CN101723564A - 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
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- 238000000926 separation method Methods 0.000 title claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 31
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- 230000009615 deamination Effects 0.000 claims abstract description 5
- 238000006481 deamination reaction Methods 0.000 claims abstract description 5
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- 238000001728 nano-filtration Methods 0.000 claims description 8
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- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 4
- 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
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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 generator 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 at 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, the more impossible stable first discharge standard that reaches.
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 based on simple biochemistry, not up to standard substantially, 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 class 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 class engineering accounts for more than 20%.
The core of above Technology all is the biochemical processing of originates from life sewage disposal, and in fact this is a detour of abroad just passing by before 20 years.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, just walked out based on reverse osmosis technology, high-efficient biological reactor is in conjunction with the technological line of reverse osmosis.
From abroad in recent ten years leachate treatment technology develop, simple biochemical process is handled the technology of percolate and is eliminated gradually, the substitute is based on the membrane treatment process of reverse osmosis and efficiently biochemical treatment in conjunction with the modern technique of 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 engineering of external advanced person's reverse-osmosis treated percolate technology 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, as 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 reverse osmosis 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 energy continuous operation, and the mechanization degree height is easy to management, and the unstable of water quality is less to the influence of film treatment effect.But this technology delays to be used to actual engineering at home, trace it to its cause to be mould material cost height, 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
Purpose of the present invention is intended to overcome the deficiencies in the prior art, and a kind of biochemistry, membrane separation process garbage leachate treatment process of efficient economy 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 magnesium oxide 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 circulating anaerobic producer stop 8～9 hours is gone in the settling tank water outlet of step 3;
Five, the liquid that is come out by the internal circulating anaerobic producer in the step 4 pumps into inner loop three phase fluidized bed reactor through Buffer Pool and stopped filling ceramsite carrier in the fluidized-bed 2～3 hours;
Six, the liquid of step 5 enter membrane bioreactor stop carried out in 6～7 hours filter membrane handle produce in water; 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 nanofiltration membrane produces can enter 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 reverse osmosis water outlet qualified discharge;
Nine, the dope that produced of step 8 reverse osmosis 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 liquor of step 10 passes back into the reaction tank of step 1.
Adding magnesium oxide 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.Step 4 internal circulating anaerobic producer 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 circulating anaerobic producer, inner loop three phase fluidized bed reactor, membrane bioreactor, smart filter, nanofiltration and reverse osmosis unit can be selected existing installation for use.
Technology of the present 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, nanofiltration membrane and reverse osmosis membrane; Compared with the prior art 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 the drawings and specific embodiments the present invention is done further to specify, 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, adjust pH value to 11～11.5 with powdery magnesium oxide, 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 the more even filling ball surface dirt that prevents simultaneously of cloth liquid.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 by blower fan, is external phase from bottom to top with the water counter current contact.Filler is the polypropylene 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 the internal circulating anaerobic producer.This device produces circulation by the lifting of biogas, improves treatment effect thereby percolate and anerobe are fully contacted.And after Buffer Pool pumps into inner loop three phase fluidized bed reactor, filling ceramsite carrier in the fluidized-bed, making into, water fully contacts with microorganism, microorganism adhering forms microbial film at carrier surface, make active sludge that good settling property be arranged, be difficult for by the water outlet band from reactor and at system's internal recycle, the top of cylindrical shell is the cap shape, the mixed solution of gas, water and mud enters the three-phase separation area of reactor upper cap shape to be separated; Gas leaves reactor from above, primary water flows out from water outlet, and carrier and part mud turn back to reactor bottom 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 by the immersion filter membrane component and extracts out; Microorganism in bio-reactor, is made reactor that huge biomass be 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 liquor 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, sodium filtering technology.Smart filter is that the pretreatment technology of follow-up sodium filter, reverse osmosis can be guaranteed the normal operation of the influent quality and the follow-up reverse osmosis high-pressure intake pump of sodium filter device, plays the effect of protection sodium filter membrane and reverse osmosis membrane simultaneously.It is in order to remove heavy metal that the sodium filter is set.Generally in the water outlet of accurate filter, sodium filter, need to add Scale inhibitors, described Scale inhibitors kind is a lot, commonly used have the U.S. to produce PTPO100 octuple concentrated solution or U.S. product MDC220 stoste, 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 sodium filter, reverse osmosis work termination, and the water after sodium filter, the reverse-osmosis treated can be better than emission standard.Owing to adopted internal circulating anaerobic producer, inner loop three phase fluidized bed reactor, membrane biological reactor process efficiently before the sodium filter, made the treatment solution water outlet be better than traditional biological method technology.Thereby alleviated sodium filter, reverse osmosis load, improved the working life of sodium filter membrane and reverse osmosis membrane.The discharging dope of reverse osmosis is dropped to below 1.5%, only be 7.5% of ultrafiltration, two-pass reverse osmosis technology dope quantity discharged, and available self-produced biogas need not used the external energy by 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 reverse osmosis of this technology can be omitted, and the sodium filtrate gets final product qualified discharge.
Through experiment relatively, adopt two-pass reverse osmosis treatment process, treatment scale 500m as 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 rate of recovery 80% has 20% reverse osmosis 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 as 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 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 is a vertical structure, highly be generally 14～25m, so floor space is little, collecting methane is also convenient simultaneously.
2, organic loading height, 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, the lifting by biogas produces circulation, does not need external impetus to mix and make mud to reflux, and saves power consumption.
Energy-efficient treating refuse percolate technology of the present invention has been owing to adopted the inner loop three phase fluidized bed reactor reactor, 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 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 is compared with other aerobic treatment process, and following characteristics is arranged:
1, height is large 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 influent COD; Sludge reflux is finished in same reactor, does not need additionaling power.
4, fluidizing performance is good, and the most of carrier of reactor participates in circulating, and does not therefore have carrier lamination in the bed. The suffered friction in bed of each carrier, shear basic identically, the carrier fluidisation has good uniformity, and this provides condition for uniform biofilm formation.
5, the rate of transform of oxygen is high. Because reactor can be carried some tiny bubbles secretly at the sectional area of central tube aeration sectional area (traditional fluid bed), the simultaneously a large amount of liquid-circulatings less than at whole bed aeration the time, solution-air is prolonged time of contact, thereby improved the transfer efficiency of oxygen. Actual measurement shows that air utilization ratio can reach 30%～50%, and dynamic efficiency can reach 2KgO2/(KW.h)～5KgO
2(KW.h)。
6, the carrier current vector is few, does not need special demoulding equipment. Because the shearing that carrier is subject in the whole reactor and the basically uniformity that rubs, therefore can not occur thickening because of biomembrane, carrier lighten and in bed lamination (this is the fundamemtal phenomena of traditional fluid bed), so can be in the situation that does not increase demoulding equipment, the film that guarantees bio-carrier in the reactor can excessive increase, simultaneously again can loss carrier, so just greatly simplified the original required auxiliary equipment of fluidized bed processing sewage.
7, biomass is high in the fluid bed, reactor volume is little, and biomass generally can reach 20g/L～40g/L, is 5～8 times of traditional activated sludge process. Because activated sludge circulates in reactor, 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 processing the compound of nitrogen-containing compound and other difficult degradation.
8, because the inner loop three phase fluidized bed reactor reactor has huge biomass, and be typical complete mixed bioreactor. Therefore impact load (hydraulic loading shock and Organic loading shock) resistivity is strong, can return to very soon the state before impacting, and treatment effeciency is high.
Internal-circulation anaerobic reactor, its sludge yield of inner loop three phase fluidized bed reactor technique only are 10% of traditional anaerobic-aerobic method, and floor space only is 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 magnesium oxide 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 circulating anaerobic producer stop 8～9 hours is gone in the settling tank water outlet of step 3;
Five, the liquid that is come out by the internal circulating anaerobic producer in the step 4 pumps into inner loop three phase fluidized bed reactor through Buffer Pool and stopped filling ceramsite carrier in the fluidized-bed 2～3 hours;
Six, the liquid of step 5 enter membrane bioreactor stop carried out in 6～7 hours filter membrane handle produce in water; 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 nanofiltration membrane produces can enter 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 reverse osmosis water outlet qualified discharge;
Nine, the dope that produced of step 8 reverse osmosis 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 liquor of step 10 passes back into the reaction tank of step 1.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN111701342A (en) * | 2020-06-18 | 2020-09-25 | 湖南恒凯环保科技投资有限公司 | Underground water organic pollution extraction treatment device and process |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2054823C (en) * | 1990-11-02 | 1996-09-24 | Denys Wickens | Wastewater treatment |
| CN1259260C (en) * | 2005-01-14 | 2006-06-14 | 清华大学 | Infiltration liquid treatment method in domestic refuse burying field |
| CN100575282C (en) * | 2005-12-06 | 2009-12-30 | 昆明市环境科学研究所 | Refuse leachate treatment technology |
| CN101250006B (en) * | 2007-12-18 | 2011-06-08 | 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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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN111701342A (en) * | 2020-06-18 | 2020-09-25 | 湖南恒凯环保科技投资有限公司 | Underground water organic pollution extraction treatment device and process |
| 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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| CN101723564B (en) | 2012-07-25 |
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