CN105565491A - Activated sludge treatment method and system for wastewater - Google Patents
Activated sludge treatment method and system for wastewater Download PDFInfo
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- CN105565491A CN105565491A CN201410548713.1A CN201410548713A CN105565491A CN 105565491 A CN105565491 A CN 105565491A CN 201410548713 A CN201410548713 A CN 201410548713A CN 105565491 A CN105565491 A CN 105565491A
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Abstract
The invention discloses an activated sludge treatment method for wastewater. The method comprises the following steps that 1, under the anoxic treatment condition, the wastewater makes contact with a material containing activated sludge, and anoxic treatment on the wastewater is performed; 2, aerobiotic treatment is performed on a mixture obtained after the contact; 3, part of a mixed material obtained through aerobiotic treatment is returned to the step 1 to serve as part of the material containing the activated sludge, wherein the particle size of at least 60 wt% of the activated sludge in the mixed material which is obtained through aerobiotic treatment and returned to the step 1 is not larger than 1 mm. The invention further provides an activated sludge treatment system for the wastewater. According to the activated sludge treatment method and system for the wastewater, the degradation and nitrification efficiency of organic matter difficult to degrade in the wastewater is promoted, and agentia feeding and O pool aeration strengthening are not needed; the advantages of being low in operation cost and free of by-products are achieved.
Description
Technical field
The present invention relates to a kind of activated sludge treatment method of waste water, and a kind of active sludge processing system for wastewater treatment.
Background technology
Existing more ripe wastewater processing technology generally adopts the combined treatment process of single-stage or two-stage air supporting and active sludge.Technique is stable using it for A/O (anoxic/aerobic), Operation and Maintenance is simple, can effectively the advantage such as denitrogenation always as the first-selected technique of biological wastewater treatment.
For refinery oily(waste)water, petroleum substance content is up to 500mg/L or more, it is after multiple-unit oil removing pre-treatment, the former water entering A/O technique still containing a certain amount of colloidal type dispersed oil and oil in water emulsion, thus there will be that these tiny oil droplets are adsorbed on active pollution index, coated situation.This causes on the one hand, and mud mass transfer is obstructed, activity is lower, can produce a large amount of oil-containing excess sludge on the other hand.Due to the existence of refinery oily(waste)water toxic, Persistent organic pollutants, the organic toxicity of the restriction of excess sludge certainly will be caused.High for large, the organic toxicity of refinery oily(waste)water biological treatment residue biological sludge output, be difficult to the problem of recycling, often carry out useless process of endangering at present, or burning disposal.All there is energy consumption waste and environment brought to the problem of remarkable risk in these two kinds of processing modes.
Therefore, by the Optimal improvements of A/O process, realizing mud Sources decreasing and toxicity source abatement, is the primary selection solving refinery water excess sludge problem.At present, conventional mud Sources decreasing method be undertaken being oxidized by uncoupler or ozone in systems in which, adopt the means such as supersonic method to be cracked by excess sludge after be back in aeration tank and be degraded by microorganisms, thus reach object source being reduced excess sludge production, but there is secondary pollution, be difficult to problems such as controlling, running cost is high in these methods.
Tiny oil droplets residual in refinery oily(waste)water is adsorbed on active pollution index, coated, and then cause substrate (organic substrates or ammonia nitrogen etc.) to mud flco active zone mass transfer difficulty, the dissolved oxygen (DO) of Aerobic Pond (O pond) is obstructed to mud flco internal mass transfer, cause sludge activity low, and the denitrifying carbon source in anaerobic pond (A pond) is not enough, makes water treatment effect reduce.For this problem, in existing engineer applied, usually through strengthening the air aeration intensity in O pond to solve this problem.The energy consumption of air aeration certainly will be caused like this to waste.
Summary of the invention
The object of the invention is, in order to overcome above-mentioned front defect, to provide a kind of carbon source that can improve activity of activated sludge, anaerobic treatment, and secondary pollution, the activated sludge treatment method of lower-cost waste water and treatment system can not be caused.
To achieve these goals, on the one hand, the invention provides a kind of activated sludge treatment method of waste water, the method comprises the following steps: (1) is under anaerobic treatment condition, waste water is contacted with the material containing active sludge, carries out the anaerobic treatment of waste water; (2) mixture of gained after contact is carried out aerobic treatment; (3) mixture after part aerobic treatment is returned step (1) as the described material containing active sludge of part, wherein, the described particle diameter containing the active sludge of in the material of active sludge at least 60 % by weight is not more than 1mm, is preferably 0.5-1mm.
Preferably, be back in the process of step (1) by the mixture after described part aerobic treatment, eddy flow process is carried out to the mixture after described part aerobic treatment, make the particle diameter of the active sludge of in the mixture after being back to the described part aerobic treatment in step (1) at least 60 % by weight be not more than 1mm, described eddy flow process is carried out in swirler.More preferably, the velocity slope of mixture in swirler after the condition of described eddy flow process makes described part aerobic treatment is not less than 1100S
-1, be preferably 2800-5600S
-1.
Preferably, the method also comprises, in the process of carrying out aerobic treatment, pass into carbonic acid gas, and the intake of carbonic acid gas makes the volume ratio of carbonic acid gas and the oxygen passed into be 0.25-1:1.
On the other hand, present invention also offers a kind of active sludge processing system of waste water, wherein, this treatment system comprises; Anoxic unit, aerobic unit and sludge crushing unit, the outlet of described anoxic unit communicates with the import of described aerobic unit, an outlet of described aerobic unit communicates with the import of sludge crushing unit, and the outlet at bottom of described sludge crushing unit and the waste water inlet of described anoxic unit lead to.
Preferably, described sludge crushing unit is swirler.
Preferably, this system also comprises the carbonic acid gas feed unit communicated with described aerobic unit.
According to technique scheme of the present invention, 1mm is being not more than by the size controlling of the active sludge by least 60 % by weight in the mixture after the part aerobic treatment be back in step (1), be preferably in the scope of 0.5-1mm, the organic exposures such as the polysaccharide in mud and protein can be made to discharge, supplement the organic carbon source in anaerobic treatment with described mixture, improve the denitrification denitrogenation usefulness in anaerobic treatment process; And when preferably by eddy flow process, carry out fluid shearing, the little oil droplet of Sludge Surface is discharged further, and the activity of mud obtains and effectively improves, enhance the mass-transfer performance of sludge interface, facilitate hardly degraded organic substance degraded and nitrated usefulness in oily(waste)water.Therefore, the present invention does not need the aeration adding medicament and strengthening O pond, has running cost low, the advantage of no coupling product.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with embodiment one below.In the accompanying drawings:
Fig. 1 is the active sludge processing system of the waste water of a kind of embodiment of the present invention.
Fig. 2 is the active sludge processing system of the waste water of the another kind of embodiment of the present invention.
Fig. 3 is the swirler of a kind of embodiment of the present invention.
Description of reference numerals
1 anoxic unit 2 aerobic unit 3 sludge crushing unit 4 carbonic acid gas feed unit
5 reflux pumps
31 overflow ports
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the following description of the present invention, the term " hydraulic detention time " used refers to the mean residence time of pending waste water in reactor, the namely average reaction time of microbial process in waste water and reactor, therefore, if the useful volume of reactor is V (m
3), flow velocity is Q (m
3/ h), then: hydraulic detention time (HRT)=V/Q, namely hydraulic detention time equals the ratio of reactor useful volume and flow velocity.
Anaerobic treatment is the stage that anti-nitration reaction mainly occurs, and anti-nitration reaction refers under anoxic condition, and the nitrite nitrogen in waste water, nitrate nitrogen are reduced into gaseous nitrogen (N by denitrifying bacteria
2) process.Denitrifying bacteria is heterotroph microorganism, belongs to facultative bacteria more, when anoxic condition, utilizes oxygen in nitrate as electron acceptor(EA), using organism (the BOD composition in sewage) as electron donor, provides energy and oxidized stable.
Aerobic treatment is the stage that nitration reaction mainly occurs, and nitration reaction refers under aerobic state, and nitrococcus utilizes inorganic carbon for carbon source is by NH
4 +change into nitrite (NO
2 -), then nitrite-oxidizing is nitrate (NO by nitrifier
3 -) process.
Denitrifying bacteria, nitrococcus and nitrifier are the conventional microorganism existed in the active sludge for purification of water quality, do not repeat them here.
" COD " i.e. chemical oxygen demand (COD), it is the index representing that in water, reducing substances is how many, COD value is larger, and illustrate that water body is more serious by organic pollution, all COD value related in the present invention are the numerical value that potassium dichromate oxidation (GB11914-89) records.
" ammonia-nitrogen content " refers to the amount of the nitrogen existed with free ammonia and ammonium ion form in every premium on currency, is abbreviated as NH
4 +-N.
" total nitrogen level ", in the nitrogenous milligram number of every premium on currency, is abbreviated as TN.
When " velocity slope " refers to that fluid flows between two interfaces, due to the existence of frictional force between material, make the velocity of flow generation difference of velocity slope internal fluid and fluid and velocity slope interface contacts, produce the velocity field of a gradual change, be called velocity slope, or claim cutting speed rate, shearing rate.
On the one hand, the invention provides a kind of activated sludge treatment method of waste water, the method comprises the following steps: (1), under anaerobic treatment condition, makes waste water contact with the material containing active sludge, carries out the anaerobic treatment of waste water; (2) mixture of gained after contact is carried out aerobic treatment; (3) mixture after part aerobic treatment is returned step (1) as the described material containing active sludge of part, wherein, the particle diameter being back to the active sludge of at least 60 % by weight in the mixture after the described part aerobic treatment in step (1) is not more than 1mm, is preferably 0.5-1mm.
Hereinafter, " mixture after the described part aerobic treatment in step (1) will be back to " unified referred to as " phegma ".
The present inventor finds, fragmentation is carried out to the active sludge in described phegma, and make the particle diameter of the active sludge of wherein at least 60 % by weight be not more than 1mm, be preferably 0.5-1mm, effectively can discharge the organic matter such as exocytosis polysaccharide and protein in mud, and recycle in A pond as organic carbon source.In addition, removing of the oil phase that the fragmentation of mud is also wrapped up along with mud, activity after the de-oiling flora that dissociates can again form high reactivity mud in the biological treatment process of A pond to O pond, with the biochemical activity of consolidation system, can effectively at mud Sources decreasing, and accelerating system biochemical activity, thus complete the present invention.
According to the present invention, in the preferred case, the described particle diameter containing active sludge whole in the material of active sludge is not more than 2mm.
Although by described phegma at least 60 % by weight the size controlling of active sludge be not more than 1mm, be preferably 0.5-1mm and can realize object of the present invention.But the present inventor finds, made the particle diameter of the active sludge of in described phegma at least 60 % by weight be not more than 1mm by eddy flow process, be preferably 0.5-1mm, also be, mixture after described part aerobic treatment is back in the process of step (1), eddy flow process is carried out to the mixture after described part aerobic treatment, make the particle diameter of the active sludge of in the mixture after being back to the described part aerobic treatment in step (1) at least 60 % by weight be not more than 1mm, the performance of mud can be made to be further enhanced.Described eddy flow process is preferably carried out in swirler, and in order to realize above-mentioned requirements, the condition of described eddy flow process makes the velocity slope of described mixture in swirler preferably be not less than 1100S
-1, be more preferably 2800-5600S
-1.
Although the velocity slope of the described mixture in swirler is controlled can effectively realize goal of the invention of the present invention within the scope of the invention.But the present inventor finds, by the condition of eddy flow process is carried out following control, exocytosis in mud in treated mixture can more effectively discharge, and more contributes to the thalline that active sludge discharges and again form highly active mud flco.The condition optimization of described eddy flow process comprises: with the intake port of described swirler for 0.02-0.04m is for benchmark, and the charging flow velocity of swirler is 1-8m/s, and opening for feed pressure is not less than 0.03MPa; The opening for feed pressure of described swirler is greater than discharge port pressure, and pressure difference is 0.03-0.15MPa.The present invention need it is noted that, the intake port of described swirler increases, and the input speed of described phegma will reduce, pressure will reduce.
According to the present invention, described phegma carries out, in the process processed, also comprising and carrying out overflow to described phegma in swirler, and the flow of described overflow is the 2-5 volume % of described phegma feed rate.By controlling the flow of described overflow, effectively can ensure the velocity slope of described phegma in swirler, thus make the particle diameter of the active sludge of in described phegma at least 60 % by weight be not more than 1mm, be preferably 0.5-1mm.
According to the present invention, the tiny oil droplets that described method comes off after also comprising the process of removing eddy flow, to realize the separation of profit, thus reduces the oil-contg of water outlet.According to method of the present invention, the tiny oil droplets come off can in swirler under Strong shear stress with aqueous phase separation, thus can to discharge from the overflow port of swirler.It should be noted that herein, when described phegma is containing Chuck Steak, needs to collect separately the overflowing liquid of discharging from overflow port, be back in step (1) after oil removing again; When described phegma oil-containing is less, the overflowing liquid of discharging from overflow port can directly be back to step (1).
The present inventor also finds, by passing into carbonic acid gas in the process of aerobic treatment, and the intake controlling carbonic acid gas makes the volume ratio of carbonic acid gas and the oxygen passed into be 0.25-1:1, preferred 0.5-1:1, can reduce the content of the amino nitrogen of the waste water after process, nitrate and total nitrogen further.Wherein, the carbonic acid gas in the volume ratio of described oxygen and carbonic acid gas only refers to the amount of the carbonic acid gas additionally passed into.Wherein, oxygen and passing into of carbonic acid gas can adopt method well known in the art to carry out, and the present invention does not repeat them here.
Although method of the present invention can be applicable to various waste water, the present inventor finds, it is 400-2500mg/L, NH that method of the present invention is specially adapted to COD value
4 +-N (amino nitrogen) content is 30-250mg/L, NO
3 --N (nitrate) content is 0-15mg/L, be preferably 8-12mg/L, the content of total nitrogen is 50-350mg/L, the content of petroleum substance is 100-1500mg/L, the content of suspended substance (SS) is 150-600mg/L, the content of sulfide is 15-25mg/L, and the waste water that basicity (with calcium carbonate) is 150-300mg/L processes.More preferably, method of the present invention is particularly useful for the electric desalting waste water that refinery discharges, brine waste, the oily(waste)water of refinery discharge and the treatment of wastewater from stripping of refinery discharge that refinery discharges, more preferably, described waste water is the oily(waste)water of refinery discharge.
The COD value of electric desalting waste water is 1500-2500mg/L, NH
4 +-N is 60-100mg/L, NO
3 --N is 0-10mg/L, be preferably 8-12mg/L, the content of total nitrogen is 100-200mg/L, the content of petroleum substance is 800-1500mg/L, the content of suspended substance (SS) is 200-400mg/L, the content of sulfide is 15-25mg/L, and basicity (with calcium carbonate) is 150-300mg/L, and pH value is 7.5-9.5.
The COD value of brine waste is 500-800mg/L, NH
4 +-N is 50-100mg/L, NO
3 --N is 0-10mg/L, be preferably 8-12mg/L, the content of total nitrogen is 50-150mg/L, the content of petroleum substance is 800-1500mg/L, the content of SS is 300-600mg/L, the content of sulfide is 15-25mg/L, and basicity (with calcium carbonate) is 200-300mg/L, and pH value is 7.5-9.5.
The COD value of oily(waste)water is 600-1000mg/L, NH
4 +-N is 30-80mg/L, NO
3 --N is 0-10mg/L, be preferably 8-12mg/L, the content of total nitrogen is 50-350mg/L, the content of petroleum substance is 300-500mg/L, the content of SS is 150-250mg/L, the content of sulfide is 15-25mg/L, and basicity (with calcium carbonate) is 200-300mg/L, and pH value is 7.5-9.5.
The COD value for the treatment of of wastewater from stripping is 1200-1800mg/L, NH
4 +-N is 150-250mg/L, NO
3 --N is 0-10mg/L, be preferably 8-12mg/L, the content of total nitrogen is 200-350mg/L, the content of petroleum substance is 100-200mg/L, the content of SS is 150-250mg/L, the content of sulfide is 15-25mg/L, and basicity (with calcium carbonate) is 200-300mg/L, and pH value is 7.5-9.5.
Wherein, term " petroleum substance " refers to the hydrocarbon polymers such as alkane, aromatic hydrocarbons, bituminous matter, colloid.
According to the present invention, in hypoxic/anaerobic technique, when the ratio of carrying out the flow of the raw wastewater of anaerobic treatment in the flow returning the described phegma in step (1) and step (1) is 2-4, by refluxing, broken mud flco can remarkable decrement discharge mud.Return the ratio carrying out the flow of the raw wastewater of anaerobic treatment in the flow of the mixture after the described part aerobic treatment in step (1) and step (1) to be referred to as " internal reflux ratio " or " return current ratio of the mixed liquid ".Wherein, described " raw wastewater " is the waste water carrying out anaerobic treatment at first.
In the present invention, the condition of anaerobic treatment and aerobic treatment can be the condition that this area routine adopts, the condition optimization of described anaerobic treatment comprises: dissolved oxygen is no more than 1mg/L (as 0.5-1mg/L), and temperature is 10-40 DEG C, and hydraulic detention time is 2-6h.The condition optimization of described aerobic treatment comprises: dissolved oxygen is 2-4mg/L, and temperature is 10-40 DEG C, and hydraulic detention time is 8-16h.
In the present invention, anaerobic treatment and aerobic treatment series connection are carried out, and to the not special requirement of its concrete series system, such as, can be the series system of anaerobic-aerobic.As required, the strict anaerobic treatment (dissolved oxygen is 0) controlling dissolved oxygen can also be set before anaerobic treatment and aerobic treatment.It is 10-40 DEG C that the condition of anaerobic treatment generally includes temperature, and hydraulic detention time is 2-6h.
In the present invention, the active sludge that this area routine can be used to use carries out biological denitrificaion, and under preferable case, the sludge loading of the active sludge that anaerobic treatment and/or aerobic treatment use is 0.15-0.5kgCOD/ (kg mud d).
In order to make full use of described active sludge, the present invention also comprises the mixture after by remaining part aerobic treatment and carries out solid-liquid separation, and active sludge solid-liquid separation obtained returns step (1) to add in whole treatment system to make sludge concentration balance.Concrete being operating as is conventionally known to one of skill in the art, and the present invention does not repeat them here.
In order to improve effluent characteristics further, waste water is first carried out homogeneous and dissolved air flotation before can also being included in and entering aerobic treatment and anaerobic treatment by method of the present invention.Described homogeneous realizes by stirring usually, and the condition of dissolved air flotation generally includes: relative to 1000m
3pending waste water, the flow of the gas passed into is preferably 200-400m
3/ h, temperature is 0-40 DEG C, and the time is 0.5-1.0h.
Second aspect, as shown in Figure 1, the invention provides a kind of active sludge processing system of waste water, and wherein, this treatment system comprises; Anoxic unit 1, aerobic unit 2 and sludge crushing unit 3, the outlet of described anoxic unit 1 communicates with the import of described aerobic unit 2, an outlet of described aerobic unit 2 communicates with the import of sludge crushing unit 3, and the outlet at bottom of described sludge crushing unit 3 and the waste water inlet of described anoxic unit 1 lead to.
Preferably, described sludge crushing unit 3 is swirler.
According to one of the present invention preferred embodiment, for the ease of the backflow of phegma, described system is also included between sludge crushing unit 3 and aerobic unit 2 and arranges reflux pump 5, to ensure that described mixture can successfully and enter sludge crushing unit 3 according to the flow velocity of predetermined amount and flow.
In the present invention, for the mode of connection between above each parts, there is no particular limitation, can be the various connections of this area routine, such as, be connected by pipeline.
As shown in Figure 3, according to one of the present invention preferred embodiment, for the ease of processing the material after eddy flow, described swirler is except import and outlet, overflow port 31 is also provided with on its top, for the overflow of phegma, thus effectively control the velocity slope of phegma in swirler.
According to the present invention, according to the amount of the material of the backflow of actual treatment, described swirler 3 can be set to the multiple of parallel connection, described mixture is processed simultaneously, number those skilled in the art of described swirler can select according to practical situation, such as, according to the flow of return flow divided by single swirler, actual swirler number can be obtained.
In addition, according to mud particle diameter in phegma in eddy flow process at below 1mm, the ratio of preferred 0.5-1mm, can also arrange circulation line between swirler 3 and anoxic unit 1, repeatedly flows through sludge crushing unit 3 carry out eddy flow process to realize phegma.
As shown in Figure 2, according to another preferred embodiment of the present invention, described system also comprises the carbonic acid gas feed unit 4 communicated with aerobic unit.
According to the present invention, described carbonic acid gas feed unit is preferably device for producing hydrogen.By being connected with device for producing hydrogen, the gas that device for producing hydrogen is arranged can be supplied to aerobic unit 2 outward by carbonic acid gas ventpipe.Thus recycled the gas that hydrogen manufacturing is arranged outward, be conducive to the protection of atmospheric environment.
According to the present invention, described system can also comprise the homogeneous unit and air supporting separating unit that set gradually to realize homogeneous and the dissolved air flotation of waste water, and described homogeneous unit and air supporting separating unit are set in turn in the anoxic unit 1 and aerobic unit 2 upstream of connecting successively.
According to the particularly preferred embodiment of the present invention, when reality uses, waste water flows through homogeneous unit, dissolved air flotation unit, anoxic unit and aerobic unit successively, and carry out subsequent disposal, wherein, preferably, the gas arranged outward by device for producing hydrogen by carbonic acid gas ventpipe supply aerobic unit, thus carries out active sludge treatment to waste water.
Below will be described the present invention by embodiment.In following examples,
The measuring method of COD value is dichromate titration (GB11914-89);
The measuring method of ammonia-nitrogen content (NH4+-N) is Berthelot spectrophotometry (HJ535-2009);
The measuring method of total nitrogen level (NO3--N) is that alkaline chitinase clears up ultraviolet spectrophotometry (HJ636-2012);
The measuring method of petroleum content is infrared spectrophotometry (HJ637-2012), and the measuring method of SS content is weighting method (GB11901-89);
The measuring method of sulfide content is the spectrophotometry (GB/T17133-1997) that directly develops the color;
The measuring method of basicity is volumetry (GB/T15451-95);
In swirler, the velocity slope of phegma is measured by U.S. YSIFlowTracker doppler velocimeter;
The particle diameter of active sludge measures (MalvemMastersizer2000, Malvem, UK) by Malvem laser particle instrument and measures;
The inlet diameter of swirler is 0.02m.
The water quality of the waste water used in embodiment is as shown in table 1.
Table 1
Embodiment 1-4
Adopt the device shown in Fig. 1, respectively active sludge treatment (comprising anaerobic treatment and aerobic treatment) is carried out to electric desalting waste water 1, brine waste 1, oily(waste)water 1 and treatment of wastewater from stripping 1, the method of described process is carried out according to " " Water Pollution Control Engineering " 342-344 page: Water Pollution Control Engineering; Wang Yu edits; Lin Fengkai associate editor; Chemical Industry Press, 2008 ".Unlike, the aerobic reflux pipeline returning anaerobism arranges swirler, the flow velocity of swirler opening for feed is 4-6m/s, feed pressure is 0.10-0.15MPa, the pressure difference of opening for feed and discharge port is 0.10-0.15MPa, the flow of the overflow port of swirler is 3.5 volume % of inlet flow rate, and mixture (phegma) velocity slope of eddy flow in swirler from aerobic treatment is 4000S
-1.After eddy flow, the particle diameter of active pollution index of 80 % by weight is 0.5-1mm, and the particle diameter of all active pollution index is no more than 2mm.Result is as shown in table 2.
Embodiment 5-8
Adopt the device shown in Fig. 1, respectively active sludge treatment (comprising anaerobic treatment and aerobic treatment) is carried out to electric desalting waste water 2, brine waste 2, oily(waste)water 2 and treatment of wastewater from stripping 2.The method of described process is carried out according to " " Water Pollution Control Engineering " 342-344 page: Water Pollution Control Engineering, Wang Yu edits, Lin Fengkai associate editor, Chemical Industry Press, 2008 ".Unlike, the aerobic reflux pipeline returning anaerobism arranges swirler, the flow velocity of swirler opening for feed is 1-4m/s, feed pressure is 0.03-0.06MPa, the pressure difference of opening for feed and discharge port is 0.06MPa, the flow of the overflow port of swirler is 2 volume % of inlet flow rate, and mixture (phegma) velocity slope of eddy flow in swirler from aerobic treatment is 2800S
-1.After eddy flow, the particle diameter of active pollution index of 60 % by weight is 0.5-1mm, and the particle diameter of all active pollution index is no more than 2mm.Result is as shown in table 2.
Embodiment 9-12
Adopt the device shown in Fig. 1, respectively active sludge treatment (comprising anaerobic treatment and aerobic treatment) is carried out to electric desalting waste water 3, brine waste 3, oily(waste)water 3 and treatment of wastewater from stripping 3.The method of described process is carried out according to " " Water Pollution Control Engineering " 342-344 page: Water Pollution Control Engineering, Wang Yu edits, Lin Fengkai associate editor, Chemical Industry Press, 2008 ".Unlike, the aerobic reflux pipeline returning anaerobism arranges swirler, the flow velocity of swirler opening for feed is 6-8m/s, feed pressure is 0.08-0.10MPa, the pressure difference of opening for feed and discharge port is 0.10MPa, the flow of the overflow port of swirler is 5 volume % of inlet flow rate, and the velocity slope from mixture eddy flow in swirler of aerobic treatment is 5600S
-1.After eddy flow, the particle diameter of active pollution index of 90 % by weight is 0.5-1mm, and the particle diameter of all active pollution index is no more than 2mm.Result is as shown in table 2.
Embodiment 13-15
Method according to embodiment 3 processes oily(waste)water 1, unlike, process in the device shown in Fig. 2, also be, in the process of aerobic treatment, in aerobic unit, pass into carbonic acid gas, the amount of the carbonic acid gas passed into makes the volume of carbonic acid gas and oxygen be respectively 0.8:1,0.5:1 and 1:1.
Comparative example 1-4
Biological denitrificaion is carried out respectively according to the method for embodiment 1-4, unlike, the aerobic reflux pipeline returning anaerobism does not arrange swirler, but is directly back to anaerobism workshop section.Result is as shown in table 2.
Table 2
As can be seen from Table 2, adopt technical scheme of the present invention, by by phegma at least 60 % by weight the size controlling of active sludge at 0.5-1mm, when the particle diameter of all active pollution index is no more than 2mm, the CER of mud can reach 60 volume %, and waste water have also been obtained and effectively processes.When preferred pass into carbonic acid gas to aerobic treatment, the content of the amino nitrogen of the waste water after process, nitrate and total nitrogen can be reduced further.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (13)
1. an activated sludge treatment method for waste water, the method comprises the following steps:
(1) under anaerobic treatment condition, waste water is contacted with the material containing active sludge, carries out the anaerobic treatment of waste water;
(2) mixture of gained after contact is carried out aerobic treatment;
(3) mixture after part aerobic treatment is returned step (1) as the described material containing active sludge of part;
Wherein, the particle diameter being back to the active sludge of at least 60 % by weight in the mixture after the described part aerobic treatment in step (1) is not more than 1mm.
2. method according to claim 1, wherein, the described particle diameter containing active sludge in the material of active sludge is not more than 2mm.
3. method according to claim 1, wherein, be back in the process of step (1) by the mixture after described part aerobic treatment, eddy flow process is carried out to the mixture after described part aerobic treatment, make the particle diameter of the active sludge of in the mixture after being back to the described part aerobic treatment in step (1) at least 60 % by weight be not more than 1mm, described eddy flow process is carried out in swirler.
4. method according to claim 3, wherein, the velocity slope of mixture in swirler after the condition of described eddy flow process makes described part aerobic treatment is not less than 1100S
-1, be preferably 2800-5600S
-1.
5. the method according to claim 3 or 4, wherein, the condition of described eddy flow process comprises: with the intake port of described swirler for 0.02-0.04m is for benchmark, and the charging flow velocity of swirler is 1-8m/s, opening for feed pressure is not less than 0.03MPa, is preferably 0.03-0.15MPa; The opening for feed pressure of described swirler is greater than discharge port pressure, and pressure difference is 0.03-0.15MPa.
6. method according to claim 3, wherein, the method also comprises: the mixture after described part aerobic treatment carries out in the process processed in swirler, carry out overflow to the mixture after described part aerobic treatment, the flow of described overflow is the 2-5 volume % of the mixture feed rate after described part aerobic treatment.
7. method according to claim 1, wherein, the method also comprises, and the mixture after remainder aerobic treatment is carried out solid-liquid separation, and active sludge solid-liquid separation obtained returns step (1) as the material containing active sludge described in another part.
8. method according to claim 1, wherein, the COD value of described waste water is 400-2500mg/L, NH
4 +-N content is 30-250mg/L, NO
3 --N content is 0-15mg/L, and the content of total nitrogen is 50-350mg/L, and the content of petroleum substance is 100-1500mg/L, and the content of suspended substance is 150-600mg/L, and the content of sulfide is 15-25mg/L, with the basicity of calcium carbonate for 150-300mg/L; Preferably, described waste water is the oily(waste)water from refinery.
9. method according to claim 1, wherein, being back to the ratio of carrying out the flow of the waste water of anaerobic treatment in the flow of the mixture after the described part aerobic treatment in step (1) and step (1) is 2-4.
10. method according to claim 1, wherein, the method also comprises, in the process of carrying out aerobic treatment, pass into carbonic acid gas, and the intake of carbonic acid gas makes the volume ratio of carbonic acid gas and the oxygen passed into be 0.25-1:1.
The active sludge processing system of 11. 1 kinds of waste water, is characterized in that, this treatment system comprises; Anoxic unit (1), aerobic unit (2) and sludge crushing unit (3), the outlet of described anoxic unit (1) communicates with the import of described aerobic unit (2), an outlet of described aerobic unit (2) communicates with the import of sludge crushing unit (3), and the outlet at bottom of described sludge crushing unit (3) and the waste water inlet of described anoxic unit (1) lead to.
12. treatment systems according to claim 11, wherein, described sludge crushing unit (3) is swirler, and the top of described swirler is provided with overflow port (31).
13. treatment systems according to claim 11, wherein, this system also comprises the carbonic acid gas feed unit (4) communicated with described aerobic unit (2).
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| CN106365314A (en) * | 2015-07-23 | 2017-02-01 | 中国石油化工股份有限公司 | Method and system for carrying out biological denitrification on waste water, and applications of system |
| CN106396271A (en) * | 2016-10-27 | 2017-02-15 | 环境保护部华南环境科学研究所 | Method for improving settling property of activated sludge |
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Inventor after: Chen Xiurong Inventor after: Liu Yi Inventor after: Yang Xuejing Inventor after: Shi Junlin Inventor after: Yu Shuilong Inventor after: Yu Huiqing Inventor before: Chen Xiurong Inventor before: Wang Hualin Inventor before: Liu Yi Inventor before: Yang Xuejing Inventor before: Shi Junlin Inventor before: Yu Shuilong Inventor before: Yu Huiqing |