CN1907889A - Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique - Google Patents
Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique Download PDFInfo
- Publication number
- CN1907889A CN1907889A CN 200610089746 CN200610089746A CN1907889A CN 1907889 A CN1907889 A CN 1907889A CN 200610089746 CN200610089746 CN 200610089746 CN 200610089746 A CN200610089746 A CN 200610089746A CN 1907889 A CN1907889 A CN 1907889A
- Authority
- CN
- China
- Prior art keywords
- water
- uasb
- level
- iii
- reactor
- 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.)
- Granted
Links
Images
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
This invention relates to a treatment device and method for municipal solid waste leachate, belonging to wastewater treatment technology field. There are contradictions between anaerobic degradation of organic matter and biological denitrification in the existing processes and the equipments of the existing processes are expensive to run. The invention includes a two-level UASB+A/O processing device and method for municipal solid waste leachate. Methane production by anoxic denitrification and anaerobic reaction is carried out in one-level UASB (II) and further anaerobic reaction of methane production is carried out in two-level UASB (III). Anoxic reaction is carried out first in A/O reactor to remove part of the residual organic matter and then aerobic nitrification reaction is carried out to remove ammonia nitrogen. The invention can adapt to water quality change of leachate well without any physicochemical treatment. Biochemical organic matter and high ammonia nitrogen can all be removed through biological treatment. Wide application can greatly reduce the construction and operation costs of leachate treatment and greatly enhance municipal solid waste leachate treatment efficiency.
Description
Technical field
The present invention relates to a kind of biochemical city domestic refuse percolation liquid of thoroughly removing of physico-chemical pretreatment that do not need can biochemical organism and the apparatus and method of high ammonia nitrogen, belong to technical field of biological sewage treatment by using, be applicable to that city domestic refuse percolation liquid and other are such as anaerobic sludge digestion liquid, the contour ammonia nitrogen of breeding wastewater and high organic organic industrial sewage processing.
Background technology
The present rubbish annual amount of China reaches 2.4 hundred million tons, and the annual growth of domestic waste was all more than 8%～10% in recent years.China has the rubbish about 90% to handle with landfill method at present, and landfill can produce a large amount of percolates.Percolate is a kind of high concentrated organic wastewater of complicated component, and the discharge amount of pollution of national percolate accounts for 1.6 ‰ of year total blowdown flow rate, adjusts with chemical oxygen demand and but accounts for 5.27%.It is last one link of sanitary filling field that percolate is handled, and deals with improperly surrounding environment is brought immeasurable pollution and harm, and HUMAN HEALTH is brought threat, also makes sanitary landfill lose original meaning simultaneously.
Because leachate quality and Changing Pattern are understood not enough or are not given enough attention, municipal sewage treatment technology and design variable are indiscriminately imitated on the percolate treating process blindly, not only processing costs costliness, and also water outlet at all can't be up to standard.Simultaneously, some conclusions that relevant percolate is handled are also lost biased, say what others say, and lack the check of test and actual engineering.For example, think concentration of heavy metal ion height in the percolate, must carry out pre-treatment after, just can carry out biochemical treatment, but this judgement of successful proof of many actual engineering biochemical treatments is unilateral.There is viewpoint to think that the percolate of high ammonia nitrogen can suppress microbic activity, so before biochemistry, must adopt physicochemical techniques such as stripping to carry out pre-treatment.This viewpoint of our evidence is not meet the water quality characteristics of percolate and Changing Pattern thereof, is applied to put into practice the error that certainly will cause design and the waste of construction fund.Abandon exploring the leachate treatment technology of economical and efficient, the simple high reverse-osmosis treated technology of cost of use blindly makes that the processing of percolate is hard to carry on because expense is expensive.
Existing percolate device is seen accompanying drawing 1, mainly is made up of water tank I, UASB II, A/O reactor IV, second pond V and other auxiliary facility and pipeline.Water tank I is connected by the water-in 17 of intake pump 9 with UASB II bottom; UASB II top is provided with rising pipe 29 and is connected with the anaerobic reaction district of A/O reactor IV, and rising pipe 29 tops are provided with internal recycle outlet valve 18 and are connected with internal circulation pump 20, and internal circulation pump 20 is connected by the water-in 17 of pipeline with UASB II bottom.A/O reactor IV is divided into anaerobic reaction district and aerobic reactor zone totally 2 workspace.The hypoxia response district is connected by sludge reflux pump 63 with the bottom of second pond V, and aerobic reactor zone is connected with pipe 29 by treating water reflux pump 92.Second pond V top is provided with outlet valve 84.
Its working process is: utilize intake pump 9 and internal circulation pump 20 recirculated water of former percolate and UASB II to be pumped into the water-in 17 of UASB II bottom, in UASB II from bottom to top produce methane reaction, the anaerobic reaction district that the rising pipe 29 that supernatant liquor is provided with through UASB II top enters with A/O reactor IV carries out anaerobic reaction, enter aerobic reactor zone after anaerobic reaction is intact and carry out aerobic reaction, after aerobic reaction finishes, supernatant liquor loops back anaerobic zone by pump 92, mixed solution enters second pond V and carries out mud-water separation, supernatant liquor after the separation is discharged system by outlet valve, and the mud of bottom carries out recycle by the aerobic reactor zone that sludge reflux pump 63 enters A/O reactor IV.
Existing this technology is the combination of anaerobic reaction and aerobic reaction, denitrification carries out behind anaerobic reaction, this makes the organism anaerobic degradation of this technology and biological denitrificaion constitute irreconcilable contradiction: if anaerobism is abundant, so follow-up anoxic denitrification will be because lacking organic carbon source inefficiency, must add the further denitrogenations of physicochemical techniques such as membrane process; And if the anaerobic treatment weak effect, the organic loading of aerobic reactor is too high, causes a large amount of heterotrophic bacteria growth and breedings, and the growth and breeding of autotrophy nitrifier will be suppressed, and can't finish sufficient denitrification, causes system's denitrogenation failure.And high ammonia nitrogen is to microorganism, and particularly the restraining effect of aerobic microbiological makes existing technology must add physico-chemical pretreatment, and ammonia nitrogen degradation after lower level, is carried out a biological disposal upon again.
Summary of the invention
The objective of the invention is without any physico-chemical pretreatment, almost completely removing percolate by biological treatment can biochemical organism and high ammonia nitrogen.Biased on technological deficiency of handling at the conventional garbage percolate and the understanding developed the apparatus and method of percolate biochemical treatment, i.e. two-stage UASB+A/O art breading city domestic refuse percolation liquid apparatus and method.These apparatus and method have broken through the limitation of leachate treatment technology in the past, under the prerequisite that does not add any medicament and carbon source, not only can biochemical organism and ammonia nitrogen almost all remove, and realized the nitrogen removal rate more than 90% by denitrification before the anaerobism and substep denitrification.Organism during denitrification will be intake before the anaerobism at first is consumed as denitrifying carbon source, and anaerobism product methane reaction can thoroughly carry out, thereby is that follow-up nitration reaction is created the adapt circumstance condition.Because effluent recycling has diluted influent ammonium concentration, need not any physico-chemical pretreatment technology.This invention not only solves the contradiction of existing technology, and have that technical process is simple, the fluctuation that adapts to the leachate quality and the water yield, flexible operation, characteristics simple to operate.Be applied to reality and can significantly reduce construction and working cost, non-secondary pollution.
Know-why:
The organic content of percolate can reach 30000mg/L, at first adopts two-stage UASB (upflow anaerobic sludge blanket process) to produce methane reaction degradation of organic substances significantly by denitrification and anaerobism.It is big to have avoided direct employing aerobe to handle the aeration power consumption that causes, the drawback that excess sludge production is high, and can reclaim methane.And the remaining organism of anaerobism water outlet is further degraded in follow-up A/O technology, makes to reach removal completely by biochemical organism.
The high ammonia nitrogen of percolate (can reach 3000mg/L) at first carries out nitration reaction completely at aerobic reactor, ammonia nitrogen NH
4 +-N is nitric nitrogen NO by oxidation by nitrobacteria all
3 --N then refluxes by treating water respectively and denitrification is finished in the backflow of second pond mud, and promptly denitrifying bacteria utilizes organic carbon source as electron donor, NO
3 --N is reduced to nitrogen as electron acceptor(EA) and overflows from percolate and finish biological denitrificaion.Most of organism had reached degraded after percolate entered into aerobic reactor, this has created suitable condition for the autotrophic type nitrifier to the oxidation of ammonia nitrogen, and ammonia nitrogen thoroughly nitrated in the aerobic reactor, diluted the ammonia nitrogen concentration of water inlet when making effluent recycling greatly, restraining effect to microorganism in the system greatly weakens, and makes the exhaustive oxidation of ammonia nitrogen and high efficiency denitrogenation become possibility.Can make full use of former water carbon source and finish denitrification and in one-level UASB, carry out denitrification, reclaim the nitration reaction that basicity is finished follow-up Aerobic Pond simultaneously.
Two-stage UASB+A/O art breading garbage filter liquid device provided by the invention is characterized in that: mainly be made up of integrated water tank I, one-level UASB II, secondary UASB III, A/O reactor IV, second pond V;
Integrated water tank I is divided into former percolate water tank 1 and treating water water tank 6 two portions, and former percolate water tank 1 is connected by the water-in 17 of intake pump 9 with one-level UASB II bottom; The top for the treatment of water water tank 6 is provided with water discharging valve 11, and treating water water tank 6 middle parts are connected with second pond V by managing 90, and treating water water tank 6 bottoms are connected with the penstock 10 of intake pump 9 by treating water recycle pump 1;
Built-in triphase separator 22 of one-level UASB II and airway 23, airway 23 is connected with alkali lye bottle 26, alkali lye bottle 26 is connected with gas meter 28, one-level UASB II top is provided with rising pipe 29 and is connected with the water-in 38 of secondary UASBIII bottom, rising pipe 29 tops are provided with internal recycle outlet valve 18 and are connected with internal circulation pump 20, and internal circulation pump 20 is connected by the water-in 17 of pipeline with one-level UASB II bottom;
The built-in triphase separator 35 of secondary UASBIII, airway 36, airway 36 is connected with alkali lye bottle 39, alkali lye bottle 39 is connected with gas meter 41, secondary UASB top is provided with rising pipe 50 and is connected with A/O reactor IV, rising pipe 50 tops are installed internal recycle outlet valve 39 and are connected with internal circulation pump 41, and internal circulation pump 41 is connected with water-in 38 bottom secondary UASB by pipeline;
A/O reactor IV is divided into anaerobic reaction district and aerobic reactor zone totally 2 workspace, and agitator 62 is installed in the anaerobic reaction district, and aerobic reactor zone is connected with air pump 59, and aerobic reactor zone is connected by the bottom of sludge reflux pump 63 with second pond V;
Second pond V top is provided with flowing water Valve 84, and flowing water Valve 84 is connected with treating water water tank 6 by return line 90.
The present invention also provides a kind of garbage leachate treatment process that utilizes said apparatus, and its step comprises:
1) denitrification mud and anaerobic grain sludge are dosed one-level UASB II, anaerobic grain sludge is dosed secondary UASBIII, simultaneously aerobic activated sludge is added to A/O reactor IV, carry out the domestication and the cultivation of bacterial classification;
2) former percolate and system's reflow treatment water are packed into respectively former percolate water tank 1 and treating water water tank 6, start intake pump 9 and treating water reflux pump 15, the flow that makes the flow of former percolate and system handles water is by 1: 2-1: 4 mixed enters the water-in 17 of one-level UASB II, when liquid is full of one-level UASB II, start internal circulation pump 20, make liquid enter into the water-in 17 of one-level UASB II through internal circulation pump 20, carry out the internal recycle of one-level UASB II, circular flow is greater than the flow of water inlet mixed solution, and working cycle is maintained until NOx--N＜10mg/L in the one-level UASB II water outlet;
In the inner cyclic process of one-level UASB II, denitrifying bacterium in the denitrification mud utilize in the former percolate can biochemical organism with the thorough denitrification of NOx--N in system's reflow treatment water, produce nitrogen, and recovery basicity, hold pH＞8.0 of system, after denitrification finishes, methane reaction takes place to produce, nitrogen, methane and the CO2 that produces flowing from bottom to top, separation through triphase separator 22, enter into alkali lye bottle 26 by airway 23, CO2 is absorbed by alkali lye in alkali lye bottle 26, and nitrogen and methane are through gas meter 28 metering back dischargings;
3) when NOx--N in the one-level UASB II water outlet＜10mg/L, make liquid among the one-level UASB II enter the water-in 38 of secondary UASBIII through rising pipe 20, when liquid is full of secondary UASBIII, start internal circulation pump 41, make liquid enter into the water-in 38 of secondary UASBIII through internal circulation pump 41, carry out the internal recycle of secondary UASBIII, circular flow is greater than the flow of water inlet mixed solution, and working cycle is maintained until that the COD concentration value is 2500-3000mg/L in the secondary UASBIII water outlet;
In the inner cyclic process of secondary UASBIII, produce methane reaction, methane that produces and CO2 flowing from bottom to top, separation through triphase separator 43, enter into alkali lye bottle 47 by airway 44, in alkali lye bottle 47, CO2 is absorbed by alkali lye, and methane is through gas meter 49 metering back dischargings;
4) when the COD concentration value is 2500-3000mg/L in the secondary UASBIII water outlet, make liquid among the secondary UASBIII enter the anaerobic reaction district of A/O reactor IV, start agitator 62, carry out anti-nitration reaction, start agitator (62), carry out anti-nitration reaction, after the denitrification mixed solution enters into aerobic reactor zone, booster air pump (59) carries out aeration, carry out nitration reaction and remove high ammonia nitrogen, when pH value is reduced to lower-most point, promptly " ammonia paddy " occurs, and during the NOx--N in the liquid＜15mg/L, nitration reaction finishes;
5) after nitration reaction finishes, make A/O reactor (IV) aerobic reactor zone liquid enter second pond (V) and carry out mud-water separation, after mud-water separation finishes, open sludge reflux pump (63), active sludge is back to A/O reactor (IV) from the bottom of second pond (V), simultaneously, open flowing water Valve (84), make the liquid return on second pond (V) top enter into treating water water tank (6);
6) when the recirculation water liquid level in the treating water water tank 6 was lower than water discharging valve 11, liquid entered penstock 10 by treating water recycle pump 1, circulates;
When the recirculation water liquid level in the treating water water tank 6 was higher than water discharging valve 11, opening water discharge valve 11 was discharged system with the recirculation water overflow.
The two-stage UASB+A/O art breading percolate apparatus and method that the present invention relates to compared with prior art have following advantage:
1) reflow treatment water not only can be finished denitrification, and can improve the upflow velocity of anaerobic reactor, has avoided mud to harden and the generation of channeling, and the effect that visible treating water refluxes is many-sided;
2) anti-nitration reaction takes place in former percolate and recycling effluent in one-level UASB, and denitrifying bacterium and methanogen are relatively, denitrifying bacterium growth velocity height, strong to the adaptability of envrionment conditions, simultaneously, it plays a protective role to the product methane reaction of secondary UASB;
3) secondary UASB removes the most of organism of one-level UASB water outlet by producing methane reaction, because pH is higher, and the part organic carbon is converted into inorganic carbon, basicity improves by a relatively large margin behind the anaerobic reaction simultaneously.The nitrated matrix and the envrionment conditions that suit created that is generated as the high ammonia nitrogen of follow-up aerobic reactor of organic degraded significantly and basicity;
4) anaerobism water outlet residual organic substances is at first as NO in the returned sluge
x -The degraded of the denitrifying carbon source of-N and anoxic.Thereby the major part in this technology can be removed under anaerobism and anoxybiotic condition by biochemical organism, has not only saved the aeration expense, and partly is utilized as denitrifying carbon source, and another part then is converted into methane or basicity;
5) enter and promptly carry out the nitrated of remaining organic thorough degraded and high ammonia nitrogen behind the aerobic zone.By the nitrated basicity of utilizing in the anaerobism water outlet, high ammonia nitrogen is removed completely;
6) in nitrifying process, as controlled variable, as the reference mark, can indicate the ammonia oxidation end point accurately and effectively with the lower-most point of pH value with pH.Thereby, after occurring, the lower-most point of pH value promptly stops aeration, not only can save aeration rate, prevented aeration, and save the aeration expense.
Description of drawings
The existing percolation liquid treating system synoptic diagram of Fig. 1;
" two-stage UASB+A/O " treatment system synoptic diagram that Fig. 2 the present invention adopts;
Reference numeral:
The integrated water tank of I-, II-one-level UASB, III-secondary UASB, IV-A/O reactor, V-second pond;
The penstock of the penstock of the former percolate water tank of the integrated water tank of I-: 1-, 6-treating water water tank, 7-water absorption tube, 8-inlet valve, 9-intake pump, 10-pump 9,11-flowing water Valve, 12-treating water reverse flow valve, 13-treating water water intaking valve, 14-treating water water inlet pipe, 15-treating water intake pump, 16-pump 15;
II-one-level UASB:17-one-level UASB water-in, 18-one-level UASB internal recycle valve, 19-one-level UASB internal recycle water inlet pipe, 20-one-level UASB internal circulation pump, 21-one-level UASB internal recycle rising pipe, 22-triphase separator, 23-airway, the clear and coherent valve of 24-gas circuit, 25-biogas delivery pipe, 26-alkali lye bottle, 27-alkali lye bottle and under meter pipe connecting, 28-gas meter, 29-one-level UASB rising pipe, 30～37-one-level UASB sampling valve;
III-secondary UASB:38-secondary UASB water-in, 39-secondary UASB internal recycle valve, 40-internal recycle water inlet pipe, 41-secondary UASB internal circulation pump, 42-internal recycle rising pipe, 43-triphase separator, 44-airway, the clear and coherent valve of 45-gas circuit, 46-biogas delivery pipe; 47-alkali lye bottle, 48-alkali lye bottle and under meter pipe connecting, 49-gas meter, 50-secondary UASB rising pipe, 51～58-secondary UASB sampling valve;
IV-A/O reactor: 59-air pump, 60-aeration tube, 61-gas meter, 62-agitator, 63-sludge reflux pump, 64-mud return line, 65～73-artificial atmosphere valve, 74～82-aeration head, 83-aeration tank rising pipe, 91-water return line, 92-water reflux pump, 93-water return line;
The V-second pond: 84-second pond outlet valve, 85～87-sampling valve, 88-pipe core, 89-sludge reflux pump advance mud pipe, 90-effluent recycling pipe.
Embodiment
In conjunction with Fig. 2, the operation operation of technology of the present invention:
Experimental water is taken from the equalizing tank percolate of Beijing's refuse landfill, and percolate is aterrimus, thickness, foul smelling, this leachate quality: COD 7000～25000mg/l; BOD5 3500～14000mg/l; NH4+-N 1250～2450mg/l; SS 2000～4000mg/l; Basicity 8000～11000mg/l; TP9～15mg/l; PH 7.2～7.9.Per two days sampling analysis once, the analytical procedure that adopts in the test all is standard methods of State Bureau of Environmental Protection issue.This percolate is typical city domestic refuse percolation liquid, organism and ammonia nitrogen concentration height, but heavy metal content is relatively low.Pilot system is made up of two-stage UASB II, III and A/O reactor IV as shown in Figure 1.The internal diameter of one-level UASB II is 5cm, highly is 210cm, and useful volume is 4.25L.The internal diameter of secondary UASBIII is 8cm, highly is 200cm, and useful volume is 8.25L.The useful volume of A/O reactor IV is 15L, is divided into ten lattice chambers, and the first lattice chamber is the oxygen-starved area.Two-stage UASB adopts preheating to add the mode control reaction temperature of insulation, and the temperature of one-level UASB II and secondary UASBIII is controlled at 30 ℃, 35 ℃ respectively, and aerobic reactor moves under 15-32 ℃ room temperature.The granule sludge of anaerobism inoculation is taken from the UASB reactor of brew-house, and the active sludge of A/O reactor IV inoculation is taken from the activated sludge reactor of handling sanitary sewage.
Detailed process is as follows:
At first raw water box 1 is filled with former percolate, treating water water tank 6 is filled with system handles water.Open valve 8 and 13, start intake pump 9 and treating water reflux pump 15, the flow of intake pump is 5.5L/d, the flow for the treatment of water reflux pump is 3 times of raw water flow, be 16.5L/d, then the flow of one-level UASB II water inlet mixed solution is the 22L/d. while, opens valve 18, start the internal recycle that internal circulation pump 20 carries out one-level UASB II, circular flow is 24L/d.
Biochemical reaction takes place with the microorganism in the cylinder in this reactor of water inlet mixed solution process from bottom to top of one-level UASB II.Denitrification at first takes place in the water inlet mixed solution in reactor, denitrifying bacteria utilizes the abundant organic carbon source of former percolate with reflow treatment water NO
x --N is converted into nitrogen.After denitrification finishes, the methanogen among the one-level UASB II will partly remain organic-biological and be converted into methane.Nitrogen that produces and methane flowing from bottom to top, the separation through triphase separator 22 enters into alkali lye bottle 26 by airway 23, the CO in alkali lye bottle 26 in the biogas
2Absorbed by alkali lye, and nitrogen and methane are through gas meter 28 metering back dischargings.By the height sampling analysis of sampling valve 30～37 from reactor, pollutent Changing Pattern is therein studied the Changing Pattern of microorganism simultaneously.Then pass through the separation of triphase separator, supernatant liquor enters into secondary UASBIII through the rising pipe 29 of one-level UASB II.
After one-level UASB II processing, its water outlet NO
x --N almost all is converted into nitrogen.Organism in the former percolate obtains the part degraded by denitrification and product methane reaction.
Start 62 pairs of mixed solutions of agitator and stir the denitrification of finishing returned sluge.Start the feed-water end that sludge reflux pump 63 is back to the mud of second pond V A/O reactor IV.By stirring the denitrification of oxygen-starved area (lattice chamber 1), the NO of returned sluge
x --N is converted into nitrogen.Open air control valve 65～73, the flow of gas meter is adjusted into 400L/h, booster air pump 59 by blast main 60, carries out aeration through the mixed solution in 74～82 pairs of aeration tanks of aeration head.The thoroughly nitrated of high ammonia nitrogen closed in the oxidation that (2-10 lattice chamber) finishes residual organic substances in the aeration zone.A/O reactor IV mixed solution enters the pipe core 88 of second pond V by rising pipe 83, and uniform water distribution in second pond V then carries out mud-water separation.Open flowing water Valve 84 after the mud-water separation, supernatant liquor enters into treating water water tank 6 by effluent recycling pipe 90.Open valve 11, final outflow water overflows system.
Long run test result shows: maximum COD removes that speed is respectively 12.5,8.5Kg COD/m in one-level UASB II and secondary UASBIII
3D, NO in one-level UASB II
x -The maximum removal rate of-N is 3.0Kg NO
x --N/m
3D.The water outlet COD of two-stage UASB is 2000-3000mg/l, and wherein about 50% COD is difficult to biochemistry, and this is nitrated the created favourable condition of high ammonia nitrogen at A/O reactor IV.The COD clearance of system is 80-92%, and water outlet COD is 800-1500mg/l.One-level UASBII is 0.28m 30 ℃ gas yield
3/ Kg COD, the composition of gas is relatively stable, CH
4, N
2, CO
2Shared ratio is respectively 63-73,25-35,2%.Secondary UASBIII is 0.40m 35 ℃ gas yield
3/ Kg COD, CH
4, CO
2Shared ratio is respectively 98,2%.The NH of former percolate
4 +-N concentration is 1100-2000mg/l, the maximum NH of A/O reactor IV
4 +It is 0.68KgNH that-N removes speed
4 +-N/m
3D, at 17-30 ℃, NH
4 +The clearance of-N about 99%, water outlet NH
4 +-N concentration is lower than 15mg/l.NO in recycling effluent and the second pond V returned sluge
x --N at the anoxic section realization denitrification almost completely of one-level UASB II and A/O reactor IV, makes system's inorganic nitrogen TIN clearance at 80-92% respectively.
Denitrification provides competent basicity for nitrated completely, makes A/O reactor IVpH＞8.5, for realizing stable nitrated creation prerequisite.The mud of each reactor all is independently in the system, has formed dominant microflora separately, finishes denitrification respectively, produces methane and nitration reaction.Remove NH with physicochemical techniques such as ammonia stripping, reverse osmosiss
4 +-N compares, and the native system economical and efficient does not have secondary pollution, and removing for the short distance nitration of high ammonia nitrogen in the percolate simultaneously provides practicable technical parameter, reduces construction and working cost that percolate is handled largely.
Claims (2)
1. a two-stage UASB+A/O art breading garbage filter liquid device is characterized in that: mainly be made up of integrated water tank (I), one-level UASB (II), secondary UASB (III), A/O reactor (IV), second pond (V);
Integrated water tank (I) is divided into former percolate water tank (1) and treating water water tank (6) two portions, former percolate water tank (1) is connected by the water-in (17) of intake pump (9) with one-level UASB (II) bottom, the top for the treatment of water water tank (6) is provided with water discharging valve (11), treating water water tank (6) is connected with second pond (V) by pipe (90), and treating water water tank (6) is connected with the penstock (10) of intake pump (9) by treating water recycle pump (15);
Built-in triphase separator of one-level UASB (II) (22) and airway (23), airway (23) is connected with external alkali lye bottle (26), alkali lye bottle (26) is connected with gas meter (28), one-level UASB (II) top is provided with rising pipe (29) and is connected with the water-in (38) of secondary UASB (III) bottom, rising pipe (29) top is provided with internal recycle outlet valve (18) and is connected with internal circulation pump (20), and internal circulation pump (20) is connected by the water-in (17) of pipeline with one-level UASB (II) bottom;
The built-in triphase separator of secondary UASB (III) (35), airway (36), airway (36) is connected with alkali lye bottle (39), alkali lye bottle (39) is connected with gas meter (41), secondary UASB (III) top is provided with rising pipe (50) and is connected with A/O reactor (IV), rising pipe (50) top is installed internal recycle outlet valve (39) and is connected with internal circulation pump (41), and internal circulation pump (41) is connected with water-in (38) bottom secondary UASB (III) by pipeline;
A/O reactor (IV) is divided into hypoxia response district and aerobic reactor zone totally 2 workspace, agitator (62) is installed in the hypoxia response district, aerobic reactor zone is connected with air pump (59), and aerobic reactor zone is connected by the bottom of sludge reflux pump (63) with second pond (V);
Second pond (V) top is provided with flowing water Valve (84), and flowing water Valve (84) is connected with treating water water tank (6) by return line (90).
2. a two-stage UASB+A/O art breading garbage filter liquid processing method is characterized in that, is made up of following steps:
1) denitrification mud and anaerobic grain sludge are dosed one-level UASB (II), anaerobic grain sludge is dosed secondary UASB (III), simultaneously aerobic activated sludge is added to A/O reactor (IV), carry out the domestication and the cultivation of bacterial classification;
2) former percolate and system's reflow treatment water are packed into respectively former percolate water tank (1) and treating water water tank (6), start intake pump (9) and treating water reflux pump (15), the flow that makes the flow of former percolate and system handles water is by 1: 2-1: 4 mixed enters the water-in (17) of one-level UASB (II), when liquid is full of one-level UASB (II), start internal circulation pump (20), make liquid enter into the water-in (17) of one-level UASB (II) through internal circulation pump (20), carry out the internal recycle of one-level UASB (II), the internal recycle flow is greater than the flow of water inlet mixed solution, and working cycle is maintained until NOx--N＜10mg/L in one-level UASB (II) water outlet;
In one-level UASB (II), the denitrifying bacterium in the denitrification mud utilize in the former percolate can biochemical organism with the NO in system's reflow treatment water
x --N denitrification produces nitrogen, and reclaims basicity, and pH＞8.0 of keeping system after denitrification finishes, methane reaction, the nitrogen of generation, methane and CO take place to produce
2Flowing from bottom to top, the separation through triphase separator (22) enters into alkali lye bottle (26) by airway (23), CO in alkali lye bottle (26)
2Absorbed by alkali lye, nitrogen and methane are through gas meter (28) metering back discharging;
3) when NOx--N in one-level UASB (II) water outlet＜10mg/L, make liquid among the one-level UASB (II) enter the water-in (38) of secondary UASB (III) through rising pipe (20), when liquid is full of secondary UASB (III), start internal circulation pump (41), make liquid enter into the water-in (38) of secondary UASB (III) through internal circulation pump (41), carry out the internal recycle of secondary UASB (III), the internal recycle flow is greater than the flow of water inlet mixed solution, and working cycle is maintained until that the COD concentration value is 2500-3000mg/L in secondary UASB (III) water outlet;
In secondary UASB (III), methane reaction, the methane of generation and CO take place to produce
2Flowing from bottom to top, the separation through triphase separator (43) enters into alkali lye bottle (47) by airway (44), in alkali lye bottle (47), CO
2Absorbed by alkali lye, methane is through gas meter (49) metering back discharging;
4) when the COD concentration value is 2500-3000mg/L in secondary UASB (III) water outlet, make liquid among the secondary UASB (III) enter the hypoxia response district of A/O reactor (IV), start agitator (62), carry out anti-nitration reaction, after the denitrification mixed solution entered into aerobic reactor zone, booster air pump (59) carried out aeration, carry out nitration reaction and remove high ammonia nitrogen, when pH value is reduced to lower-most point, promptly " ammonia paddy " occurs, and the NO in the liquid
x -During-N＜15mg/L, nitration reaction finishes;
5) after nitration reaction finishes, make A/O reactor (IV) aerobic reactor zone liquid enter second pond (V) and carry out mud-water separation, after mud-water separation finishes, open sludge reflux pump (63), active sludge is back to A/O reactor (IV) from the bottom of second pond (V), simultaneously, open flowing water Valve (84), make the liquid return on second pond (V) top enter into treating water water tank (6);
6) when the recirculation water liquid level in the treating water water tank (6) is lower than water discharging valve (11), liquid enters penstock (10) by treating water recycle pump (1), circulates;
When the recirculation water liquid level in the treating water water tank (6) is higher than water discharging valve (11), carry out the overflow water outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610089746XA CN100422096C (en) | 2006-07-14 | 2006-07-14 | Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610089746XA CN100422096C (en) | 2006-07-14 | 2006-07-14 | Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1907889A true CN1907889A (en) | 2007-02-07 |
| CN100422096C CN100422096C (en) | 2008-10-01 |
Family
ID=37699147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200610089746XA Active CN100422096C (en) | 2006-07-14 | 2006-07-14 | Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100422096C (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101284697B (en) * | 2008-04-02 | 2010-06-02 | 北京城市排水集团有限责任公司 | Device and method for realizing shortcut nitrification of sludge-digestion liquid by combined control of FA and FNA |
| CN101805096A (en) * | 2010-03-26 | 2010-08-18 | 北京工业大学 | Method for treating rubbish percolates of different times for deep denitrification by using bipolar USAB+A/O+SBR process |
| CN102107997A (en) * | 2011-01-12 | 2011-06-29 | 北京林业大学 | Method for treating leachate of domestic waste incineration plants |
| CN101723538B (en) * | 2008-10-24 | 2012-01-25 | 北京华明广远环境科技有限公司 | Process for treating landfill leachate |
| CN102351366A (en) * | 2011-06-30 | 2012-02-15 | 北京交通大学 | Device and method for treating pharmaceutical waste water through synchronous biological denitrification and devulcanization and autotrophic biological denitrification |
| CN102515429A (en) * | 2011-12-09 | 2012-06-27 | 北京工业大学 | Device and method for combined denitrification of anoxic-oxic (A/O) shortcut nitrification and anaerobic ammonia oxidation of late-stage landfill leachate |
| CN102515428A (en) * | 2011-12-09 | 2012-06-27 | 北京工业大学 | Combined device for synchronous denitrification and methanogenesis as well as autotrophic nitrogen removal of landfill leachate and method thereof |
| CN102557339A (en) * | 2011-12-19 | 2012-07-11 | 北京昊业怡生科技有限公司 | Treatment method of landfill leachate |
| CN104291517A (en) * | 2014-08-25 | 2015-01-21 | 杭州清城能源环保工程有限公司 | Standard discharge treatment system for livestock and poultry waste water and method thereof |
| CN105668780A (en) * | 2014-11-21 | 2016-06-15 | 中国寰球工程公司 | Acidification quick-recovery anaerobic reaction system |
| CN110104907A (en) * | 2019-06-11 | 2019-08-09 | 武汉深能环保新沟垃圾发电有限公司 | A kind of landfill leachate oil removing system and method |
| CN111018238A (en) * | 2019-11-27 | 2020-04-17 | 中建科技有限公司 | System and method for treating press filtrate of refuse transfer station |
| CN113264643A (en) * | 2021-06-02 | 2021-08-17 | 知和环保科技有限公司 | Treatment process for standard discharge of leachate in incineration plant |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100361909C (en) * | 2005-10-20 | 2008-01-16 | 彭永臻 | Adjusting method for A/O biological denitrification reactor and nitrification process, its on-line fuzzy controller and control thereof |
-
2006
- 2006-07-14 CN CNB200610089746XA patent/CN100422096C/en active Active
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101284697B (en) * | 2008-04-02 | 2010-06-02 | 北京城市排水集团有限责任公司 | Device and method for realizing shortcut nitrification of sludge-digestion liquid by combined control of FA and FNA |
| CN101723538B (en) * | 2008-10-24 | 2012-01-25 | 北京华明广远环境科技有限公司 | Process for treating landfill leachate |
| CN101805096A (en) * | 2010-03-26 | 2010-08-18 | 北京工业大学 | Method for treating rubbish percolates of different times for deep denitrification by using bipolar USAB+A/O+SBR process |
| CN102107997B (en) * | 2011-01-12 | 2012-09-05 | 北京林业大学 | Method for treating leachate of domestic waste incineration plants |
| CN102107997A (en) * | 2011-01-12 | 2011-06-29 | 北京林业大学 | Method for treating leachate of domestic waste incineration plants |
| CN102351366A (en) * | 2011-06-30 | 2012-02-15 | 北京交通大学 | Device and method for treating pharmaceutical waste water through synchronous biological denitrification and devulcanization and autotrophic biological denitrification |
| CN102351366B (en) * | 2011-06-30 | 2013-01-23 | 北京交通大学 | Device and method for treating pharmaceutical waste water through synchronous biological denitrification and devulcanization and autotrophic biological denitrification |
| CN102515428A (en) * | 2011-12-09 | 2012-06-27 | 北京工业大学 | Combined device for synchronous denitrification and methanogenesis as well as autotrophic nitrogen removal of landfill leachate and method thereof |
| CN102515429A (en) * | 2011-12-09 | 2012-06-27 | 北京工业大学 | Device and method for combined denitrification of anoxic-oxic (A/O) shortcut nitrification and anaerobic ammonia oxidation of late-stage landfill leachate |
| CN102515428B (en) * | 2011-12-09 | 2013-11-06 | 北京工业大学 | Combined device for synchronous denitrification and methanogenesis as well as autotrophic nitrogen removal of landfill leachate and method thereof |
| CN102557339A (en) * | 2011-12-19 | 2012-07-11 | 北京昊业怡生科技有限公司 | Treatment method of landfill leachate |
| CN102557339B (en) * | 2011-12-19 | 2014-10-01 | 北京昊业怡生科技有限公司 | Treatment method of landfill leachate |
| CN104291517A (en) * | 2014-08-25 | 2015-01-21 | 杭州清城能源环保工程有限公司 | Standard discharge treatment system for livestock and poultry waste water and method thereof |
| CN105668780A (en) * | 2014-11-21 | 2016-06-15 | 中国寰球工程公司 | Acidification quick-recovery anaerobic reaction system |
| CN105668780B (en) * | 2014-11-21 | 2018-10-16 | 中国寰球工程公司 | It is acidified fast quick-recovery anaerobic reaction system |
| CN110104907A (en) * | 2019-06-11 | 2019-08-09 | 武汉深能环保新沟垃圾发电有限公司 | A kind of landfill leachate oil removing system and method |
| CN110104907B (en) * | 2019-06-11 | 2022-03-29 | 武汉深能环保新沟垃圾发电有限公司 | Landfill leachate oil removal system and method |
| CN111018238A (en) * | 2019-11-27 | 2020-04-17 | 中建科技有限公司 | System and method for treating press filtrate of refuse transfer station |
| CN113264643A (en) * | 2021-06-02 | 2021-08-17 | 知和环保科技有限公司 | Treatment process for standard discharge of leachate in incineration plant |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100422096C (en) | 2008-10-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100422096C (en) | Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique | |
| CN100534928C (en) | Short-path deep biological denitrogenation method for city garbage percolate | |
| CN1032527C (en) | Method of treating waste water and equipment therefor | |
| CN104761097B (en) | It is a kind of suitable for high concentration, the processing method of organic wastewater with difficult degradation thereby total nitrogen | |
| CN110143725A (en) | Mixing sludge fermentation liquid is that carbon source continuous flow short-cut denitrification couples anaerobic ammonia oxidation process Treating Municipal Sewage device and method | |
| CN100357201C (en) | Artificial leather effluent treating process | |
| CN101376552A (en) | Process for processing high concentration refractory organic wastewater containing paratoluidine | |
| KR100815017B1 (en) | Method For Purifying Leachate of Landfill and Dewatering Water of Food Waste | |
| CN102010094A (en) | Method for treating high-calcium and high-salt industrial wastewater | |
| CN206580707U (en) | A kind of coking chemical waste water total system | |
| CN110642474A (en) | anaerobic-AO-SACR combined type high ammonia nitrogen sewage deep denitrification system and process | |
| CN105712584A (en) | Denitrification method and device for synchronously treating livestock farm biogas liquid wastewater and municipal sewage through combination of segmented partial nitrification and anaerobic ammonia oxidation | |
| CN102351366B (en) | Device and method for treating pharmaceutical waste water through synchronous biological denitrification and devulcanization and autotrophic biological denitrification | |
| CN101805096B (en) | Method for treating rubbish percolates of different times for deep denitrification by using bipolar USAB+A/O+SBR process | |
| CN106882906A (en) | It is exclusively used in the efficient low-consume denitrifying method of trade effluent | |
| CN112744912A (en) | Sulfur autotrophic denitrification biological filter, sewage treatment system and treatment method thereof | |
| CN1385380A (en) | Method for treating acrylonitrile and acrylic waste water | |
| CN113698049A (en) | Process for treating and recycling pig-raising wastewater containing water-washed manure and water-soaked manure | |
| CN107055963B (en) | Efficient and low-consumption advanced treatment device and treatment method for landfill leachate | |
| CN101050020A (en) | Method for treating wastewater by technique of sludge decrement type biomembrane piled ball packing | |
| CN2931465Y (en) | Apparatus of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique | |
| CN104310710A (en) | High-efficiency energy-saving treatment process for coal chemical industry wastewater | |
| CN218811022U (en) | Integrated treatment device for deep denitrification of garbage penetration filtrate | |
| CN111977893B (en) | Biochemical treatment method for wastewater generated in production of hydrogen peroxide by anthraquinone process based on composite microbial inoculum | |
| CN110697991B (en) | Garbage leachate biological treatment process and system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |