CN104016477A - Immersed anaerobic positive permeable membrane bioreactor - Google Patents
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- 239000012528 membrane Substances 0.000 title claims abstract description 91
- 239000010802 sludge Substances 0.000 claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000005273 aeration Methods 0.000 claims abstract description 14
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 238000009292 forward osmosis Methods 0.000 claims description 46
- 239000007789 gas Substances 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 24
- 238000007654 immersion Methods 0.000 claims description 17
- 239000012141 concentrate Substances 0.000 claims description 9
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 6
- 150000001720 carbohydrates Chemical class 0.000 claims description 3
- 229920002301 cellulose acetate Polymers 0.000 claims description 3
- 229910017053 inorganic salt Inorganic materials 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 150000003016 phosphoric acids Chemical class 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 239000012266 salt solution Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 9
- 230000002349 favourable effect Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 20
- 230000008569 process Effects 0.000 description 19
- 230000008901 benefit Effects 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 11
- 239000010841 municipal wastewater Substances 0.000 description 9
- 239000010865 sewage Substances 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 8
- 230000006872 improvement Effects 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 230000002906 microbiologic effect Effects 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 230000002269 spontaneous effect Effects 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000010893 paper waste Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000003245 working effect Effects 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
-
- 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
- B01D61/0022—Apparatus therefor
-
- 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
- B01D61/0024—Controlling or regulating
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to an immersed anaerobic positive permeable membrane bioreactor which comprises a water inlet tank, a closed anaerobic reactor tank body, a positive permeable membrane separation system, a marsh gas collector and a marsh gas circulating aerating system, wherein the water inlet tank is connected with the anaerobic reactor tank body through a water inlet pump; the positive permeable membrane separation system comprises a positive permeable membrane component, a sucked solution storage tank, a reverse osmosis concentrating component, a gas circulation pump and a concentrating pump; the marsh gas circulating aerating system comprises an aeration pipe, a gas circulation pump and a gas pipeline; the aeration pipe is arranged on the lower part of the positive permeable membrane component; the aeration pipe is connected with the gas circulation pump through the gas pipeline; the gas circulation pump is connected with the upper space of the anaerobic reactor tank body; and the marsh gas collector is also connected with the upper space of the anaerobic reactor tank body. The immersed anaerobic positive permeable membrane bioreactor can generate a energy source, and has the characteristics of favorable effluent water quality, light membrane pollution level, low operating cost, low sludge yield, high organic load and small occupied area.
Description
Technical field
The invention belongs to sewage disposal and membrane separation technique field, be specifically related to a kind of immersion type anaerobic forward osmosis membrane bioreactor.
Technical background
Shortage of water resources and water environment pollution are the huge challenges that current mankind faces, one of top-priority key subjects of Ye Shi China the Implement of sustainable development strategic demand.Reuse is processed and realized to sewage is the important channel addressing this problem.Along with the fast development of national economy, the shortage of water resources of China and water environment pollution situation are particularly serious, therefore in the urgent need to developing efficient sewage disposal and reuse technology.
Water anaerobic biological treatment (AD) technology has that reduced investment, energy consumption are low, recoverable biogas energy, load high, produce the plurality of advantages such as mud is few, anti impulsion load, in wastewater treatment, be with a wide range of applications.Anaerobic membrane bioreactor (AnMBR) is a kind of Novel sewage treatment technology being combined with anaerobic biological treatment unit by film separation unit.Due to the introducing of membrane module, in retaining AD technological merit, also introduce series of advantages, as little in water outlet, low sludge yield, high organic loading, the floor space of sludge retention, high-quality completely and capable of recovering energy source.And adopt immersion configuration can effectively reduce the energy consumption in AnMBR system operational process.The effect that these advantages are brought is very significant, taking China as example, existing municipal wastewater treatment technology mainly carrys out decomposing pollutant by oxygen, and its power consumption has accounted for 3% of national wastage in bulk or weight, is difficult to and at least produce 2,000 ten thousand tons every year simultaneously the mud of effectively processing.Adopt immersion AnMBR technical finesse municipal wastewater not only can produce the water outlet of the energy and high-quality, but also can make the productive rate of excess sludge reduce by 90%.
Although AnMBR technology has plurality of advantages, also there are two large technical barriers in its widespread use.The one, membrane pollution problem, membrane pollution problem is considered to restrict the bottleneck of AnMBR widespread use.Film pollutes and causes membrane flux to decline, and increases the frequency that film cleans and membrane module is changed, and has had a strong impact on economy and the practicality of AnMBR technology.In AnMBR actual moving process, often adopt increase aeration, add the measures such as medicament, reduction sludge concentration and small throughput operation to reduce film pollution, but these measures generally all exist, and energy consumption is high, expense is high, sacrifice the deficiencies such as AnMBR handling property, and actual effect is often also also not obvious.The 2nd, Anaerobic Microbiological Treatment Technology comprises that AnMBR technology is as poor in the treatment effect of the ammonia nitrogen in municipal wastewater to general waste water, and in effluent quality, ammonia nitrogen index is often not up to standard.
Just permeate the new membrane isolation technique that (FO) is a kind of concentration drive of getting up of development in recent years, just permeating the membrane sepn process (as micro-filtration, ultrafiltration and reverse osmosis membrane process) that is different from pressure-driven type, it does not need extra hydraulic pressure as motivating force, and relies on the spontaneous membrane sepn of realizing of permeable pressure head drawing between liquid and stock liquid.If low pressure is even without press operation, thereby energy consumption is lower; Many pollutents are almost held back to (can hold back ammonia nitrogen), good separating effect completely; Low film contamination characteristics; Membrane process and equipment are simple etc.These advantages are expected to solve the two large technical barriers that exist in AnMBR technology.Thereby in AnMBR process, introduce forward osmosis membrane process can be effectively in conjunction with AnMBR and forward osmosis membrane process advantage separately.
Summary of the invention
In order to solve above-mentioned technical problem, the present invention aims to provide a kind of immersion type anaerobic forward osmosis membrane bioreactor system.This system has advantages of that the water outlet of high-quality, low sludge yield, film pollution level are low, capable of recovering energy source, high organic loading, floor space is little and operation energy consumption is low.Be suitable for the processing of municipal wastewater and commonly industrial wastewater.
In order to realize above-mentioned object, the present invention has adopted following technical scheme:
A kind of immersion type anaerobic forward osmosis membrane bioreactor, this reactor comprises anaerobic reactor casing, forward osmosis membrane separation system, sludge gas collecting device and the biogas recirculation aerating system of inlet chest, sealing, described inlet chest connects described anaerobic reactor casing by intake pump, described forward osmosis membrane separation system comprises forward osmosis membrane assembly, draw liquid storage tank, reverse osmosis concentration assembly, gas recycle pump and concentrate pump, the submergence of forward osmosis membrane assembly is arranged in anaerobic reactor casing, the top of forward osmosis membrane assembly is connected with draws liquid pipeline, draw liquid pipeline and connect the described liquid storage tank that draws, the bottom of forward osmosis membrane assembly is connected with outlet pipeline, outlet pipeline connects described reverse osmosis concentration assembly by concentrate pump, reverse osmosis concentration assembly top connects the described liquid storage tank that draws by concentrated pipeline is set, on reverse osmosis concentration assembly, be provided with rising pipe, described biogas recirculation aerating system comprises aeration tube, gas recycle pump and gas tube, and aeration tube is arranged on the bottom of forward osmosis membrane assembly, and aeration tube connects gas recycle pump by gas tube, and gas recycle pump connects anaerobic reactor casing upper space, described sludge gas collecting device also connects anaerobic reactor casing upper space.
As further improvement, described sludge gas collecting device comprises water leg, gas-collecting pipe and airway, and airway connects anaerobic reactor casing upper space, and gas-collecting pipe is arranged in water leg, the airway the other end is provided with U-shaped head, and the end of U-shaped head stretches in gas-collecting pipe.
As further improvement, this reactor also comprises automatic control system, automatic control system comprises level sensor and two-position controller, and level sensor is separately positioned in inlet chest and anaerobic reactor casing, and two-position controller connects intake pump, gas recycle pump and concentrate pump.
As further improvement, described anaerobic reactor casing top is provided with grid, and inlet chest is connected to the top of grid by intake pump.
As further improvement, the membrane material of described forward osmosis membrane assembly is cellulose acetate, and membrane module form is flat sheet membrane.
As further improvement, draw liquid is inorganic salt solution or saccharide solution.As preferred again, draw liquid is the sodium chloride solution of 20-50 g/L.
As further improvement, described inlet chest influent quality parameter is: 200-800 mg/L COD, 1-60 mg/L ammonia nitrogen, 0.5-10 mg/L phosphoric acid salt, pH=6.5-8.0.
As further improvement, this reactor operation parameter is: temperature=20-60 DEG C, and HRT=5-25 h, SRT=60-300 d, membrane flux is 5-20 L/m
2h.
The present invention compared with prior art, has following characteristics:
1. can produce the energy.The present invention has good conversion capability for organism in municipal wastewater, most of organism can be converted into the energy of methane form, and apparent factor of created gase is 0.24 LCH
4/ g COD.Calculating shows, the value of the energy that produces is that 1.5 times of its operation energy consumption expense are above [referring to applicant's paper Lin Hongjun, Chen Jianrong, Wang Fangyuan, Ding Linxian, Hong Huachang, Desalination, 2011,280:120-126.].Illustrate that adopting the present invention to process municipal wastewater not only can offset working cost, and can additionally make money.
2. effluent quality is good.The present invention adopts forward osmosis membrane process to replace ultrafiltration and the microfiltration membrane process in traditional MBR technology, and because forward osmosis membrane almost can be held back the pollutent including ion completely, thereby effluent quality is high, can reach reuse standard.Tradition Anaerobic Microbiological Treatment Technology can effectively be removed organism, but the removal effect to nitrogen, Phosphorus pollutent is poor, the present invention introduces forward osmosis membrane process in anaerobic biological treatment, thereby in retaining anaerobic treatment advantage, can effectively overcome again the shortcoming of anaerobic treatment.
3. film pollution level is light, and running cost is low.Because forward osmosis membrane process relies on the spontaneous membrane sepn of realizing of permeable pressure head drawing between liquid and stock liquid, and do not need impressed pressure as motivating force, thereby membrane sepn process pollution level is light, operation energy consumption is lower.Simultaneously lighter film pollutes the expense that film cleans is reduced, and extend the work-ing life of film.The present invention adopts the configuration of immersion in addition, and operation energy consumption significantly reduces than external placed type configuration.Running cost when these features make to adopt the present invention to dispose of sewage is lower.
4. sludge yield is low.The observed growth yield of apparatus of the present invention during for the treatment of municipal wastewater is only 0.032 kg MLSS/kgCOD left and right, the observed growth yield when activated sludge process that tradition is aerobic and aerobic membrane bioreactor are processed municipal wastewater is between 0.35-0.45 kg MLSS/kg COD, and both differ more than 10 times.In a lot of sewage works, the expense of only processing excess sludge has just accounted between the 20-50% of all running costs.Visible the present invention has cost advantage during for the treatment of municipal wastewater.
5. organic loading is high, and floor space is little.Membrane Bio-reactor Technology realizes the holding back completely of mud by membrane module, realized separating completely of hydraulic detention time (HRT) and sludge retention time (SRT), thereby organic loading is very high.The present invention has this remarkable advantage.Simultaneously the present invention has higher integrated level, than the aerobic activated sludge process of tradition, under the condition of same treatment amount, its floor space only for the former 1/10 less than.
6. full automatic control.In the present invention, all electron devices all adopt the unified control of automaticallyprogrammed controller, and level of automation is high, and reliability is strong, has reduced human cost.
Brief description of the drawings
Fig. 1 is one-piece construction schematic diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is made a detailed explanation.
A kind of immersion type anaerobic forward osmosis membrane bioreactor as shown in Figure 1, this reactor comprises anaerobic reactor casing 10, forward osmosis membrane separation system, sludge gas collecting device and the biogas recirculation aerating system of inlet chest 1, sealing.Described anaerobic reactor casing 10 tops are provided with grid 9, and inlet chest 1 connects the top of water inlet pipe 5 to grid 9 by intake pump 4.Described forward osmosis membrane separation system comprises forward osmosis membrane assembly 12, draws liquid storage tank 18, reverse osmosis concentration assembly 21 and concentrate pump 22,12 submergences of forward osmosis membrane assembly are arranged in anaerobic reactor casing 10, the top of forward osmosis membrane assembly 12 is connected with draws liquid pipeline 14, draw liquid pipeline 14 and connect the described liquid storage tank 18 that draws, the bottom of forward osmosis membrane assembly 12 is connected with outlet pipeline, and outlet pipeline connects described reverse osmosis concentration assembly 21 by concentrate pump 22.Reverse osmosis concentration assembly 21 tops connect the described liquid storage tank 18 that draws by concentrated pipeline 20 is set, and are provided with rising pipe 22 on reverse osmosis concentration assembly 21.Described biogas recirculation aerating system comprises aeration tube 13, gas recycle pump 15 and gas tube 16, aeration tube 13 is arranged on the bottom of forward osmosis membrane assembly 12, aeration tube 13 connects gas recycle pump 15 by gas tube 16, and gas recycle pump 15 connects anaerobic reactor casing 10 upper spaces.Described sludge gas collecting device also connects anaerobic reactor casing 10 upper spaces, described sludge gas collecting device comprises water leg 8, gas-collecting pipe 7 and airway 6, airway 6 connects anaerobic reactor casing 10 upper spaces, gas-collecting pipe 7 is arranged in water leg 8, airway 6 the other ends are provided with U-shaped head, and the end of U-shaped head stretches in gas-collecting pipe 7.
As shown in Figure 1, this reactor also comprises automatic control system, automatic control system comprises level sensor 2,11 and two-position controller 3, level sensor 2,11 is separately positioned in inlet chest 1 and anaerobic reactor casing 10, and two-position controller 3 connects intake pump 4, gas recycle pump 15 and concentrate pump 22.
The present invention adopts forward osmosis membrane separation system to separate the replacement granular sludge of traditional anaerobic process or the mud-water separation mode of apposition growth; and forward osmosis membrane assembly 12 is directly immersed in the anaerobic sludge mixed solution 17 in reactor casing; adopt recycled biogas to carry out aeration to membrane module, this is core content of the present invention simultaneously.
The membrane material of forward osmosis membrane assembly 12 of the present invention is cellulose acetate, and membrane module form is flat sheet membrane.Described draw liquid is inorganic salt solution or saccharide solution, as the sodium chloride solution of 20-50 g/L.
The applicable influent quality parameter of the present invention is: 200-800 mg/L COD, 1-60 mg/L ammonia nitrogen, 0.5-10 mg/L phosphoric acid salt, pH=6.5-8.0.
The applicable operation parameter of the present invention is: temperature=20-60 DEG C, and HRT=5-25 h, SRT=60-300 d, membrane flux is 5-20 L/m
2h.
application Example 1
Adopt the present invention to process certain real life sewage.After sludge seeding and domestication, (seed sludge is the mud of processing in the UASB of high concentrated organic wastewater, domestication is 30 d), flow condition is as follows: COD=413 ± 58 mg/L, TSS=267 ± 27 mg/L, ammonia nitrogen=30.2 ± 9.4 mg/L, total phosphorus=4.1 ± 0.6 mg/L, pH=7.4 ± 0.4.Setting operation condition is as follows: HRT=6 h, SRT=220 d, temperature=30 ± 3 DEG C, membrane flux=12 L/m
2h, MLSS=8-12 g/L.Continuously operation 6 months, effluent COD concentration is lower than 12 mg/L during this time, clearance >97%.Ammonia nitrogen concentration is lower than 10 mg/L, the clearance of corresponding 70% left and right.Total tp removal rate > 80%.SS does not detect.Effluent quality is good, reaches the standard-required of " urban sewage reutilization city miscellaneous water water quality " (GB/T 18920-2002).Align during this time permeable membrane element 12 and clean, membrane module is stable.Observed growth yield is only 0.032 kg MLSS/kgCOD, and apparent factor of created gase is 0.24 LCH
4/ g COD.
application Example 2
Adopt the present invention to process certain paper waste.Seed sludge is the mud of processing in the UASB of high concentrated organic wastewater, and domestication is 60 d.After having tamed, move continuously reactor 5 months, the influent COD of run duration is 2800 mg/L left and right, pH=7.0 ± 0.2.Operational condition is as follows: HRT=23 h, SRT=280 d, temperature=37 ± 2 DEG C, membrane flux=6-8 L/m
2h, MLSS=12-15 g/L.Between continuing phase, effluent COD concentration is lower than 25 mg/L, clearance >99%.SS does not detect.Effluent quality is good, reaches the standard-required of " urban sewage reutilization city miscellaneous water water quality " (GB/T 18920-2002).Apparent factor of created gase is 0.35 LCH
4/ g.Align during this time permeable membrane element 12 and clean, membrane module is stable.
As known from the above examples, the present invention has advantages of that effluent quality is good, produce the energy, sludge yield is low and film pollution level is light.
Claims (9)
1. an immersion type anaerobic forward osmosis membrane bioreactor, is characterized in that: this reactor comprises anaerobic reactor casing (10), forward osmosis membrane separation system, sludge gas collecting device and the biogas recirculation aerating system of inlet chest (1), sealing, described inlet chest (1) connects described anaerobic reactor casing (10) by intake pump (4), described forward osmosis membrane separation system comprises forward osmosis membrane assembly (12), draw liquid storage tank (18), reverse osmosis concentration assembly (21) and concentrate pump (22), forward osmosis membrane assembly (12) submergence is arranged in anaerobic reactor casing (10), the top of forward osmosis membrane assembly (12) is connected with draws liquid pipeline (14), draw liquid pipeline (14) and connect the described liquid storage tank (18) that draws, the bottom of forward osmosis membrane assembly (12) is connected with outlet pipeline, outlet pipeline connects described reverse osmosis concentration assembly (21) by concentrate pump (22), reverse osmosis concentration assembly (21) top connects the described liquid storage tank (18) that draws by concentrated pipeline (20) is set, on reverse osmosis concentration assembly (21), be provided with rising pipe (23), described biogas recirculation aerating system comprises aeration tube (13), gas recycle pump (15) and connecting pipeline, aeration tube (13) is arranged on the bottom of forward osmosis membrane assembly (12), aeration tube (13) connects gas recycle pump (15) by connecting pipeline (16), and gas recycle pump (15) connects anaerobic reactor casing (10) upper space, described sludge gas collecting device also connects anaerobic reactor casing (10) upper space.
2. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, it is characterized in that: described sludge gas collecting device comprises water leg (8), gas-collecting pipe (7) and airway (6), airway (6) connects anaerobic reactor casing (10) upper space, gas-collecting pipe (7) is arranged in water leg (8), airway (6) the other end is provided with U-shaped head, and the end of U-shaped head stretches in gas-collecting pipe (7).
3. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, it is characterized in that: this reactor also comprises automatic control system, automatic control system comprises level sensor (2) and two-position controller (3), level sensor (2) is separately positioned in inlet chest (1) and anaerobic reactor casing (10), and two-position controller (3) connects intake pump (4), gas recycle pump (15) and concentrate pump (22).
4. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that: anaerobic reactor casing (10) top is provided with grid (9), and inlet chest (1) is connected to the top of grid (9) by intake pump (4).
5. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that: the membrane material of forward osmosis membrane assembly (12) is cellulose acetate, membrane module form is flat sheet membrane.
6. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that: draw liquid is inorganic salt solution or saccharide solution.
7. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that: draw liquid is the sodium chloride solution of 20-50 g/L.
8. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that inlet chest (1) influent quality parameter is: 200-800 mg/L COD, 1-60 mg/L ammonia nitrogen, 0.5-10 mg/L phosphoric acid salt, pH=6.5-8.0.
9. a kind of immersion type anaerobic forward osmosis membrane bioreactor according to claim 1, is characterized in that this reactor operation parameter is: temperature=20-60 DEG C, and HRT=5-25 h, SRT=60-300 d, membrane flux is 5-20 L/m
2h.
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104860394A (en) * | 2015-05-15 | 2015-08-26 | 刘婷 | Oxygen-enriched aeration system |
| CN105481180A (en) * | 2015-12-28 | 2016-04-13 | 清华大学 | Sewage treatment method and device |
| JP5998254B1 (en) * | 2015-06-19 | 2016-09-28 | 株式会社神鋼環境ソリューション | Digestion processing apparatus and digestion processing method |
| CN106336253A (en) * | 2016-08-16 | 2017-01-18 | 宁夏顺宝现代农业股份有限公司 | Production process for producing organic fertilizer through concentrating biogas slurry by using multistage membrane separation technology |
| CN107089725A (en) * | 2017-04-28 | 2017-08-25 | 河海大学 | A kind of forward osmosis membrane magnetic anaerobic biological reactor for wastewater treatment |
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| CN109294879A (en) * | 2018-09-29 | 2019-02-01 | 南京和润隆环保科技有限公司 | A kind of plug-flow reactor founding device |
| CN109867414A (en) * | 2019-03-20 | 2019-06-11 | 北京科技大学 | Using the integrated apparatus in Dynamic Membrane anaerobism MBR- positive infiltration technology processing mankind Heisui River |
| EP3426607A4 (en) * | 2016-03-09 | 2019-10-16 | Enrgistream Pty Ltd | Process and system for treating waste water and generating power |
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| CN113651420A (en) * | 2021-08-16 | 2021-11-16 | 北控水务(中国)投资有限公司 | Anaerobic self-driven membrane reactor suitable for high COD wastewater treatment and regeneration |
| WO2023019806A1 (en) * | 2021-08-16 | 2023-02-23 | 北控水务(中国)投资有限公司 | Anaerobic self-driven membrane reactor suitable for high cod wastewater treatment and regeneration |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786768A (en) * | 2010-03-09 | 2010-07-28 | 天津膜天膜工程技术有限公司 | Forward osmosis membrane bioreactor |
| CN102276113A (en) * | 2011-07-08 | 2011-12-14 | 国家***天津海水淡化与综合利用研究所 | Combined fresh water increment method of forward osmosis membrane bioreactor / reverse osmosis |
| CN103332835A (en) * | 2013-07-29 | 2013-10-02 | 哈尔滨工业大学 | Anaerobic membrane bioreactor and forward-osmosis reverse-osmosis combined sewage treatment system |
| JP2014061487A (en) * | 2012-09-21 | 2014-04-10 | Kubota Corp | Water treatment method and water treatment system |
-
2014
- 2014-05-13 CN CN201410199932.3A patent/CN104016477A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786768A (en) * | 2010-03-09 | 2010-07-28 | 天津膜天膜工程技术有限公司 | Forward osmosis membrane bioreactor |
| CN102276113A (en) * | 2011-07-08 | 2011-12-14 | 国家***天津海水淡化与综合利用研究所 | Combined fresh water increment method of forward osmosis membrane bioreactor / reverse osmosis |
| JP2014061487A (en) * | 2012-09-21 | 2014-04-10 | Kubota Corp | Water treatment method and water treatment system |
| CN103332835A (en) * | 2013-07-29 | 2013-10-02 | 哈尔滨工业大学 | Anaerobic membrane bioreactor and forward-osmosis reverse-osmosis combined sewage treatment system |
Non-Patent Citations (4)
| Title |
|---|
| ANDREA ACHILLI ET AL: "The forward osmosis membrane bioreactor: A low fouling alternative to MBR processes", 《DESALINATION》, vol. 239, no. 13, 30 April 2009 (2009-04-30) * |
| 卞文娟等: "《环境工程实验》", 31 December 2011, article "水处理实验", pages: 125 * |
| 林红军等: "厌氧膜生物反应器的研究和应用进展", 《净水技术》, vol. 26, no. 6, 25 December 2007 (2007-12-25) * |
| 林红军等: "平板式MBR处理城市生活污水的性能与经济性分析", 《中国给水排水》, vol. 23, no. 19, 31 October 2007 (2007-10-31), pages 48 - 51 * |
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