in Figure 3, pump P1, pump P2 and pump P3 are out of service, and filtered liquid, hypochlorite liquid and acid liquid stop importing to film separation unit 53.Meanwhile, blower B 1 is out of service, and air stops importing to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 stop aeration.Meanwhile, pump P4 is out of service, and filtered liquid stops outwards deriving from film separation unit 53.
In empty aeration operation, described micro-filtration or ultrafiltration membrane separating device 5 is made to carry out aeration operation.
That is, as shown in Figure 4, blower B 1 is run, and air is directed to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52 respectively.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 carry out aeration.
Meanwhile, pump P1, pump P2 and pump P3 are out of service, and filtered liquid, hypochlorite liquid and acid liquid stop importing to film separation unit 53.Meanwhile, pump P4 is out of service, and filtered liquid stops outwards deriving from film separation unit 53.
In washing step, water is injected the water washed filter membrane of film separation unit 53 of micro-filtration or ultrafiltration membrane separating device 5.
That is, as shown in Figure 5, pump P1 runs, by after film separation unit 53 filters, the filtered liquid be stored in aqua storage tank 12 imports in film separation unit 53, filtering membrane is washed.Blower B 1 is run, and air is directed to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52 respectively.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 carry out aeration.
Meanwhile, pump P2 and pump P3 is out of service, and hypochlorite liquid and acid liquid stop importing to film separation unit 53.
Meanwhile, pump P4 is out of service, and filtered liquid stops outwards deriving from film separation unit 53.
In discharge operation, the water after washing is made to turn back in aeration tube 52 and be discharged in the membrane sepn groove 51 of micro-filtration or ultrafiltration membrane separating device 5.
That is, as shown in Figure 6, pump P4 runs, and the water after washing is outwards derived from film separation unit 53.Blower B 1 is run, and air is directed to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52 respectively.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 carry out aeration.Further, at C place, the water after washing and air mixed, together import in aeration tube 52, and the water thus after washing enters in membrane sepn groove 51.
Meanwhile, pump P1, pump P2 and pump P3 are out of service, and filtered liquid, hypochlorite liquid and acid liquid stop importing to film separation unit 53.
In acid liquid injection process, acid liquid medicine injection is entered the cleaned filter membrane of film separation unit 53 of micro-filtration or ultrafiltration membrane separating device 5.
As described in Figure 7, pump P1 runs, by after film separation unit 53 filters, the filtered liquid be stored in aqua storage tank 12 imports to film separation unit 53, pump P3 runs, the acid liquid be stored in acid chemical liquid groove 14 is imported to film separation unit 53, filtered liquid and acid liquid together import in film separation unit 53 after B place mixes, and clean the filtering membrane of film separation unit 53.Acid liquid can be add H in process water
2sO
4deng and formed.
Meanwhile, pump P2 is out of service, and the hypochlorite liquid be stored in hypochlorite chemical liquid groove 13 stops importing to film separation unit 53.
Meanwhile, blower B 1 is out of service, and air stops importing to the aeration tube 41 in treatment trough 4, the aeration tube 54 in membrane sepn groove 51, aeration tube 52.Therefore, aeration tube 41, aeration tube 54, aeration tube 52 stop aeration.
Meanwhile, pump P4 is out of service, and filtered liquid stops outwards deriving from film separation unit 53.
Afterwards, above-mentioned placement operation, empty aeration operation, washing step, discharge operation is carried out again.
Operation is washed through above-mentioned medicine, the organism of filter membrane surface can be removed, and in the filtered liquid that the material such as hypochlorite, acid can not be made to be mixed in high concentration after film separation unit 53 filters, prevent from soaking into film or nanofiltration membrane separation device generation detrimentally affect to counter.
More preferably, the treatment unit containing organism sewage can also comprise oil-water separation tank, device on flow adjustment tank and Pressurized flotation.
First former water be directed in oil-water separation tank.In oil-water separation tank, oil is separated from former water.
Then, the former water being separated oil is imported to flow adjustment tank.Utilize flow adjustment tank, control the flow that former water imports to Pressurized dissolved gas flotation device.
These suspended solids are removed by making the suspended solid comprising SiO2 and Ca in former water float by Pressurized dissolved gas flotation device.Pressurized dissolved gas flotation device can comprise reactive tank, groove on Pressurized flotation, neutralizing well.
First former water be directed in reactive tank, successively add as the polymerize aluminum chloride (PAC) of flocculation agent, polyacrylamide (PAM) utilize agitator to stir in two reactive tanks, make polymerize aluminum chloride (PAC), polyacrylamide (PAM) fully dissolves in former water, by suspended solid flocculation together.
Then, on Pressurized flotation in groove, by air injection device, by air Injection in former water, produce a large amount of fine gas bubbles, fine gas bubbles captures the suspended solid flocculated in former water, and utilizes the buoyancy of fine gas bubbles that suspended solid is floated.Float to the water surface of former water at suspended solid after, utilize trap setting, suspended solid is removed from the water surface.
Wherein, about SiO2, it is colloidal and with negative charge, when adding polymerize aluminum chloride (PAC), SiO2 can flocculate together, and floats, thus is removed by from former water as described above.
About Ca, its can from as stripping the concrete water tank of reactive tank in former water.In order to remove Ca, needing in flow adjustment tank, to add Na2CO3 in advance, making Ca insoluble in former water, then by above-mentioned flocculation agent, making it flocculate together, and float, thus removed by from former water as described above.
The former water eliminating suspended solid is directed in neutralizing well.In neutralizing well, add H2SO4, the pH value of former water is neutralized.
Afterwards, the more former water after having carried out pH value adjustment is imported in aerobic slot 4, carry out above-mentioned aerobic treatment, solid-liquid separation, ion-exchange, desalting treatment, alkali interpolation, evaporation concentration and condensing water conveying operation successively.
Embodiment
According to embodiment, the present invention to be further illustrated below.
About the operation conditions of the treatment unit containing organism sewage, 8-10m when the former water yield of process is for running
3/ d, 16m during design
3/ d.
About the operational conditions of Pressurized dissolved gas flotation device, the former water yield of process is 1m
3/ h, water area load is 24m
3/ m
2/ d, the residence time of former water is 2.8h.Polymerize aluminum chloride (PAC) input rate is 500mg PAC purity/L, and polyacrylamide (PAM) input rate is 3mg PAM purity/L.The pH value of reactive tank is 8.5, and the pH value of neutralizing well is 7.5.
About the operational conditions of micro-filtration or ultrafiltration membrane separating device 5, biochemical oxygen demand (BOD) (BOD) volumetric loading is 0.045kgBOD/m
3/ d.Biochemical oxygen demand (BOD) (BOD) sludge loading is 0.015kgBOD/kgMLSS/d.The membrane area of filtering membrane is 10m
2/ sheet * 5=50m
2, membrane flux is 0.18m
3/ m
2/ d.
About anti-operational conditions of soaking into film or nanofiltration membrane separation device 7, the former water yield of process is 1m
3/ h, the process water yield after process is 0.8m
3/ h, the rate of recovery is more than 80%.The anti-first step of soaking into film or nanofiltration membrane separation device is counter soaks into film or nanofiltration membrane component 72 is the anti-membrane module that soaks into of anti-pollution low pressure spiral type, and the membrane area of filtering membrane is 7.43m
2/ * 9=67m
2, membrane flux is 0.33m
3/ m
2/ d.The anti-second stage soaking into film or nanofiltration membrane separation device is counter soaks into film or nanofiltration membrane component 73 is the anti-membrane module that soaks into of ultralow pressure, and the membrane area of filtering membrane is 7.9m
2/ * 6=47m
2, membrane flux is 0.41m
3/ m
2/ d.About the rate of recovery, the anti-membrane module 72 that soaks into of the first step is 80%, and the anti-membrane module 73 that soaks in the second stage is 88%.
About the operational conditions of evaporation concentration device 9, the former water yield of process is 1.6-3.2m
3/ d, can carry out 8-16 doubly concentrated, the condensed water of generation is 0.2m
3/ d.This evaporation concentration device 9 is vacuum-evaporation steam-heated cal(l)andria type.
Above-mentioned embodiment is just in order to illustrate the specific embodiment of the present invention, and the present invention is also only not limited to above-mentioned embodiment.Can suitable change be carried out to above-mentioned embodiment or the feature of the respective embodiments described above be combined arbitrarily, only otherwise depart from the scope of the aim described in claims, all belong to the present invention and want protection domain.
Such as, in the above-described embodiment, the treatment unit containing organism sewage includes aerobic slot 4, micro-filtration or ultrafiltration membrane separating device 5, water softener 6, instead soaks into film or nanofiltration membrane separation device 7, alkali adding set 8, evaporation concentration device 9 and condensing water transfer unit etc.But, the present invention is not limited thereto, treatment unit containing organism sewage comprises aerobic slot 4, micro-filtration or ultrafiltration membrane separating device 5, instead soak into film or nanofiltration membrane separation device 7, and evaporation concentration device 9 can realize main purpose of the present invention, or also can comprise these devices containing the treatment unit of organism sewage, and any one or a few in water softener 6, alkali adding set 8 and condensing water transfer unit.
Such as, in the above-described embodiment, medicine wash operation comprise hypochlorite liquid injection process, place operation, empty aeration operation, washing step, discharge operation, acid liquid injection process, place operation, empty aeration operation, washing step, discharge operation.But the present invention is not limited thereto, medicine is washed operation and also only can be comprised hypochlorite liquid injection process, place operation, empty aeration operation, washing step, discharge operation.
Claims (19)
1., containing a treatment unit for organism sewage, it is characterized in that having:
Under aerobic conditions, aerobic treatment is containing the aerobic slot of organism sewage;
The process water of described aerobic slot is carried out to micro-filtration or the ultrafiltration membrane separating device of solid-liquid separation;
The counter of desalting treatment is carried out to the filtered liquid of described micro-filtration or ultrafiltration membrane separating device and soaks into film or nanofiltration membrane separation device; And
Evaporation concentration device concentrated is further carried out to described anti-condensed water of soaking into film or nanofiltration membrane separation device.
2. the treatment unit containing organism sewage as claimed in claim 1, it is characterized in that, also have: ion exchange unit, instead soak into before film or nanofiltration membrane separation device carry out desalting treatment to described filtered liquid described, described ion exchange unit carries out ion-exchange to described filtered liquid.
3. the treatment unit containing organism sewage as claimed in claim 2, is characterized in that also having: alkali adding set, and before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water.
4. the treatment unit containing organism sewage as claimed in claim 2, it is characterized in that also having: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
5. the treatment unit containing organism sewage as claimed in claim 2, is characterized in that also having: alkali adding set, and before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water; And condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
6. the treatment unit containing organism sewage as claimed in claim 1, is characterized in that also having: alkali adding set, and before described evaporation concentration device concentrates further to described condensed water, described alkali adding set adds alkali to described condensed water.
7. the treatment unit containing organism sewage as claimed in claim 6, it is characterized in that also having: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
8. the treatment unit containing organism sewage as claimed in claim 1, it is characterized in that also having: condensing water transfer unit, the condensing water that the moisture that described evaporation concentration device evaporates by described condensing water transfer unit is condensing obtained is transported to described aerobic slot.
9., containing a treatment process for organism sewage, it is characterized in that having:
Aerobic slot aerobic treatment under aerobic conditions is utilized to contain the aerobic treatment operation of organism sewage;
Micro-filtration or the process water of ultrafiltration membrane separating device to described aerobic slot is utilized to carry out the solid-liquid separation process of solid-liquid separation;
Utilize and instead soak into the desalting treatment operation that film or the nanofiltration membrane separation device filtered liquid to described micro-filtration or ultrafiltration membrane separating device carries out desalting treatment; And
Evaporation concentration device is utilized to carry out evaporation concentration operation concentrated further to described anti-condensed water of soaking into film or nanofiltration membrane separation device.
10. the treatment process containing organism sewage as claimed in claim 9, is characterized in that also having: before described desalting treatment operation, utilizes ion exchange unit to carry out the ion-exchange process of ion-exchange to described filtered liquid.
11., as claimed in claim 10 containing the treatment process of organism sewage, is characterized in that also having: before described evaporation concentration operation, utilize alkali adding set to add operation to the alkali that described condensed water adds alkali.
12. as claimed in claim 10 containing the treatment process of organism sewage, it is characterized in that also having: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
13., as claimed in claim 10 containing the treatment process of organism sewage, is characterized in that also having: before described evaporation concentration operation, utilize alkali adding set to add operation to the alkali that described condensed water adds alkali; And condensing the obtained condensing water of the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is transported to the condensing water conveying operation of described aerobic slot.
14., as claimed in claim 9 containing the treatment process of organism sewage, is characterized in that also having: before described evaporation concentration operation, utilize alkali adding set to add operation to the alkali that described condensed water adds alkali.
15. as claimed in claim 14 containing the treatment process of organism sewage, it is characterized in that also having: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
16. as claimed in claim 9 containing the treatment process of organism sewage, it is characterized in that also having: the condensing water that the moisture utilizing condensing water transfer unit to be evaporated by described evaporation concentration device is condensing obtained is transported to the condensing water conveying operation of described aerobic slot.
17. as claimed in claim 9 containing the treatment process of organism sewage, it is characterized in that, also have: under the state stopping described solid-liquid separation process, wash operation to the medicine that the filtering membrane of the film separation unit of described micro-filtration or ultrafiltration membrane separating device cleans, this medicine is washed operation and is had:
Liquid is injected the film separation unit of described micro-filtration or ultrafiltration membrane separating device to clean the liquid injection process of described filtering membrane;
When described film separation unit has been filled with liquid, the aeration making described micro-filtration or ultrafiltration membrane separating device keep utilizing aeration tube to carry out has run the placement operation of the state stopped;
Described micro-filtration or ultrafiltration membrane separating device is made to carry out the empty aeration operation of described aeration operation;
Water is injected the film separation unit of described micro-filtration or ultrafiltration membrane separating device to wash the washing step of described filtering membrane; And
The water after washing is made to be discharged to the discharge operation of the membrane sepn groove of described micro-filtration or ultrafiltration membrane separating device by described aeration tube from described film separation unit.
18. as claimed in claim 17 containing the treatment process of organism sewage, and it is characterized in that, described liquid is hypochlorite liquid.
19., as claimed in claim 18 containing the treatment processs of organism sewage, is characterized in that, then carry out once described medicine and wash operation, after medicine once wash in operation, described liquid is acid liquid.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310413803.5A CN104418472A (en) | 2013-09-11 | 2013-09-11 | Treatment device and treatment method of wastewater containing organic matters |
| JP2014546219A JP6264296B2 (en) | 2013-09-11 | 2014-09-08 | Organic wastewater treatment apparatus and treatment method |
| PCT/JP2014/073649 WO2015037557A1 (en) | 2013-09-11 | 2014-09-08 | Apparatus and method for treating organic-containing wastewater |
| CN201480050088.6A CN105555717B (en) | 2013-09-11 | 2014-09-08 | The processing unit and processing method of organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310413803.5A CN104418472A (en) | 2013-09-11 | 2013-09-11 | Treatment device and treatment method of wastewater containing organic matters |
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| CN104418472A true CN104418472A (en) | 2015-03-18 |
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| CN201480050088.6A Active CN105555717B (en) | 2013-09-11 | 2014-09-08 | The processing unit and processing method of organic sewage |
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| JP (1) | JP6264296B2 (en) |
| CN (2) | CN104418472A (en) |
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Cited By (3)
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|---|---|---|---|---|
| CN105293805A (en) * | 2015-11-11 | 2016-02-03 | 光大环保技术研究院（深圳）有限公司 | High-salinity high-hardness waste water zero-discharge processing apparatus and method thereof |
| CN106565044A (en) * | 2015-10-08 | 2017-04-19 | 新世膜科技股份有限公司 | Recovery processing system of concentrated waste water of tanning |
| CN113800557A (en) * | 2021-09-27 | 2021-12-17 | 上海安赐环保科技股份有限公司 | Water recycling system and method for preparing titanium dioxide calcination crystal seeds by sulfuric acid method |
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| CN107344800A (en) * | 2017-08-22 | 2017-11-14 | 贵阳台农种养殖有限公司 | A kind of aquaculture wastewater processing system |
| CN108675500A (en) * | 2018-05-31 | 2018-10-19 | 芜湖裕优机械科技有限公司 | A kind of sewage treatment pot and its cleaning method that can have cleaning filter membrane function |
| KR101948185B1 (en) * | 2018-10-08 | 2019-02-14 | (주)이앤씨 | Treatment of reverse osmosis concentrated water using Electro-Dialysis system and vacuum evaporation drying system |
| CN110028201A (en) * | 2019-05-08 | 2019-07-19 | 杭州齐创环境工程有限公司 | A kind of waste emulsified mixture resource utilization processing system and technique |
| WO2021117309A1 (en) * | 2019-12-13 | 2021-06-17 | 株式会社 東芝 | Water treatment device |
| CN111807394B (en) * | 2020-07-24 | 2022-10-28 | 沈阳工业大学 | A kind of method for removing organic matter from mother liquor of Bayer process |
| CN113880339B (en) * | 2021-10-09 | 2024-01-16 | 福建省环境保护设计院有限公司 | Advanced treatment and reuse technology for high-salinity industrial wastewater |
| CN115818880A (en) * | 2022-12-07 | 2023-03-21 | 北京国泷环保科技有限公司 | A method for treating high-salt, high-organic, and high-hardness wastewater |
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| Publication number | Publication date |
|---|---|
| JPWO2015037557A1 (en) | 2017-03-02 |
| CN105555717A (en) | 2016-05-04 |
| WO2015037557A1 (en) | 2015-03-19 |
| JP6264296B2 (en) | 2018-01-24 |
| CN105555717B (en) | 2018-06-05 |
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Address after: Japan Tokyo Marunouchi Chiyoda Ku, 1-1-1 Applicant after: Mitsubishi Kasei Corporation Address before: Japan Tokyo Marunouchi Chiyoda Ku, 1-1-1 Applicant before: Mitsubishi Reiyon Co., Ltd. |
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Application publication date: 20150318 |