CN101723564B - Garbage percolate treating process by biochemical and membrane separation - Google Patents
Garbage percolate treating process by biochemical and membrane separation Download PDFInfo
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- 239000012528 membrane Substances 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 13
- 238000000926 separation method Methods 0.000 title claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000010802 sludge Substances 0.000 claims abstract description 24
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 18
- 239000002455 scale inhibitor Substances 0.000 claims abstract description 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 230000009615 deamination Effects 0.000 claims abstract description 5
- 238000006481 deamination reaction Methods 0.000 claims abstract description 5
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 4
- 239000006228 supernatant Substances 0.000 claims abstract description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 20
- 238000001728 nano-filtration Methods 0.000 claims description 15
- 238000012545 processing Methods 0.000 claims description 15
- 239000002562 thickening agent Substances 0.000 claims description 11
- 229910021529 ammonia Inorganic materials 0.000 claims description 10
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- 229910001385 heavy metal Inorganic materials 0.000 claims description 3
- GVALZJMUIHGIMD-UHFFFAOYSA-H magnesium phosphate Chemical compound [Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O GVALZJMUIHGIMD-UHFFFAOYSA-H 0.000 claims description 3
- 229910000400 magnesium phosphate tribasic Inorganic materials 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000010865 sewage Substances 0.000 abstract description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 abstract 2
- 239000000969 carrier Substances 0.000 abstract 1
- 238000001914 filtration Methods 0.000 abstract 1
- 239000012530 fluid Substances 0.000 abstract 1
- 239000000395 magnesium oxide Substances 0.000 abstract 1
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 24
- 230000000694 effects Effects 0.000 description 7
- 208000028659 discharge Diseases 0.000 description 5
- 230000003851 biochemical process Effects 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000005273 aeration Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
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- 230000015556 catabolic process Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
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- -1 nitrogenous compound Chemical class 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
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- Y02W10/12—
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the field of sewage treatment, in particular to a treating process for high-concentration garbage percolate. The process comprises the following steps of: 1. adding magnesia into garbage percolate to be treated in a reaction tank, and adjusting the pH value to 11-11.5; 2. deamination treatment; 3. adjusting the PH value to 8-8.5 by using phosphoric acid; 4. delivering into an internal circulating anaerobic reactor to dwell for 8-9 hours; 5. delivering into an internal circulating three-phase biological fluidized bed to dwell for 2-3 hours, and filling ceramsite carriers into the fluidized bed; 6. delivering into a membrane bioreactor to dwell for 6-7 hours, treating by a filter membrane to generate neutralized water; 7. delivering the neutralized water into a precision filter, adding commercial scale inhibitor to the discharged water to the extent that the subsequent filter membrane does not form scale, and then delivering into a nanometer filtering treating system; 8. supplementing commercial scale inhibitor into the discharged water to the extent that the subsequent filter membrane does not form scale before delivering the discharged water into a reverse osmosis device, and exhausting reverse osmosis discharged water after achieving standard; 9. performing burning treatment on concentrated liquor produced by reverse osmosis; 10. delivering the produced sludge and concentrated liquor to a sludge concentrated tank, and then returning to a landfill; and 11. enabling the supernatant fluid of the sludge concentrated tank in the step 10 to flow back into the reaction tank in step 1.
Description
Technical field
The present invention relates to sewage treatment area, particularly be directed against the treatment process of high-concentration garbage percolate.
Background technology
Organic pollutant is dense in the percolate; Accomplish qualified discharge; The clearance of chemical oxygen demand will guarantee that more than 99% traditional biochemical conventional treatment process can't reach at all, and it is few that the percolate in present domestic each refuse tip is handled the running example that can reach secondary discharge standard.The pollution that will thoroughly solve percolate is a technical problem, also is a social concern, is perplexing environmental sanitation and environmental administration always, and many for many years people did unremitting effort, but produced little effect.Percolate treatment project by secondary and three grades of emission standard design and operations does not reach design objective mostly, more can not stablize to reach first discharge standard.
It is three kinds that present China leachate treatment technology roughly has following: the one, continue to use the traditional life technology of waste water control, and be main with simple biochemistry, not up to standard basically, this engineering accounts for more than 60% of percolate engineering total.The 2nd, many in recent years scientific research institutions consider the characteristics of percolate, constantly explore some new technologies, have improved some old ways, integrated some novel procesies, and be applied to actual engineering, but effect is unsatisfactory, and this type engineering accounts for about 10%.The 3rd, some landfill yards are suffered from does not have good treatment technology, and clear-cut self-degradation simply tackles, and this type engineering accounts for more than 20%.
The core of above Technology all is the biochemical processing of originates from life WWT, and in fact this is a detour of abroad before 20 years, just passing by.Western developed country is paid close attention to and carried out the percolate processing on a large scale is in the 1950's; Basically be in helpless and failure, to explore; Handle along with membrane technology is applied to percolate up to the eighties; It is main just having walked out with reverse osmosis technology, and high-efficient biological reactor combines the technological line of r-o-.
From abroad in recent ten years leachate treatment technology develop, the technology that simple biochemical process is handled percolate is eliminated gradually, the substitute is with the r-o-is the modern technique that main membrane treatment process and efficient biochemical treatment combine embrane method.Since 2003; Along with country strengthens environmental protection, rubbish and percolate strength disposal; The long-living bridge in Chongqing, Beijing Nangong composting plant, Qingdao Xiao Jianxi and Guangzhou Xing Feng refuse landfill etc. are successively introduced the external advanced technological engineering of reverse-osmosis treated percolate and are built up in succession, make advanced in years the stepping a stage of percolate processing horizontal of China.
The problem that membrane separation technique exists:
Reverse osmosis process has high efficiency, modularity and is being easy to advantage such as automatically control because of it aspect the percolate processing; Use more and morely; But its following shortcoming also will draw attention: 1. the material of small molecular weight to hold back efficient also not fully up to expectations, like materials such as ammonia, micromolecular AOX; 2. but the organism of high density or inorganic sediment pollute film or easily in problems such as film surface scales; 3. because the very high energy consumption that causes of working pressure is very high; 4. the processing of r-o-dope has big difficulty, and general two-pass reverse osmosis total yield is 75%～80%, and the total flow rate of dope is 20%～25% of a treatment capacity, recharges in the landfill yard it inadvisable.Because the Pollutant levels of dope are very high, belong to dangerous rubbish.The at present employing evaporated and the exsiccant method more, but expense is very high.
The effect of membrane sepn pollutent is conspicuous, and the water outlet after separating can reach the corresponding emission standard of country, this method ability continuous operation, and mechanization degree is high, is easy to management, and the unstable of water quality is less to the influence of film treatment effect.But should technology delay at home to be used to actual engineering, tracing it to its cause is that the mould material cost is high, and film is when handling this contaminated more serious water body, and film is very easily contaminated, and difficult the cleaning is difficult to utilize once more.
What develop a kind of suitable national conditions is that main binding film is treated to auxilliary technology the raising that practical engineering application is worth is had far reaching significance with high-efficient biological reactor for this reason.
Summary of the invention
The object of the invention is intended to overcome the deficiency of prior art, and a kind of biochemistry, membrane separation process garbage leachate treatment process of highly economical is provided.
Biochemistry of the present invention, membrane separation process garbage leachate treatment process are made up of following steps:
One, percolate pending in the reaction tank is added Natural manganese dioxide and regulate pH value to 11～11.5;
Two, the treatment solution of step 1 is sent into Ammonia blowing-out tower, carries out deamination and handles;
Three, the liquid after the step 2 deamination is handled is again with phosphoric acid regulating ph value to 8～8.5; Water outlet is removed trimagnesium phosphate through settling tank;
Four, internal-circulation anaerobic reactor stop 8～9 hours is gone in the settling tank water outlet of step 3;
Five, the liquid that is come out by internal-circulation anaerobic reactor in the step 4 pumps into inner loop three phase fluidized bed reactor through Buffer Pool and stopped 2～3 hours, filling ceramsite carrier in the fluidized-bed;
Six, the water outlet of step 5 inner loop three phase fluidized bed reactor entering membrane bioreactor stops and carried out water in the filter membrane processing generation in 6～7 hours; The unnecessary mud of handling the back generation is regularly pumped into perpendicular heavy formula sludge thickener;
Seven, water is sent into accurate filter in the filter membrane of step 6, and water outlet adds commercially available Scale inhibitors, and add-on is with follow-up filter membrane non-scaling degree of being; Go into the nanofiltration treatment system then; The dope that nf membrane produces can get into perpendicular heavy formula sludge thickener because of not containing heavy metal;
Eight, the water outlet of step 7 nanofiltration replenishes before sending into reverse osmosis unit and adds commercially available Scale inhibitors, and add-on is with follow-up filter membrane non-scaling degree of being, but r-o-water outlet qualified discharge;
Nine, the dope that produced of step 8 r-o-passes through burning disposal;
Ten, return landfill yard after the dope of the mud of step 3, step 6 generation and step 7 generation goes into to erect heavy formula sludge thickener;
11, the sludge thickener supernatant of step 10 passes back into the reaction tank of step 1.
Adding Natural manganese dioxide in the step 1 mainly is to regulate pH value to 11～11.5, and the ammonium ion in the percolate is existed with the form of free ammonia.Ammonia blowing-out tower described in the step 2 is an existing installation, serves as preferred with rapid ball packing tower, and significant feature is that stripping is removed the free ammonia in the percolate.The step 4 internal-circulation anaerobic reactor in Yunnan-Guizhou and the areas to the south generally adopt the normal temperature anaerobism, can water inlet heating improve treatment effect to anaerobism with self-produced biogas to the north of Yunnan-Guizhou.Step 2, four, five, six, seven, eight described Ammonia blowing-out towers, internal-circulation anaerobic reactor, inner loop three phase fluidized bed reactor, membrane bioreactor, smart filter, nanofiltration and reverse osmosis unit can be selected existing installation for use.
Technology according to the invention makes construction costs and running cost greatly reduce owing to organically adopted materialization, biochemistry, membrane separation process treatment process; Improved the working life of membrane bioreactor filter membrane, nf membrane and reverse osmosis membrane; Compared with present technology institute of the present invention adopting process handles the load height; Easy and simple to handle, can realize automated operation.
Description of drawings
Fig. 1 is the process flow sheet of the embodiment of the invention.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is done specifying further, above-mentioned and otherwise advantage of the present invention will become apparent, but does not limit the present invention.
The described percolate of present embodiment is the Kunming percolate from garbage filling field; Percolate is from the equalizing tank gravity flow or pump into reaction tank; With powdery Natural manganese dioxide adjustment pH value to 11～11.5; Ammonium ion in the percolate is existed with the form of free ammonia, be lifted into rapid ball packing type Ammonia blowing-out tower with pump then, tubulent contact tower can make cloth liquid more evenly prevent the filling ball surface dirt simultaneously.The packing layer of device certain altitude in the tower.Percolate is film like along filling surface and flows downward from the cat head spray down.Air is gone into from the tower pucking through blower fan, is external phase from bottom to top with the water counter current contact.Filler is the Vestolen PP 7052 hollow ball.Remove treatment solution behind the ammonia with phosphoric acid regulating ph value to 8～8.5 to remedy the deficiency in percolate phosphorus source, go into settling tank then and separate trimagnesium phosphate, water outlet is from flowing into internal-circulation anaerobic reactor.This device leans on the lifting of biogas to produce circulation, improves treatment effect thereby percolate and anerobes are fully contacted.And after Buffer Pool pumps into inner loop three phase fluidized bed reactor; Filling ceramsite carrier in the fluidized-bed makes into that water fully contacts with mikrobe, and microorganism adhering forms microbial film at carrier surface; Make active sludge that good settling property arranged; Be difficult for by the water outlet band from reactor drum and at system's internal recycle, the top of cylindrical shell is the cap shape, the mixed solution of gas, water and mud gets into the three-phase separation area of reactor drum upper cap shape to be separated; Gas leaves reactor drum from above, primary water flows out from water outlet, and carrier turns back to reactor bottom with part mud through the negative area, and water outlet is carried out aerobic aeration and biological treatment from flowing into membrane bioreactor.Water after the processing filters the back by pump through the immersion filter membrane component and extracts out; Mikrobe in bio-reactor, is made reactor drum that huge living weight arranged by membrane retention, has eliminated sludge bulking problem in the traditional activated sludge process; Realize thoroughly separating of hydraulic detention time and mud mud age, can carry out nitrated, denitrification simultaneously; The unnecessary mud that produces regularly pumps into perpendicular heavy formula sludge thickener, and the sludge thickener supernatant passes back into the chopped-off head reaction tank.Membrane bioreactor has replaced second pond and tertiary treatment technology in traditional biochemical process, and institute goes out Zhong Shui and goes into smart filter, nanofiltration technique.The pretreatment technology that smart filter is follow-up nanofiltration, r-o-can be guaranteed the normal operation of the influent quality and the follow-up reverse osmosis high-pressure intake pump of nanofiltration device, plays the effect of protection nf membrane and reverse osmosis membrane simultaneously.It is in order to remove heavy metal that nanofiltration is set.The general adding Scale inhibitors that in the water outlet of accurate filter, nanofiltration, needs; Described Scale inhibitors kind is a lot; Commonly used have the U.S. to produce PTPO100 octuple liquid concentrator or U.S. product MDC220 stoste, and compound concentration is for containing stoste 10%～20% (weight percent, down together); Add-on is generally 1mg/L～3mg/L Scale inhibitors stoste with follow-up filter membrane non-scaling degree of being.When percolate CODcr＞15000mg/L; There is the COD of 400mg/L～500mg/L to remove in the percolate with biochemical process; Water outlet will reach the new demand of " city life garbage landfill pollution control criterion " GB16889-2008; It is necessary checking on and handle with nanofiltration, r-o-work termination, and the water after nanofiltration, the reverse-osmosis treated can be superior to emission standard.Owing to adopted internal-circulation anaerobic reactor, inner loop three phase fluidized bed reactor, membrane biological reactor process efficiently before the nanofiltration, made the treatment solution water outlet be superior to traditional biological method technology.Thereby nanofiltration, r-o-load have been alleviated, the working life of having improved nf membrane and reverse osmosis membrane.The discharging dope of r-o-is dropped to below 1.5%, be merely 7.5% of ultrafiltration, two-pass reverse osmosis technology dope quantity discharged, and available self-produced biogas need not used the external energy through the incinerator processing.The mud that technology produces returns the anaerobically fermenting that landfill yard helps rubbish behind perpendicular heavy formula sludge thickener.When percolate CODcr＜15000mg/L, the follow-up r-o-of this technology can be omitted, and the nanofiltration water outlet gets final product qualified discharge.
Through experiment relatively, adopt two-pass reverse osmosis treatment process, treatment scale 500m like the long-living bridge percolate in Chongqing treatment plant on the market
3/ d, about 3,700 ten thousand yuan of construction investment, theoretical treatment becomes 10 yuan/m of this newspaper
3, the actual motion cost is much higher, and the treatment solution recovery 80% has 20% r-o-dope can only store processing.Also useful traditional anaerobism, aerobic process are done the pre-treatment of reverse osmosis process on the market, because traditional anaerobism, aerobic treatment load is low, the residence time is long, and floor space is big, so construction investment is big.What adopt like Xinfeng, Guangzhou percolate treatment plant is the UASB+SBR+ ro treatment technology, treatment scale 500m
3/ d, about 6,000 ten thousand yuan of construction investment, the about 25 yuan/m of processing cost
3
Internal-circulation anaerobic reactor, inner loop three phase fluidized bed reactor reactor drum are at first by Dutch Paques B. V. Application and Development.Internal-circulation anaerobic reactor is to succeed in developing according to the principle of UASB.It is made up of mixing zone, sludge bulking bed, precision processing district and four parts of the recycle system.It has compared following characteristics with other anaerobic treatment process:
1, because of reactor drum is a vertical structure, highly be generally 14～25m, so floor space is little, collecting methane is also convenient simultaneously.
2, organic loading is high, and hydraulic detention time is short.The organic loading and the hydraulic detention time of it and other anaerobic treatment process relatively see the following form.
| Technology | Organic loading KgCOD/ (m 3·d) | Hydraulic detention time h |
| Common digester | 0.5～2 | ＞90 |
| The contact digester | 2～4 | 10～15 |
| Anaerobic filter | 3～10 | ＞20 |
| UASB | 10～30 | 1～12 |
| Internal-circulation anaerobic reactor | 18～70 | 2～6 |
3, excess sludge is few, is about 1% of water COD into, and dehydration easily.
4, lean on the lifting of biogas to produce circulation, do not need external impetus to mix and make mud to reflux, save power consumption.
Energy-efficient treating refuse percolate technology according to the invention has been owing to adopted the inner loop three phase fluidized bed reactor reactor drum, and when after the percolate anaerobic treatment during CODcr:1500mg/L, load can reach 10～15KgCOD/ (m
3D).Processing rate can reach more than 70%.The inner loop three phase fluidized bed reactor reactor drum succeed in developing the breakthrough that has realized equally quality and quantity in the aerobic biochemical process field.
The inner loop three phase fluidized bed reactor reactor drum is compared with other aerobic treatment process, and following characteristics are arranged:
1, height is big with the diameter ratio, so floor space is little.
2, hydraulic detention time is short, is generally 0.5～4h.
3, excess sludge is few, less than 5% of water inlet COD; Mud refluxes and in same reactor drum, accomplishes, and does not need additionaling power.
4, fluidizing performance is good, and the most of carrier of reactor drum participates in circulating, and does not therefore have carrier demixing phenomenon in the bed.The suffered friction in bed of each carrier, shear basic identically, the carrier fluidisation has good homogeneous property, and this forms the condition that provides for uniform microbial film.
5, the rate of transform of oxygen is high.Because reactor drum is carried some tiny bubbles secretly in sectional area (traditional fluidized-bed), the simultaneously a large amount of liquid circulation meetings less than at the whole bed aeration time of the sectional area of central tube aeration, solution-air is prolonged duration of contact, thereby improved the transfer efficiency of oxygen.Actual measurement shows that air utilization ratio can reach 30%～50%, and dynamicefficiency can reach 2KgO
2/ (KW.h)～5KgO
2(KW.h).
6, the carrier current vector is few, does not need special demoulding equipment.Because the shearing that carrier receives in the whole reactor and the uniformity basically that rubs; Therefore can not occur thickening because of microbial film; Carrier lighten and in bed demixing phenomenon (this is the fundamemtal phenomena of traditional fluidized-bed), so can be under the situation that does not increase demoulding equipment, the film that guarantees bio-carrier in the reactor drum can excessive increase; The carrier that can not run off has again simultaneously so just been simplified the original required utility appliance of fluidized bed processing sewage greatly.
7, living weight is high in the fluidized-bed, reactor volume is little, and living weight generally can reach 20g/L～40g/L, is 5～8 times of traditional activated sludge process.Because of active sludge at the reactor drum internal recycle, mud age very high (being generally 20d), sludge yield is low, and can produce the very slow nitrifier of some speeds of growth etc., so inner loop three phase fluidized bed reactor is suitable for handling the compound of nitrogenous compound and other difficult degradation.
8,, and be typical complete mixed bioreactor because the inner loop three phase fluidized bed reactor reactor drum has huge living weight.Therefore impact load (hydraulic load impacts and organic loading impacts) resistivity is strong, can return to the state before impacting very soon, and processing efficiency is high.
Internal-circulation anaerobic reactor, its sludge yield of inner loop three phase fluidized bed reactor technology are merely 10% of traditional anaerobic-aerobic method, and floor space is merely 20% of traditional anaerobic-aerobic method.
Claims (1)
1. a biochemistry, membrane separation process garbage leachate treatment process is characterized in that being made up of following steps:
One, percolate pending in the reaction tank is added Natural manganese dioxide and regulate pH value to 11～11.5;
Two, the treatment solution of step 1 is sent into Ammonia blowing-out tower, carries out deamination and handles;
Three, the liquid after the step 2 deamination is handled is again with phosphoric acid regulating ph value to 8～8.5; Water outlet is removed trimagnesium phosphate through settling tank;
Four, internal-circulation anaerobic reactor stop 8～9 hours is gone in the settling tank water outlet of step 3;
Five, the liquid that is come out by internal-circulation anaerobic reactor in the step 4 pumps into inner loop three phase fluidized bed reactor through Buffer Pool and stopped 2～3 hours, filling ceramsite carrier in the fluidized-bed;
Six, the water outlet of step 5 inner loop three phase fluidized bed reactor entering membrane bioreactor stops and carried out water in the filter membrane processing generation in 6～7 hours; The unnecessary mud of handling the back generation is regularly pumped into perpendicular heavy formula sludge thickener;
Seven, water is sent into accurate filter in the filter membrane of step 6, and water outlet adds commercially available Scale inhibitors, and add-on is with follow-up filter membrane non-scaling degree of being; Go into the nanofiltration treatment system then; The dope that nf membrane produces can get into perpendicular heavy formula sludge thickener because of not containing heavy metal;
Eight, the water outlet of step 7 nanofiltration replenishes before sending into reverse osmosis unit and adds commercially available Scale inhibitors, and add-on is with follow-up filter membrane non-scaling degree of being, but r-o-water outlet qualified discharge;
Nine, the dope that produced of step 8 r-o-passes through burning disposal;
Ten, return landfill yard after the dope of the mud of step 3, step 6 generation and step 7 generation goes into to erect heavy formula sludge thickener;
11, the sludge thickener supernatant of step 10 passes back into the reaction tank of step 1.
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| CN102336470A (en) * | 2011-08-29 | 2012-02-01 | 太平洋水处理工程有限公司 | Sludge circulation and jet flow aeration combination for garbage percolate treatment system |
| CN104860477A (en) * | 2015-05-20 | 2015-08-26 | 天紫环保投资控股有限公司 | Efficient sewage treatment and purification system realizing resource recovery of refuse |
| CN111701342B (en) * | 2020-06-18 | 2021-05-04 | 湖南恒凯环保科技投资有限公司 | Underground water organic pollution extraction treatment device and process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0486199A1 (en) * | 1990-11-02 | 1992-05-20 | The Commonwealth Industrial Gases Limited | Wastewater treatment |
| CN1669958A (en) * | 2005-01-14 | 2005-09-21 | 清华大学 | Infiltration liquid treatment method in domestic refuse burying field |
| CN1978346A (en) * | 2005-12-06 | 2007-06-13 | 昆明市环境科学研究所 | Refuse leachate treatment technology |
| CN101250006A (en) * | 2007-12-18 | 2008-08-27 | 华南理工大学 | Aerobic-anaerobic cycling treatment fluidized bed reactor for landfill leachate |
| CN201136823Y (en) * | 2007-12-18 | 2008-10-22 | 华南理工大学 | Aerobic-anaerobic circulating treatment device for waste water |
-
2010
- 2010-01-22 CN CN2010100392033A patent/CN101723564B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0486199A1 (en) * | 1990-11-02 | 1992-05-20 | The Commonwealth Industrial Gases Limited | Wastewater treatment |
| CN1669958A (en) * | 2005-01-14 | 2005-09-21 | 清华大学 | Infiltration liquid treatment method in domestic refuse burying field |
| CN1978346A (en) * | 2005-12-06 | 2007-06-13 | 昆明市环境科学研究所 | Refuse leachate treatment technology |
| CN101250006A (en) * | 2007-12-18 | 2008-08-27 | 华南理工大学 | Aerobic-anaerobic cycling treatment fluidized bed reactor for landfill leachate |
| CN201136823Y (en) * | 2007-12-18 | 2008-10-22 | 华南理工大学 | Aerobic-anaerobic circulating treatment device for waste water |
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