CN103787547B - The treatment process of aging percolate - Google Patents

The treatment process of aging percolate Download PDF

Info

Publication number
CN103787547B
CN103787547B CN201310753307.4A CN201310753307A CN103787547B CN 103787547 B CN103787547 B CN 103787547B CN 201310753307 A CN201310753307 A CN 201310753307A CN 103787547 B CN103787547 B CN 103787547B
Authority
CN
China
Prior art keywords
level
treatment
percolate
zone
reaction tank
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201310753307.4A
Other languages
Chinese (zh)
Other versions
CN103787547A (en
Inventor
陈新芳
李泽清
唐艳萍
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GARDEN ENVIRONMENTAL PROFECTION
Original Assignee
GARDEN ENVIRONMENTAL PROFECTION
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by GARDEN ENVIRONMENTAL PROFECTION filed Critical GARDEN ENVIRONMENTAL PROFECTION
Priority to CN201310753307.4A priority Critical patent/CN103787547B/en
Publication of CN103787547A publication Critical patent/CN103787547A/en
Application granted granted Critical
Publication of CN103787547B publication Critical patent/CN103787547B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The invention provides the treatment process of aging percolate, it comprises following concrete operations: imported in equalizing tank by aging percolate and regulate, enter in hydrolysis acidification pool the acidifying that is hydrolyzed afterwards; Percolate after acidication flows into one-level A/O by hydrolysis acidification pool 2denitrification/oxidation of coal/nitration reaction is carried out in reaction tank; One-level A/O 2the water outlet of reaction tank enters in secondary A/O reaction tank carries out denitrification/nitration reaction with denitrogenation and decarburization further; The water outlet of secondary A/O reaction tank enters ultrafiltration system and carries out ultrafiltration; The permeate that ultrafiltration produces sends into nanofiltration system successively and reverse osmosis system carries out advanced treatment; The concentrated solution that nanofiltration system and reverse osmosis system produce all adopts concentrated solution system to process.The inventive method effectively can reduce the concentration of discharging water pollutant, to ensure the qualified discharge of water outlet.

Description

The treatment process of aging percolate
[technical field]
The present invention relates to the wastewater processing technology of field of Environment Protection, particularly relate to a kind for the treatment of process of aging percolate.
[background technology]
Along with the quickening of Chinese Urbanization paces, its municipal wastes also sharply increases accordingly.The percolate produced in garbage loading embeading process is one of waste water of more difficult high density in current water surrounding, to human body and environmental hazard very large.The percolate of refuse landfill is that constantly change occurs with its composition of landfill time lengthening, early stage percolate general landfill age is 3-5, wherein VFA (voltaile fatty acid) content is higher, approximately can account for more than 50% of TOC (total organic carbon), easily degrade by biology.BOD/COD (biodegradability) value is higher, and generally 0.4 ~ 0.8, ammonia nitrogen concentration is about 1000mg/L.Be called aging percolate more than the percolate in 3 ~ 5 years landfill ages, its biodegradability ratio is generally 0.1 ~ 0.2, and ammonia nitrogen concentration to extend with landfill and increase year by year age, and processing target is now based on the removal of ammonia nitrogen.Therefore, suitable measure need be adopted to improve its biodegradability, to improve the running environment of subsequent technique.
In Practical Project, aging percolate is compared with early stage method for treating garbage percolation liquid, and aging percolate has following difficult point:
1, ammonia-nitrogen content is high, and microbial nutrition element is lacked of proper care
Along with the prolongation of landfill time, in percolate, ammonia-nitrogen content increases gradually, and high ammonia nitrogen has very strong restraining effect to microbic activity, reduce the biological removal efficiency to high loading organic pollutant, thus it is up to standard to cause water outlet to be difficult to.Therefore require that the clearance of ammonia nitrogen and total nitrogen reaches more than 99%, suitable technique in technique, should be selected to improve the clearance of ammonia nitrogen and total nitrogen; For biological treatment, nutritive element ratio suitable in sewage is C: N: P=100: 5: 1, and aging percolate C/N is less than 10, C/P and is greater than 300, the nutritive element numerous imbalances of microorganism.
2, B/C is lower, and biodegradability is poor
The organic content of aging garbage filter percolate is not high, is degraded gradually along with the growth of landfill time, and remaining is not biodegradable soil ulmin.Select processing mode rationally and effectively, improve B/C and discharge than guarantee standard water discharge.
3, water quality and quantity change greatly, complicated component
The water quality characteristic of percolate along with the garbage loading embeading time limit, seasonal variation amplitude large, as carbon-nitrogen ratio, biodegradability, Pollutant levels etc. all change.Require that treatment facility has and regulate surplus, the impact load of resistance to waterpower, biological treatment system can adapt to the organic loading of constantly change, can adapt to the restraining effect of venomous injurant confrontation microorganism.
Technique for landfill leachate treatment is a lot, but because the concentration of percolate is high and complicated component, proposes special requirement to treatment process.Only rely on single treatment process to be difficult to reach strict water outlet require or the reprocessing requirement to resistates will be produced.From means and the degree of current China landfill leachate treatment, simple employing two-stage A/O+ ultrafiltration+nanofiltration/reverse osmosis process, is fundamentally difficult to solve the pollutent excessive problem such as water outlet total nitrogen and hardly degraded organic substance.
[summary of the invention]
Technical problem to be solved by this invention is the treatment process providing a kind of aging percolate, the B/C of aging percolate can be effectively regulated when to improve the nitrogen removal rate of biochemical system, and then reduce the concentration of discharging water pollutant, ensure the qualified discharge of water outlet.
The present invention solves the problems of the technologies described above by the following technical programs: a kind for the treatment of process of aging percolate, and this treatment process comprises following concrete operations:
(1) pre-treatment: aging percolate is imported the adjustment carrying out water quality, the water yield and B/C ratio in equalizing tank, and the hydraulic detention time in equalizing tank is 90 ~ 150d; The water outlet of equalizing tank enters in hydrolysis acidification pool the acidifying that is hydrolyzed, and hydraulic detention time is 6 ~ 8h;
(2) biochemical treatment: the percolate after acidication flows into one-level A/O by hydrolysis acidification pool 2denitrification/oxidation of coal/nitration reaction is carried out in reaction tank, to remove organism in percolate and ammonia nitrogen, and one-level A/O 2hydraulic detention time in reaction tank is 7d; One-level A/O 2the water outlet of reaction tank enters in secondary A/O reaction tank carries out denitrification/nitration reaction with denitrogenation and decarburization further, and the hydraulic detention time of secondary A/O reaction tank is 1.5d; The deep bed filter of water outlet first in ultrafiltration system of secondary A/O reaction tank filters, and is aspirated by ultrafiltration intake pump, and after fibre object such as interception large particulate matter and hair etc., carry out ultrafiltration, the sludge reflux that ultrafiltration produces is to hydrolysis acidification pool; And the mud that secondary A/O reaction tank produces is sent in sludge treating system, through precipitation and sludge condensation, the supernatant liquor obtained is back to hydrolysis acidification pool, and the thickened sludge obtained carries out drying and other treatment;
(3) advanced treatment: the permeate that ultrafiltration produces sends into nanofiltration system and reverse osmosis system carries out advanced treatment successively, removal can not biochemical substances and colourity further, makes water outlet reach emission standard; And the concentrated solution that nanofiltration system and reverse osmosis system produce all adopts concentrated solution system to process.
Further, the operating temperature of the whole process of described biochemical treatment controls as 30-37 DEG C.
Further, the upper strata of described hydrolysis acidification pool sets out mill weir, and the submersible agitator improving percolate biodegradability is established in bottom, and its power of agitator is 8-10W/m 3, and the liquid level lift velocity of hydrolysis acidification pool controls at 0.5-1.8m/h.
Further, described one-level A/O 2reaction tank comprises one-level denitrification zone, one-level oxidation of coal district and one-level nitrification zone successively; Percolate after acidication enters one-level denitrification zone by hydrolysis acidification pool and carries out denitrogenation, to improve percolate biodegradability, the water outlet gravity flow of one-level denitrification zone enters one-level oxidation of coal district to remove the organism such as CODcr in percolate, and the district's water outlet of one-level oxidation of coal enters one-level nitrification tank and carries out biological nitration effect removal ammonia nitrogen; Wherein, the one-level nitrification liquid partial reflux that one-level nitrification zone produces is to one-level denitrification zone, and quantity of reflux controls 8-10 times for flooding velocity; And the hydraulic detention time of each reaction zone is: one-level denitrification zone 2.0d, one-level oxidation of coal district 2.5d, one-level nitrification zone 2.5d.
Further, establish aerating system in described one-level oxidation of coal district, gas-water ratio controls at 300:1.
Further, a defoaming pump is established in outside, described one-level nitrification zone, and the import of defoaming pump is connected with one-level nitrification zone, and froth breaking pump outlet is connected with spiral spray device, carries out waterpower froth breaking; And establish aerating system in one-level nitrification zone, gas-water ratio controls at 200:1.
Further, described secondary A/O reaction tank comprises secondary denitrification zone and secondary nitrification zone; One-level A/O 2the water outlet of reaction tank enters secondary denitrification zone, secondary nitrification zone successively and processes, the secondary nitrification liquid that the hydraulic detention time of secondary denitrification zone is 0.75d, the hydraulic detention time of secondary denitrification zone is 0.75d, secondary nitrification zone produces is partly refluxed to secondary denitrification zone, and quantity of reflux controls 5-6 times for flooding velocity.
Further, establish aerating system in described secondary nitrification zone, gas-water ratio controls at 120:1.
Further, a cement baffle plate for being surrounded by the water inlet pipe mouth of ultrafiltration system being also set in described secondary nitrification zone, entering ultrafiltration system to avoid bubble.
Further, with the addition of medicament during the mud that described sludge treating system process secondary A/O reaction tank produces, this medicament is polyacrylamide.
Further, the ultrafiltration membrane pipe of described ultrafiltration system adopts external placed type tubular ultra-filtration membrane, film design flux 70L/m 2h, operating pressure 5-6bar.
Further, the nanofiltration membrane of described nanofiltration system adopts rolling polyamide composite film, film design flux 12L/m 2h, the design rate of recovery is 85%, operating pressure 5-8bar.
Further, the reverse osmosis membrane of described reverse osmosis system adopts rolling polyamide composite film, film design flux 10L/m 2h, the design rate of recovery is 75%, operating pressure 17-20bar.
The beneficial effect of the treatment process of aging percolate of the present invention is:
1, ammonia nitrogen and total nitrogen removal effect good;
2, can adapt to the fluctuation of Various Seasonal, different year percolate concentration, stronger capacity of resisting impact load, can ensure the stability of water outlet;
3, the usefulness of high loading, the process of high density percolate can be ensured;
4, the problem effectively avoiding percolate Middle nutrition out of proportion.
[accompanying drawing explanation]
The invention will be further described in conjunction with the embodiments with reference to the accompanying drawings.
Fig. 1 is the process flow sheet of the treatment process of aging percolate of the present invention.
[embodiment]
Refer to Fig. 1, the treatment process of aging percolate of the present invention comprises following concrete operations:
(1) pre-treatment: aging percolate is imported the adjustment carrying out water quality, the water yield and B/C ratio in equalizing tank, and the hydraulic detention time in equalizing tank is 90 ~ 150d; The water outlet of equalizing tank enters in hydrolysis acidification pool the acidifying that is hydrolyzed;
(2) biochemical treatment: the percolate after acidication flows into one-level A/O by hydrolysis acidification pool 2denitrification/oxidation of coal/nitration reaction is carried out in reaction tank, to remove organism in percolate and ammonia nitrogen, and one-level A/O 2hydraulic detention time in reaction tank is 7d; One-level A/O 2the water outlet of reaction tank enters in secondary A/O reaction tank carries out denitrification/nitration reaction with denitrogenation and decarburization further, and the hydraulic detention time of secondary A/O reaction tank is 1.5d; The deep bed filter of water outlet first in ultrafiltration system of secondary A/O reaction tank filters, and is aspirated by ultrafiltration intake pump, and after fibre object such as interception large particulate matter and hair etc., carry out ultrafiltration, the sludge reflux that ultrafiltration produces is to hydrolysis acidification pool; And the mud that secondary A/O reaction tank produces is sent in sludge treating system, through precipitation and sludge condensation, the supernatant liquor obtained is back to hydrolysis acidification pool, the thickened sludge obtained carries out drying and other treatment (with the addition of medicament during the mud that sludge treating system process secondary A/O reaction tank produces, this medicament is polypropylene amine);
(3) advanced treatment: the permeate that ultrafiltration produces sends into nanofiltration system and reverse osmosis system carries out advanced treatment successively, removal can not biochemical substances and colourity further, makes water outlet reach emission standard; And the concentrated solution that nanofiltration system and reverse osmosis system produce all adopts concentrated solution system to process.
It should be noted that, the operating temperature of the whole process of biochemical treatment controls as 30-37 DEG C; The upper strata of hydrolysis acidification pool sets out mill weir, and this effluent weir is for collecting the supernatant liquor on hydrolysis acidification pool top, and the submersible agitator improving percolate biodegradability is established in bottom, and its power of agitator is 8-10W/m 3, and the liquid level lift velocity of hydrolysis acidification pool controls at 0.5-1.8m/h.
One-level A/O 2reaction tank comprises one-level denitrification zone, one-level oxidation of coal district and one-level nitrification zone successively; Percolate after acidication enters one-level denitrification zone by hydrolysis acidification pool and carries out denitrogenation, to improve percolate biodegradability, the water outlet gravity flow of one-level denitrification zone enters one-level oxidation of coal district to remove the organism such as CODcr in percolate, and the district's water outlet of one-level oxidation of coal enters one-level nitrification tank and carries out biological nitration effect removal ammonia nitrogen; Wherein, the one-level nitrification liquid partial reflux that one-level nitrification zone produces is to one-level denitrification zone, and quantity of reflux controls 8-10 times for flooding velocity (referring to that equalizing tank enters the treatment capacity of hydrolysis acidification pool); And the hydraulic detention time of each reaction zone is: one-level denitrification zone 2.0d, one-level oxidation of coal district 2.5d, one-level nitrification zone 2.5d;
One-level oxidation of coal establishes aerating system in district, and the aerator top of aerating system is connected with gas, and its underpart is connected with a jet-loop pump, and gas-water ratio controls at 300:1; A defoaming pump is established in outside, one-level nitrification zone, the import of defoaming pump is connected with one-level nitrification zone, froth breaking pump outlet is connected with a spiral spray device, carry out waterpower froth breaking, and be provided with aerating system equally in one-level nitrification zone, the aerator top of this aerating system is connected with gas, and its underpart is connected with a jet-loop pump, and gas-water ratio controls at 200:1.
Secondary A/O reaction tank comprises secondary denitrification zone and secondary nitrification zone; One-level A/O 2the water outlet of reaction tank enters secondary denitrification zone, secondary nitrification zone successively and processes, the secondary nitrification liquid that the hydraulic detention time of secondary denitrification zone is 0.75d, the hydraulic detention time of secondary denitrification zone is 0.75d, secondary nitrification zone produces is partly refluxed to secondary denitrification zone, and quantity of reflux controls 5-6 times for flooding velocity (referring to that equalizing tank enters the treatment capacity of hydrolysis acidification pool).
Secondary establishes aerating system in nitrification zone, and the aerator top of aerating system is connected with gas, and its underpart is connected with a jet-loop pump, and gas-water ratio controls at 120:1; One cement baffle plate for being surrounded by the water inlet pipe mouth of ultrafiltration system being also set in secondary nitrification zone, entering ultrafiltration system to avoid bubble.
The ultrafiltration membrane pipe of ultrafiltration system adopts external placed type tubular ultra-filtration membrane (belonging to brackish water membrane element series), film design flux 70L/m 2h, operating pressure 5-6bar; The water outlet of secondary A/O reaction tank first through deep bed filter (filtering accuracy 40 order), after being aspirated by ultrafiltration intake pump, treat the interception fibre object such as large particulate matter and hair laggard enter ultrafiltration system; The permeate of ultrafiltration system enters ultrafiltration and produces pond, and the thickened sludge that ultrafiltration system produces then refluxes and enters hydrolysis acidification pool; And produce pond adjustment pH in ultrafiltration, prevent acid adding in the pipeline of nanofiltration system, basicity is too high can produce carbonic acid gas, causes damage to nanofiltration system pump; Ultrafiltration system configuration ultrafiltration cleaning system, comprises ultrafiltration cleaning water tank and flushing water pump.
The nanofiltration membrane of nanofiltration system adopts rolling polyamide composite film, film design flux 12L/m 2h, two-piece design, arrangement is than being 2:1, and front and back section uses different membrane modules, can ensure the membrane flux of two sections, front and back, makes product water comparatively balanced; The design rate of recovery of nanofiltration system is 85%, and operating pressure 5-8bar; The permeate of ultrafiltration system is promoted by the raw water pump of nanofiltration system, the deep bed filter entering nanofiltration system after Scale inhibitors fully mixes is added from pipeline, enter in nanofiltration system after being pressurizeed by the topping-up pump of nanofiltration system again, the permeate of nanofiltration system enters nanofiltration and produces pond, and nanofiltration dope is then outer drains into concentrated solution storage pond; Nanofiltration system 9 configures nanofiltration cleaning system, comprises nanofiltration cleaning water tank and flushing water pump.
The reverse osmosis membrane of reverse osmosis system adopts rolling polyamide composite film, film design flux 10L/m 2h, two sections of arrangements, arrangement, than being 2:1, has higher ratio of desalinization, and average ratio of desalinization, up to 99.8%, ensure that the high-quality of producing water; The design rate of recovery of reverse osmosis system is 75%, and operating pressure 17-20bar; The permeate of nanofiltration system is promoted by the raw water pump of reverse osmosis system, the deep bed filter entering reverse osmosis system after Scale inhibitors fully mixes is added from pipeline, enter in reverse osmosis system after being pressurizeed by the topping-up pump of reverse osmosis system again, the permeate of reverse osmosis system enters reverse osmosis produced pond, and reverse osmosis dope is then outer to be drained in concentrated solution storage pond or equalizing tank.Reverse osmosis system film design flux is 10LMH, adopts brackish water type desalination film.Reverse osmosis system 10 configures reverse osmosis cleaning system, comprises reverse osmosis cleaning water tank and flushing water pump.
During the inventive method process aging percolate: aging percolate first imports equalizing tank through special conduit, percolate general hydraulic detention time in equalizing tank is 90-150d, the B/C ratio in percolate is have adjusted, for follow-up biochemical treatment creates favourable condition while homogeneous even amount; The water outlet of equalizing tank promotes through lift pump the thickened sludge, the sludge treating system that produce with ultrafiltration system and dewaters after the supernatant liquor that produces mixes, and enter in hydrolysis acidification pool the acidifying that is hydrolyzed, the water outlet of hydrolysis acidification pool is flow automatically and entered one-level A/O 2reaction tank, first one-level denitrification zone is entered, in one-level denitrification zone, controlling one-level nitrification liquid quantity of reflux is under 8-10 operation scheme doubly, for denitrification flora provides suitable growth conditions, under the effect of denitrification flora, the one-level nitrification liquid of percolate and backflow carries out denitrification denitrogenation through being uniformly mixed, and the water outlet of one-level denitrification zone enters one-level oxidation of coal district, in one-level oxidation of coal district, remove the organism such as the CODcr in percolate, be beneficial to the carrying out of follow-up nitrifying process; The water outlet in one-level oxidation of coal district enters one-level nitrification zone, carries out biological nitration effect and removes ammonia nitrogen.One-level A/O 2after reaction tank water outlet mixes with the volume ratio of 1:4-5 with secondary nitrification liquid, (mixed solution total amount is that equalizing tank enters the 5-6 of the treatment capacity of hydrolysis acidification pool doubly) enters secondary A/O reaction tank, carry out further denitrogenation and decarburizating, to ensure the requirement of water outlet to total nitrogen and COD, one-level A/O 2the total hrt of reaction tank and secondary A/O reaction tank is 8.5d.The water outlet of secondary A/O reaction tank is with pump suction ultrafiltration system (employing tubular ultra-filtration membrane), carry out mud-water separation, the thickened sludge be retained down is back to hydrolysis acidification pool, because tubular ultra-filtration membrane has very high interception capacity, organism can be retained on the one hand, can retain active sludge on the other hand, make the sludge concentration in biochemical reaction tank reach 10-20g/L, therefore biochemical have higher organic matter removal ability and denitrification ability; The water outlet of secondary A/O reaction tank sends into nanofiltration system successively by high-pressure pump after uf processing and reverse osmosis system carries out advanced treatment, and removing further can not biochemical substances and colourity etc., last standard water discharge discharge.
To sum up, the present invention adopts the biochemical treatment process combined with film of strengthening, effectively have adjusted the B/C ratio of sewage, and by controlling the key index such as reflux ratio, hydraulic detention time of strengthening biochemical system inside, well can reduce the total nitrogen index of ultrafiltration system water outlet, namely ammonia nitrogen and total nitrogen removal effect good, and then extend the membrane element work-ing life of subsequent nano-filtration system and reverse osmosis system; Can adapt to the fluctuation of Various Seasonal, different year percolate concentration, stronger capacity of resisting impact load, can ensure the stability of water outlet; The usefulness of high loading, the process of high density percolate can be ensured; Effectively can avoid the problem that percolate Middle nutrition is out of proportion; Generally speaking, the present invention while meeting effluent quality requirement, can give play to the characteristic of low cost of biochemical treatment as far as possible, to obtain good economy and Social Ecology benefit.

Claims (13)

1. a treatment process for aging percolate, is characterized in that: this treatment process comprises following concrete operations:
(1) pre-treatment: aging percolate is imported the adjustment carrying out water quality, the water yield and B/C ratio in equalizing tank, and the hydraulic detention time in equalizing tank is 90 ~ 150d; The water outlet of equalizing tank enters in hydrolysis acidification pool the acidifying that is hydrolyzed, and hydraulic detention time is 6 ~ 8h;
(2) biochemical treatment: the percolate after acidication flows into one-level A/O by hydrolysis acidification pool 2denitrification/oxidation of coal/nitration reaction is carried out in reaction tank, to remove organism in percolate and ammonia nitrogen, and one-level A/O 2hydraulic detention time in reaction tank is 7d; One-level A/O 2the water outlet of reaction tank enters in secondary A/O reaction tank carries out denitrification/nitration reaction with denitrogenation and decarburization further, and the hydraulic detention time of secondary A/O reaction tank is 1.5d; The deep bed filter of water outlet first in ultrafiltration system of secondary A/O reaction tank filters, and aspirated by ultrafiltration intake pump, after interception large particulate matter and hair fiber thing, carry out ultrafiltration, the sludge reflux that ultrafiltration produces is to hydrolysis acidification pool; And the mud that secondary A/O reaction tank produces is sent in sludge treating system, through precipitation and sludge condensation, the supernatant liquor obtained is back to hydrolysis acidification pool, and the thickened sludge obtained carries out drying and other treatment;
(3) advanced treatment: the permeate that ultrafiltration produces sends into nanofiltration system and reverse osmosis system carries out advanced treatment successively, removal can not biochemical substances and colourity further, makes water outlet reach emission standard; And the concentrated solution that nanofiltration system and reverse osmosis system produce all adopts concentrated solution system to process.
2. the treatment process of aging percolate according to claim 1, is characterized in that: the operating temperature of the whole process of described biochemical treatment controls as 30-37 DEG C.
3. the treatment process of aging percolate according to claim 1, it is characterized in that: the upper strata of described hydrolysis acidification pool sets out mill weir, the submersible agitator improving percolate biodegradability is established in bottom, and its power of agitator is 8-10W/m 3, and the liquid level lift velocity of hydrolysis acidification pool controls at 0.5-1.8m/h.
4. the treatment process of aging percolate according to claim 1, is characterized in that: described one-level A/O 2reaction tank comprises one-level denitrification zone, one-level oxidation of coal district and one-level nitrification zone successively; Percolate after acidication enters one-level denitrification zone by hydrolysis acidification pool and carries out denitrogenation, to improve percolate biodegradability, the water outlet gravity flow of one-level denitrification zone enters one-level oxidation of coal district to remove the CODcr organism in percolate, and the district's water outlet of one-level oxidation of coal enters one-level nitrification tank and carries out biological nitration effect removal ammonia nitrogen; Wherein, the one-level nitrification liquid partial reflux that one-level nitrification zone produces is to one-level denitrification zone, and quantity of reflux controls 8-10 times for flooding velocity; And the hydraulic detention time of each reaction zone is: one-level denitrification zone 2.0d, one-level oxidation of coal district 2.5d, one-level nitrification zone 2.5d.
5. the treatment process of aging percolate according to claim 4, is characterized in that: establish aerating system in described one-level oxidation of coal district, gas-water ratio controls at 300:1.
6. the treatment process of aging percolate according to claim 4, is characterized in that: a defoaming pump is established in outside, described one-level nitrification zone, and the import of defoaming pump is connected with one-level nitrification zone, and froth breaking pump outlet is connected with spiral spray device, carries out waterpower froth breaking; And establish aerating system in one-level nitrification zone, gas-water ratio controls at 200:1.
7. the treatment process of aging percolate according to claim 1, is characterized in that: described secondary A/O reaction tank comprises secondary denitrification zone and secondary nitrification zone; One-level A/O 2the water outlet of reaction tank enters secondary denitrification zone, secondary nitrification zone successively and processes, the secondary nitrification liquid that the hydraulic detention time of secondary denitrification zone is 0.75d, the hydraulic detention time of secondary denitrification zone is 0.75d, secondary nitrification zone produces is partly refluxed to secondary denitrification zone, and quantity of reflux controls 5-6 times for flooding velocity.
8. the treatment process of aging percolate according to claim 7, is characterized in that: establish aerating system in described secondary nitrification zone, gas-water ratio controls at 120:1.
9. the treatment process of aging percolate according to claim 8, is characterized in that: also arranging a cement baffle plate for being surrounded by the water inlet pipe mouth of ultrafiltration system in described secondary nitrification zone, entering ultrafiltration system to avoid bubble.
10. the treatment process of aging percolate according to claim 1, is characterized in that: with the addition of medicament during the mud that described sludge treating system process secondary A/O reaction tank produces, this medicament is polyacrylamide.
The treatment process of 11. aging percolates according to claim 1, is characterized in that: the ultrafiltration membrane pipe of described ultrafiltration system adopts external placed type tubular ultra-filtration membrane, film design flux 70L/m 2h, operating pressure 5-6bar.
The treatment process of 12. aging percolates according to claim 1, is characterized in that: the nanofiltration membrane of described nanofiltration system adopts rolling polyamide composite film, film design flux 12L/m 2h, the design rate of recovery is 85%, operating pressure 5-8bar.
The treatment process of 13. aging percolates according to claim 1, is characterized in that: the reverse osmosis membrane of described reverse osmosis system adopts rolling polyamide composite film, film design flux 10L/m 2h, the design rate of recovery is 75%, operating pressure 17-20bar.
CN201310753307.4A 2013-12-31 2013-12-31 The treatment process of aging percolate Active CN103787547B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201310753307.4A CN103787547B (en) 2013-12-31 2013-12-31 The treatment process of aging percolate

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201310753307.4A CN103787547B (en) 2013-12-31 2013-12-31 The treatment process of aging percolate

Publications (2)

Publication Number Publication Date
CN103787547A CN103787547A (en) 2014-05-14
CN103787547B true CN103787547B (en) 2016-01-20

Family

ID=50663672

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310753307.4A Active CN103787547B (en) 2013-12-31 2013-12-31 The treatment process of aging percolate

Country Status (1)

Country Link
CN (1) CN103787547B (en)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104478175B (en) * 2014-12-24 2016-08-24 北京桑德环境工程有限公司 The processing system of a kind of kitchen castoff anaerobic fermentation biogas slurry and method
CN105439389B (en) * 2015-12-30 2018-07-03 北京欧亚泉环境投资管理有限公司 A kind of landfill leachate zero-discharge treatment system
CN105585196B (en) * 2016-01-26 2019-01-08 安徽普朗膜技术有限公司 The processing system of consumer waste infiltration liquid
CN105621807A (en) * 2016-02-02 2016-06-01 广东省环境保护工程研究设计院 Municipal domestic waste leachate (A/O)2 combined membrane biochemical reaction-reverse osmosis membrane treatment process
CN106277613B (en) * 2016-08-29 2019-07-05 江苏维尔利环保科技股份有限公司 Method for treating garbage percolation liquid
CN107473514B (en) * 2017-09-04 2020-12-29 高科环保工程集团有限公司 Household garbage leachate treatment system and technology
CN108002646A (en) * 2017-11-30 2018-05-08 重庆三峰环境产业集团有限公司 A kind of system and method for landfill leachate zero-emission

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1686863A (en) * 2005-04-05 2005-10-26 太原理工大学 Technique of biological treatment for wastewater of carbonization
CN101113065A (en) * 2007-06-27 2008-01-30 同济大学 Impact-resistant multiplication combined type coking waste water treatment process
CN101139137A (en) * 2007-08-17 2008-03-12 浙江大学 High-efficiency biological treatment method of high-organic matter high-kjeldahl type nitrogen chemical industry wastewater
CN101254980A (en) * 2008-03-25 2008-09-03 浙江大学 Biological denitrification system and method for low C/N ratio high strength ammonia chemical comprehensive wastewater
CN101445306A (en) * 2008-12-24 2009-06-03 哈尔滨工业大学 Coking wastewater treating method
CN101708919A (en) * 2009-11-16 2010-05-19 北京大学深圳研究生院 Method for treating leachate in refuse landfill site
CN101830610A (en) * 2010-05-31 2010-09-15 浙江汉蓝环境科技有限公司 Method for treating garbage percolate by using microbe
CN102001786A (en) * 2010-10-22 2011-04-06 中国瑞林工程技术有限公司 New high-nitrogen organic sewage treatment biochemical denitrification process
CN202529954U (en) * 2012-04-25 2012-11-14 株洲南方宇航环保工业有限公司 Municipal domestic waste leachate treatment system
CA2583752C (en) * 2004-10-12 2013-11-26 Biocast Systems, Inc. Integrated multi-zone wastewater treatment system and method

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100340098B1 (en) * 2000-05-08 2002-06-10 김동우 An elevated disposal process for the leakage water of reclaimed land

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2583752C (en) * 2004-10-12 2013-11-26 Biocast Systems, Inc. Integrated multi-zone wastewater treatment system and method
CN1686863A (en) * 2005-04-05 2005-10-26 太原理工大学 Technique of biological treatment for wastewater of carbonization
CN101113065A (en) * 2007-06-27 2008-01-30 同济大学 Impact-resistant multiplication combined type coking waste water treatment process
CN101139137A (en) * 2007-08-17 2008-03-12 浙江大学 High-efficiency biological treatment method of high-organic matter high-kjeldahl type nitrogen chemical industry wastewater
CN101254980A (en) * 2008-03-25 2008-09-03 浙江大学 Biological denitrification system and method for low C/N ratio high strength ammonia chemical comprehensive wastewater
CN101445306A (en) * 2008-12-24 2009-06-03 哈尔滨工业大学 Coking wastewater treating method
CN101708919A (en) * 2009-11-16 2010-05-19 北京大学深圳研究生院 Method for treating leachate in refuse landfill site
CN101830610A (en) * 2010-05-31 2010-09-15 浙江汉蓝环境科技有限公司 Method for treating garbage percolate by using microbe
CN102001786A (en) * 2010-10-22 2011-04-06 中国瑞林工程技术有限公司 New high-nitrogen organic sewage treatment biochemical denitrification process
CN202529954U (en) * 2012-04-25 2012-11-14 株洲南方宇航环保工业有限公司 Municipal domestic waste leachate treatment system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"复合式膜生物反应器处理老龄垃圾渗滤液的中试";王薇等;《中国给水排水》;20110331;第27卷(第5期);第93-96页 *

Also Published As

Publication number Publication date
CN103787547A (en) 2014-05-14

Similar Documents

Publication Publication Date Title
Peng Perspectives on technology for landfill leachate treatment
Lu et al. Study on method of domestic wastewater treatment through new-type multi-layer artificial wetland
Ødegaard A road-map for energy-neutral wastewater treatment plants of the future based on compact technologies (including MBBR)
CN102336498B (en) Nitrogen-phosphorus wastewater treating method by sequencing batch reactor coupled photobioreactor
US8246829B2 (en) Systems and methods for water treatment and remediation
Singh et al. Nutrient removal from membrane bioreactor permeate using microalgae and in a microalgae membrane photoreactor
CN101891336B (en) System and method for leachate treatment in sanitary landfill
Ma et al. Organic matter recovery from municipal wastewater by using dynamic membrane separation process
CN101234836B (en) Garbage percolate treatment technique
CN104671615B (en) A kind of Taihu Lake that is used for enters lake livestock and poultry cultivation sewage treatment process
CN100406399C (en) Method and system for harnessing consumer waste landfill percolate
US20020153303A1 (en) Reclaiming water and usable brine concentrate from domestic sewage
Farizoglu et al. Simultaneous removal of C, N, P from cheese whey by jet loop membrane bioreactor (JLMBR)
Li et al. Resources and nutrients oriented greywater treatment for non-potable reuses
CN1309665C (en) Nitrogen and phosphorus removing process
CN101357812B (en) Processing method for domestic garbage leachate
CN101671090B (en) Combined processing technique of garbage percolates
CN204454829U (en) A kind of integrated underground sewage treatment equipment efficiently
CN100398470C (en) Infiltration method for treating garbage
Moawad et al. Coupling of sequencing batch reactor and UASB reactor for domestic wastewater treatment
CN103819049B (en) A kind of sewage water treatment method and system
WO2010133177A1 (en) Landfill leachate wastewater treatment system and process thereof
CN101898854B (en) Method and device for treatment of high-sulfur content and low-permeability oil reservoir produced wastewater
CN100534928C (en) Short-path deep biological denitrogenation method for city garbage percolate
CN103880248B (en) A kind of coking wastewater processing system and treatment process

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
COR Change of bibliographic data

Free format text: CORRECT: APPLICANT; FROM: FUZHOU GARDEN ENVIRONMENTAL PROTECTION ENGINEERING CO., LTD. TO: GARDEN ENVIRONMENTAL PROTECTION CO., LTD.

C53 Correction of patent for invention or patent application
CB02 Change of applicant information

Address after: 350000 Gulou District, Fuzhou, Fuzhou Software Park, No. 89, software park, building C, No. 27

Applicant after: GARDEN ENVIRONMENTAL PROFECTION

Address before: 350000 Gulou District, Fuzhou, Fuzhou Software Park, No. 89, software park, building C, No. 27

Applicant before: Fuzhou Garden Environmental Protection Engineering Co., Ltd.

C14 Grant of patent or utility model
GR01 Patent grant