CN106007223A - Forward osmosis membrane and MF (microfiltration) membrane coupling anaerobic sewage treatment method - Google Patents
Forward osmosis membrane and MF (microfiltration) membrane coupling anaerobic sewage treatment method Download PDFInfo
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- CN106007223A CN106007223A CN201610560793.1A CN201610560793A CN106007223A CN 106007223 A CN106007223 A CN 106007223A CN 201610560793 A CN201610560793 A CN 201610560793A CN 106007223 A CN106007223 A CN 106007223A
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- 239000012528 membrane Substances 0.000 title claims abstract description 107
- 238000001471 micro-filtration Methods 0.000 title claims abstract description 59
- 239000010865 sewage Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 30
- 238000009292 forward osmosis Methods 0.000 title claims abstract description 28
- 230000008878 coupling Effects 0.000 title claims abstract description 18
- 238000010168 coupling process Methods 0.000 title claims abstract description 18
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 238000004062 sedimentation Methods 0.000 claims abstract description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 10
- 230000008569 process Effects 0.000 claims abstract description 9
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 7
- 238000001179 sorption measurement Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 30
- 239000003463 adsorbent Substances 0.000 claims description 12
- 230000004907 flux Effects 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 10
- 238000005273 aeration Methods 0.000 claims description 8
- 230000000694 effects Effects 0.000 claims description 8
- 238000005374 membrane filtration Methods 0.000 claims description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims description 8
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 7
- 239000011574 phosphorus Substances 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 239000004952 Polyamide Substances 0.000 claims description 5
- 239000004695 Polyether sulfone Substances 0.000 claims description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 229920002647 polyamide Polymers 0.000 claims description 5
- 229920006393 polyether sulfone Polymers 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 230000033228 biological regulation Effects 0.000 claims description 3
- 239000001506 calcium phosphate Substances 0.000 claims description 3
- 229910000389 calcium phosphate Inorganic materials 0.000 claims description 3
- 235000011010 calcium phosphates Nutrition 0.000 claims description 3
- 229920005989 resin Polymers 0.000 claims description 3
- 239000011347 resin Substances 0.000 claims description 3
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 claims description 3
- 230000003204 osmotic effect Effects 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 claims 1
- 239000001913 cellulose Substances 0.000 claims 1
- 229920002678 cellulose Polymers 0.000 claims 1
- ILJSQTXMGCGYMG-UHFFFAOYSA-N triacetic acid Chemical compound CC(=O)CC(=O)CC(O)=O ILJSQTXMGCGYMG-UHFFFAOYSA-N 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 8
- 229910019142 PO4 Inorganic materials 0.000 abstract description 4
- 238000009825 accumulation Methods 0.000 abstract description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract description 4
- 239000010452 phosphate Substances 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract 2
- 230000029087 digestion Effects 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 239000002033 PVDF binder Substances 0.000 description 4
- 239000004743 Polypropylene Substances 0.000 description 4
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 4
- 229920002492 poly(sulfone) Polymers 0.000 description 4
- 229920001155 polypropylene Polymers 0.000 description 4
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 4
- -1 alkene nitrile Chemical class 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 229920006304 triacetate fiber Polymers 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 229920006221 acetate fiber Polymers 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 235000020188 drinking water Nutrition 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000003673 groundwater Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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- 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
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0023—Accessories; Auxiliary operations
-
- 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
- B01D2311/2688—Biological processes
-
- 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
- B01D61/002—Forward osmosis or direct osmosis
-
- 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
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- 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
- C02F2303/14—Maintenance of water treatment installations
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2866—Particular arrangements for anaerobic reactors
- C02F3/2893—Particular arrangements for anaerobic reactors with biogas recycling
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- 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)
Abstract
The invention discloses a forward osmosis membrane and MF (microfiltration) membrane coupling anaerobic sewage treatment method, and belongs to the technical field of sewage treatment. For municipal sewage, the method comprises the following steps: causing raw water to enter an anaerobic reaction area through a water feed pump, and collecting generated biogas for reuse after the biogas passes through a water seal; for part of sewage, implementing separation and purification under the action of a forward osmosis membrane, and then implementing reuse by treatment with a reverse osmosis membrane; for the other part of sewage, implementing separation and purification by virtue of an MF membrane, then recycling phosphate by virtue of a sedimentation tank, and finally implementing up-to-standard effluent discharge or reuse by virtue of an activated carbon adsorption column. According to the method, forward osmosis membrane and MF membrane technologies and an anaerobic digestion technology are coupled into a sewage treatment process, so that effluent is guaranteed to stably meet reclaimed water reuse requirements, and a smaller area is occupied; organic matters in the sewage are recycled in form of biogas; the phosphate in the sewage is recycled; salinity accumulation of forward osmosis is relieved, and membrane pollution is effectively controlled; the whole system can be automatically controlled.
Description
Technical field
The present invention relates to a kind of anaerobism sewage water treatment method coupling forward osmosis membrane and micro-filtration membrane, belong to technical field of sewage.
Background technology
A large amount of discharges of sewage, had both wasted resource, had added again water body environment load.Along with world water resources and the day of the energy
Benefit shortage, owing to having contained the resource such as abundant water resource and a large amount of C, N, P, sewage has been counted as a kind of water source and money
Source.In this context, the sewage treatment process for the purpose of reusing sewage and energy recovery has been subjected to more and more pay attention to.
The most such a kind of technique of anaerobic membrane bioreactor (anaerobic membrane bioreactor, AnMBR), is processing
Methane can be reclaimed during sewage, and the introducing of microfiltration or Ultra filtration membrane technology substantially increases the effect of anaerobic effluent.
But, AnMBR there is also effluent quality can not direct reuse and the problem such as fouling membrane is heavier.
Additionally, also there is scholar to propose anaerobism forward osmosis membrane bioreactor (anaerobic forward osmosis membrane
Bioreactor, AnFOMBR).Compared with AnMBR, owing to just permeating efficiently cutting of (forward osmosis, FO) film
The advantages such as staying ability and high contamination resistance, it is good that AnFOMBR has effluent quality, and energy consumption is low and fouling membrane trend is little.So
And, owing to solute is retained and reverse salt penetration by FO film, the problem that AnFOMBR there is also high salinity.Such as, have
Singapore scholar finds when studying AnFOMBR: in 22 days, in reactor, salinity increases to from initial 1.0mS/cm
20.5mS/cm, water flux drops to 3.5LMH from 9.5LMH, the 58% of methane average product the most reasonable opinion gas production.Salt
The accumulation of degree, strongly limit the further application of reactor.At present, high salinity solution party in AnFOMBR also it is not related to
The report of method.
Summary of the invention
In order to solve the problems referred to above, a kind of Novel anaerobic coupling forward osmosis membrane and micro-filtration membrane that proposes of the invention is reacted
Device (MFO-AnMBR) and anaerobism sewage treatment process.The reactor of the present invention uses microfiltration (microfiltration, MF)
Film alleviates the accumulation of salinity, and improves the flux of FO film further.MFO-AnMBR is in sewage disposal process, permissible
Reclaim biogas；The effluent quality of FO film is relatively good, can be used for reuse or recharge of groundwater money as the water quality of a kind of high-quality
Source；MF water outlet, while carrying out urban reclaimed water reuse, can carry out the recovery of phosphorus.Therefore, MFO-AnMBR technique
It is possible not only to realize reusing sewage, and resource and energy recovery can be realized, be a kind of sustainable sewage disposal faced the future
Technology, the development to sewage disposal technology from now on has good supplementing.
First purpose of the present invention there is provided a kind of anaerobic reactor coupling forward osmosis membrane and micro-filtration membrane
(MFO-AnMBR)。
Described anaerobic reactor mainly includes film reaction device, draws at liquid pool, reverse osmosis (reverse osmosis, RO) film
Reason device, sedimentation tank, adsorbent equipment；Described film reaction device includes MF membrane module and FO membrane module；Described MF film group
Part is connected with sedimentation tank by pipeline, and sedimentation tank is connected with adsorbent equipment by pipeline；Described FO membrane module passes through pipeline and draws
Take liquid pool to connect, draw liquid pool and be connected with RO membrane treatment appts.
In one embodiment, the bottom in described film reaction device is provided with aeration tube, biogas recirculation pump one end and aeration tube
Connecting, the other end extends to the top of film reaction device.
In one embodiment, the top of described film reaction device is connected with water seal arrangement by pipeline.
In one embodiment, described sedimentation tank is connected with pH controller.
In one embodiment, described pH controller is connected with NaOH solution pond.
In one embodiment, the middle and upper part of described sedimentation tank is connected with adsorbent equipment with water pump by pipeline.
In one embodiment, described adsorbent equipment is active carbon adsorption column.
In one embodiment, described FO membrane module with draw liquid pool and constitute circulation by drawing liquid circulating pump and pipeline.
In one embodiment, draw liquid pool described in and constitute circulation with RO membrane treatment appts by high-pressure pump and pipeline.
In one embodiment, the material of the FO film in described FO membrane module is triacetate fiber (CTA) film, polyamide
(TFC) any one in film, polyethersulfone resin (PES).
In one embodiment, the MF film in described MF membrane module be Kynoar (PVDF), polysulfones (PSF), poly-third
Any one of alkene nitrile (PAN), polrvinyl chloride (PVC), polypropylene (PP) etc..
In one embodiment, the aperture of described MF film is 0.1-1 micron.
In one embodiment, described MF membrane module is in plate film assembly, hollow fiber film assembly or tubular membrane component one
Kind
In one embodiment, the RO film in described RO membrane treatment appts is acetate fiber (CTA) film, polyamide (TFC)
Any one in composite membrane.
Second object of the present invention is to provide a kind of anaerobism sewage water treatment method, and described method is that the coupling utilizing the present invention is just oozed
The anaerobic reactor of permeable membrane and micro-filtration membrane carries out sewage disposal.
In described method, after sewage enters the film reaction device of anaerobic reactor, under the effect of anaerobe, realize Organic substance
Degraded and conversion, the biogas of generation can be circulated by biogas recirculation pump in film reaction device, finally processes through water seal
Rear recovery；Under the permeable pressure head effect drawn between liquid and mud mixed liquid, water passes through FO film, then is obtained by RO film
Recycle-water, the liquid that draws after concentration continues on for FO film and carries out the extraction of water；Controlled by the operating flux of regulation and control MF film
The discharge of the solute in film reaction device, thus realize the control of salinity；MF film water outlet first under alkaline environment with phosphate
The form of precipitation realizes the recovery to phosphorus, then adsorbs remaining ammonia nitrogen by adsorbent equipment.
In one embodiment, the described operating flux by regulating and controlling MF film, refer to control reactor (in film reaction device
Mixture) in electrical conductivity be 5-6mS/cm.
In one embodiment, described in draw the initial concentration of liquid be 0.5MNaCl, drawing liquid cycle rate is 0.4L/min.
In one embodiment, in described method, biogas recirculation speed is 2L/min.The form using biogas recirculation realizes control
FO film processed and the Environmental capacity of MF film and the effective of anaerobic sludge mix.
In one embodiment, described alkaline environment refers at pH 10～12.
In one embodiment, described alkaline environment refers to control pH about 11.0 by pH controller.
In one embodiment, being added with activated carbon in described adsorbent equipment, activated carbon dosage is 50g/L, and the time of staying is
12h。
In one embodiment, microfiltration (MF) film is Kynoar (PVDF) material.
The reactor of the present invention and sewage water treatment method, after the double filtration of FO film and RO film, effluent quality is relatively good,
Emergency drinking water or recharge of groundwater resource can be used as the water quality of a kind of high-quality；The addition of MF film not only solves
The problem of salinity accumulation, and improve the flux of FO film；MF water outlet COD is less than 50mg/L, and ammonia nitrogen cannot meet
Urban reclaimed water reuse standard, by realizing the recovery to phosphorus with the form of calcium phosphate precipitation, then by living under alkaline environment
Property charcoal adsorb remaining ammonia nitrogen, thus both ensure that MF water outlet reached urban reclaimed water reuse standard, achieved again the money to phosphorus
Sourceization reclaims；The biogas produced in anaerobic processes can be recycled.Therefore, MFO-AnMBR technique is possible not only to realize dirt
Water reaches or the water quality requirement that is better than in " urban sewage reutilization urban reclaimed water water quality " (GB/T 18920-2002) returns
For producing, and the recovery of biogas and phosphorus can be realized, be a kind of sustainable sewage disposal technology faced the future, to from now on
The development of sewage disposal technology has good supplementing.
The relatively conventional anaerobic membrane bioreactor of the present invention has the advantage that
(1) tradition AnFOMBR anaerobic reactor, owing to water inlet solute is retained and reverse salt penetration, reactor by FO film
In salinity can accumulate, affect the operation of device.FO film and MF film are coupled and use by the present invention, can be by changing MF
The water flux of film controls the discharge of the solute in reactor, thus realizes the control of salinity；The sewage disposal of the present invention is divided into two
Part, the water outlet of FO film, through RO PROCESS FOR TREATMENT, can reach the requirement of drinking water, and the water outlet of MF film can reach " city
City's reuse of wastewater urban reclaimed water water quality " water quality requirement in (GB/T 18920-2002), it is back to produce.
(2) FO film uses permeable pressure head rather than hydraulic pressuring difference as driving force, and fouling membrane trend is less, and plant running is more
Stable.
(3) realizing can realizing while methane recovery utilizes the recovery of phosphorus.
(4) use the method for the present invention to carry out sewage disposal, in principle, by the extraction to solute of the MF film, reaction can be controlled
In device, salinity is any numerical value.But, if electrical conductivity controls higher, fouling membrane is more serious, then water flux declines very fast, unfavorable
Operation steady in a long-term in reactor；If electrical conductivity controls relatively low, then affect phosphatic enrichment and organic efficiency.Pass through MF
Mixed liquor electrical conductivity is controlled not only to maintain preferable water flux but also can reclaim more phosphate at 5-6mS/cm by film, and
And anaerobic reactor can run steadily in the long term.
Accompanying drawing explanation
Fig. 1 is the structural representation that the present invention couples the anaerobic reactor (MFO-AnMBR) of forward osmosis membrane and micro-filtration membrane；In figure, 1
Intake pool, 2 intake pumps, 3 aeration tubes, 4 MF membrane modules, 5 biogas recirculation pumps, 6 FO membrane modules, 7 draw liquid
Circulating pump, 8 draw liquid pool, 9 high-pressure pumps, 10 RO membrane treatment appts, 11 suction pumps, 12 NaOH solution ponds, and 13
PH controller, 14 sedimentation tanks, 15 water pumps, 16 adsorbent equipments, 17 water seal arrangements.
Detailed description of the invention
Below in conjunction with embodiment, the invention will be further described:
Embodiment 1: coupling forward osmosis membrane and the anaerobic reactor of micro-filtration membrane
Fig. 1 is the structural representation of the anaerobic reactor (MFO-AnMBR) coupling forward osmosis membrane and micro-filtration membrane of the present invention.
Described anaerobic reactor mainly includes film reaction device, draws liquid pool 8, RO membrane treatment appts 10, sedimentation tank 14, suction
Adsorption device 16；Described film reaction device includes MF membrane module 4, FO membrane module 6；Described MF membrane module 4 by pipeline with
Sedimentation tank 14 connects, and sedimentation tank 14 is connected with adsorbent equipment 16 by pipeline；Described FO membrane module 6 passes through pipeline and draws
Liquid pool 8 connects, and draws liquid pool 8 and is connected with RO membrane treatment appts 10.
Described film reaction bottom of device is provided with aeration tube 3, and biogas recirculation pump 5 one end is connected with aeration tube 3, and the other end extends
Top to film reaction device.The biogas produced can be circulated in film reaction device by biogas recirculation pump 5, uses natural pond
The form of gas circulation realizes controlling effective mixing of FO film and the control of MF fouling membrane and anaerobic sludge.
The top of described film reaction device is connected with water seal arrangement 17 by pipeline.Described sedimentation tank 14 and pH controller 13 phase
Even.Described pH controller 13 is connected with NaOH solution pond 12.
The middle and upper part of described sedimentation tank is connected with adsorbent equipment 16 with water pump 15 by pipeline.
Alternatively, described adsorbent equipment 16 is active carbon adsorption column.Ammonia nitrogen is adsorbed, reaches urban reclaimed water reuse standard.
Additionally, described FO membrane module 6 with draw liquid pool 8 and constitute circulation by drawing liquid circulating pump 7 and pipeline.After concentration
Draw liquid to continue on for FO film and carry out the extraction of water.By with osmotic pressure as driving force, it is achieved retaining of FO film.
Alternatively, draw liquid pool 8 described in and constitute circulation with RO membrane treatment appts 10 by high-pressure pump 9 and pipeline.Through FO film
The water processed with RO film, can reach high-quality water outlet requirement.
Alternatively, the material of the FO film in described FO membrane module 6 is triacetate fiber (CTA) film, polyamide (TFC)
Any one in film, polyethersulfone resin (PES).
Alternatively, the MF film in described MF membrane module 4 be Kynoar (PVDF), polysulfones (PSF), polyacrylonitrile (PAN),
Any one of polrvinyl chloride (PVC), polypropylene (PP) etc.；The salinity in reactor can be controlled by MF membrane module to accumulate.
Alternatively, the RO film in described RO membrane treatment appts is acetate fiber (CTA) film, polyamide (TFC) composite membrane
In any one.
Embodiment 2: utilize the MFO-AnMBR of the present invention to carry out sewage disposal
Use coupling forward osmosis membrane and the novel anaerobic reactor (MFO-AnMBR) of micro-filtration membrane of structure as shown in Figure 1,
Run under room temperature.
Being passed through the simulation town sewage through artificial preparation, its water quality index is: TOC:143.97 ± 2.23mg/L, NH4-N:
28.95 ± 2.34mg/L, TN:30.71 ± 2.18mg/L, TP:2.70 ± 0.34mg/L.Membrane module FO and MF Flat Membrane group
Part, respectively triacetate fiber (CTA) material and Kynoar (PVDF) material, membrane area is 0.025m2, its
The average pore size of middle MF is 0.2 μm.Water inlet is squeezed into MFO-AnMBR from intake pool 1 by intake pump 2, at biogas recirculation pump
Mix rapidly under the effect of 5.A part of mixed liquor passes through FO membrane module 6 under the effect drawing liquid 8, it is achieved the first of sewage
Secondary purification, the second time through the RO film of RO membrane treatment appts 10 purifies the recycled water obtaining high-quality the most again.Meanwhile,
Another part mixed liquor passes through MF membrane module 4 under the effect of suction pump 11, subsequently into sedimentation tank 14 under alkaline environment
Form calcium phosphate precipitation, enter active carbon adsorption column 16 finally by water pump 15 and obtain satisfied " urban sewage reutilization city
Miscellaneous water water quality " (GB/T 18920-2002) recycled water of requiring.MFO-AnMBR uses the circulation self producing biogas real
Existing mixed liquor stirring and control membrane fouling, unnecessary biogas is collected after water seal 17.MFO-AnMBR processing means
Sludge retention time be 80d, mixed liquor concentration of suspension is about 2.0g/L, and aeration cycle speed is 2L/min, temperature
It it is 25 DEG C.
The anaerobic reactor of the present invention runs 100d, and mixed liquor electrical conductivity maintains 5-6mS/cm all the time, and membrane module does not carries out appointing
What cleans.After process, FO effluent quality is: TOC:21mg/L, NH4-N:22.48mg/L, TN:23.92mg/L,
TP:0-0.32mg/L, MF effluent quality is COD:20mg/L, TP:0.1mg/l, NH4-N:8.05mg/L, water outlet
Water quality reaches the water quality requirement in " urban sewage reutilization urban reclaimed water water quality " (GB/T 18920-2002).Methane
Productivity is 0.23-0.27L CH4g-1COD。
Although the present invention is open the most as above with preferred embodiment, but it is not limited to the present invention, any person skilled in the art,
Without departing from the spirit and scope of the present invention, all can do various changes and modification, therefore protection scope of the present invention should be with
What claims were defined is as the criterion.
Claims (10)
1. the anaerobic reactor coupling forward osmosis membrane and micro-filtration membrane, it is characterised in that described anaerobic reactor mainly includes film
Reaction unit, draw liquid pool, reverse osmosis membrane processing device, sedimentation tank, adsorbent equipment；Described film reaction device includes micro-filtration membrane
Assembly and forward osmosis membrane assembly；Described micro-filtration membrane module is connected with sedimentation tank by pipeline, and sedimentation tank passes through pipeline and adsorbent equipment
Connect；Described forward osmosis membrane assembly is connected with drawing liquid pool by pipeline, draws liquid pool and is connected with reverse osmosis membrane processing device.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described film is anti-
Answering the bottom in device to be provided with aeration tube, biogas recirculation pump one end is connected with aeration tube, and the other end extends to film reaction device
Top.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described just ooze
Permeable membrane assembly with draw liquid pool and constitute circulation by drawing liquid circulating pump and pipeline.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described in draw
Liquid pool constitutes circulation with reverse osmosis membrane processing device by high-pressure pump and pipeline.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described absorption
Device is active carbon adsorption column.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described film is anti-
The top answering device is connected with water seal arrangement by pipeline.
Coupling forward osmosis membrane the most according to claim 1 and the anaerobic reactor of micro-filtration membrane, it is characterised in that described just ooze
The material of the forward osmosis membrane in permeable membrane assembly is any one in triacetate cellulose membrane, polyamide membrane, polyethersulfone resin.
8. an anaerobism sewage water treatment method, it is characterised in that described method is to utilize the arbitrary described coupling of claim 1～7
Forward osmosis membrane and the anaerobic reactor of micro-filtration membrane.
Method the most according to claim 8, it is characterised in that in described method, the film that sewage enters anaerobic reactor is anti-
After answering device, realizing organic degraded and conversion under the effect of anaerobe, the biogas of generation can pass through biogas recirculation
Pump is circulated in film reaction device, finally reclaims after water seal processes；At the osmotic pressure drawn between liquid and mud mixed liquid
Under difference effect, water passes through forward osmosis membrane, then obtains recycle-water by reverse osmosis membrane, and the liquid that draws after concentration continues on for just permeating
Film carries out the extraction of water；Control the solute in film reaction device by the operating flux of regulation and control micro-filtration membrane to discharge, thus realize salt
The control of degree；First micro-filtration membrane water outlet realizes the recovery to phosphorus with the form of calcium phosphate precipitation under alkaline environment, then by inhaling
Adsorption device adsorbs remaining ammonia nitrogen.
Method the most according to claim 9, it is characterised in that the operating flux of described regulation and control micro-filtration membrane, refers to control instead
Answering the electrical conductivity in device is 5-6mS/cm.
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