CN105293826B - A kind of efficient desulfurizing denitrification method of devulcanization Anammox - Google Patents
A kind of efficient desulfurizing denitrification method of devulcanization Anammox Download PDFInfo
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Abstract
The invention discloses a kind of efficient desulfurizing denitrification method of devulcanization Anammox, this method is simple, efficient, while investment and operating cost are relatively low.The method of the present invention comprises the following steps：The first step, raw water enters AnV reactors and carries out devulcanization and aminating reaction, and by AnV reactor outlet water at tail end partial reflux to water inlet end, is mixed raw water and AnV reactors recirculation water by water quality blender；Second step, the water outlet that AnV reactors are not flowed back adds desulfurizing agent by tubular static mixer, AnV reactors is gone out Sulfide in water and is sufficiently mixed with desulfurizing agent；3rd step, through entering EAO ponds with the waste water after desulphurizer mixing, carries out flocculation reaction；The water outlet of EAO ponds is divided into two strands, one enters NNIT ponds and carries out nitrosation reaction；4th step, REGSB reactors are introduced by another burst of water outlet of EAO ponds water outlet together with the water outlet in NNIT ponds.
Description
Technical field
The present invention relates to a kind of desulfurizing denitrification method, and in particular to a kind of efficient desulfurizing denitrification side of devulcanization Anammox
Method.
Background technology
Along with industrial expansion, many production fields have all been emerged substantial amounts of to be contained containing high concentration sulfate and high concentration
The industrial wastewater of sulphur, itrogenous organic substance, such as Gourmet Powder Factory, pharmaceutical factory, printing and dyeing mill, molasses-spirit factory.Due to most sulfuric acid
Solubility of the salt in water is very big, and property is stable in nature, so simple dependence self cleaning is difficult to get rid of.
The influence of any discharge of sewage containing high concentration sulfate in a short time to natural water and ecological environment is little, but sulfuric acid
Once salt pollution large area is formed, improvement is suitable difficult.The underground water in many cities of current China has been received
Different degrees of sulfate contamination, the problem of paying attention to and study improvement sulfate contamination is extremely urgent.
Begin to use homogenous anaerobic PROCESS FOR TREATMENT high concentration sulfate wastewater both at home and abroad from 1970s.But
It is that the successful example of reactor operation is seldom.Because in anaerobic technique, when the sulfate containing high concentration in waste water
When, anaerobic digestion process will be had adverse effect on.It is summarized as following two aspects：One is due to SRB (sulfate reductions
Bacterium) and MPB (methanogen) may be by acetic acid and H2And the substrate competition inhibitory action produced；Two be sulfate reduction
End-product --- the toxic action that sulfide is directly produced to methanogen and other anaerobic bacterias.
At present, for the sulfate containing high concentration waste water enter Anaerobic Treatment before will pre-process reduction sulfate it is dense
Degree, current treatment technology has physico-chemical process and biochemical process.Physico-chemical process is exactly that sulfate radical reacts with calcium ion to be produced by feeding lime
Gypsum is precipitated, to reach sulfate radical purpose.Biochemical process, which is mainly, is converted the sulfate radical in waste water by cultivating SRB
Out.Physico-chemical process processing is needed to add substantial amounts of lime, and substantial amounts of chemical sludge-gypsum tailings is produced accordingly, can increase solid waste
Processing cost.And biochemical process processing operating cost it is relatively low, but produce tail gas in hydrogen sulfide need to handle after can arrange
Put, generally by alkali liquor absorption or low-level oxidation (be passed through air, or low concentration the oxidant such as pure oxygen), bioanalysis is added at tail gas
The link of reason, and then increase processing infrastructure investment and operating cost.Due to the deficiency of the presence of bioanalysis, occur in that some are improved
Desulfurization process, such as patent publication No. be the B of CN 102351366 " devulcanization of synchronous biological denitrification and denitrification of autotrophic organism
The device and technology of Pharmaceutical Wastewater Treatment ", it is proposed that carry out devulcanization while Anaerobic Treatment, but unresolved SRB and MPB it
Between substrate competition problem.Such as " integrated printing and dyeing waste water treatment process " that patent publication No. is the B of CN 101164923, it is proposed that
Fe is directly added in anaerobic pond2+, the S produced to devulcanization2+Precipitated, this technology, which have ignored, adds Fe in anaerobic pond2+No
The salinity of anaerobic pond is increase only, while will also result in Fe2+Have a negative impact to normal anaerobic methanogens.
It can be seen that, it is not enough due to understanding sulfur-bearing chemical industry, pharmacy waste water water quality and biochemical treatment process microbial action mechanism
Or it is not given to move to chemical industry after enough attention, the handling process simple superposition by municipal sewage of blindness, at pharmacy waste water
In science and engineering skill, not only processing cost is expensive, and has a strong impact on follow-up materialization and biochemical treatment.Existing sulfur-bearing chemical industry, system
Medicine wastewater processing technology is typically first only to consider to detest without well by anaerobism devulcanization, denitrification and the devulcanization coordinating and unifying
Oxygen devulcanization denitrification, as a result causes in sewage that sulphates content is higher, has a strong impact on the normal fortune of follow-up REGSB reactors
OK.Exploitation be adapted to sulfur-bearing chemical industry, pharmacy waste water water quality characteristicses, efficiently collaboration depth remove the biochemical technology of removing sulfate, be whole
Cover sulfur-bearing chemical industry, the key of pharmaceutical wastewater treatment process efficient stable operation.In addition in high-sulfur, high ammonia nitrogen, high COD industrial wastewaters
In processing, the purpose of devulcanization is prevented under conditions of anaerobism, and sulfide generation, which has suppression to acid-producing bacteria and MPB and poisoned, to be made
Hydrogen sulfide, thioether, mercaptan.Secondly, devulcanization is carried out prior to ammonification and carburizing reagent, and is carbonized and is pressed down substantially
Make, in a dormant state.Therefore need research and development one kind can significantly, while reach desulfurizing denitrification, the pretreatment for reducing COD is made
New technology, to ensure the normal operation of follow-up aerobic treatment.
The content of the invention
For deficiencies of the prior art, it is acidified that the present invention solves chemical industry, pharmacy sulfur-containing waste water devulcanization
There is provided a kind of devulcanization Anammox is efficient for the problem of sulfate influence anaerobic digestion produced in journey is removed with sulfate hardly possible
Desulfurizing denitrification method, this method is simple, efficient, while investment and operating cost are relatively low.
The technical solution adopted in the present invention is as follows：
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, it comprises the following steps：
The first step, raw water enter AnV reactors (i.e. devulcanization ammoniation reactor, also abbreviation AnV ponds) carry out devulcanization with
Aminating reaction, and by AnV reactor outlet water at tail end partial reflux to water inlet end, reacted raw water and AnV by water quality blender
Device recirculation water is mixed；Wherein AnV structure of reactor is many gallery plug flow reactors, is fixed in AnV reactors using suspending
SRB (i.e. sulfate reducing bacteria) is planted and fixed by bed process, it is ensured that the residence time of SRB kinds is more than its generation time；
Second step, the water outlet that AnV reactors are not flowed back adds desulfurizing agent by tubular static mixer, reacts AnV
Device goes out Sulfide in water and is sufficiently mixed with desulfurizing agent, AnV reactors is gone out Sulfide in water and desulfurizing agent formation S2-Salt is precipitated；
3rd step, through entering EAO ponds (i.e. advanced oxidation depositing reservoir) with the waste water after desulphurizer mixing, progress is flocculated anti-
Should；The water outlet of EAO ponds is divided into two strands, one enters NNIT ponds (i.e. nitrosation reactor) and carries out nitrosation reaction；
4th step, introduces REGSB reactors by another burst of water outlet of EAO ponds water outlet together with the water outlet in NNIT ponds and (changes
Type is anaerobic expanded granular sludge bed), Anammox reaction denitrogenation is carried out in REGSB reactors, while carrying out carburizing reagent；
NNIT ponds effluent recycling device is set in addition, and reflux ratio is：50%~2000%.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme is described takes off
Sulphur agent is FeSO4、FeCl2Or FeSO4And FeCl2Mixture, wherein the sulphur added takes off agent and sulphur i.e. S in AnV reactor water outlets2-
Mol ratio be (1~4)：1.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be the
The hydraulic detention time of AnV reactors described in one step is 8h~20h, and water temperature control is at 30 DEG C~65 DEG C, and pH value control exists
Between 6.5~7.5.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be the
AnV reactor outlet water at tail end partial reflux described in one step and the ratio not flowed back are 100%~1800%, many gallery pulling flow types
The ratio between its width of corridor of reactor and the depth of water are 1：(1~3), return current ratio of the mixed liquid is 100%~1800%, and setting is pushed away under water
Enter device, power mixing intensity is controlled in 4~12w/m3。
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be the
Use floating stuffing fixed bed described in one step uses high density polyethylene (HDPE) material, and density is 0.95-0.98g/cm2, space
Rate is 95%, to fix sulfate reducing bacteria, while adding iron plate and reduced iron powder in suspension condiment.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be institute
The EAO ponds stated are the concentric structure of outer shroud inner circle, and outer shroud is water distribution, hybrid reaction area, and inner circle is depositing separation area；Outer shroud is set
Impeller under water is equipped with, the rotating speed of impeller is 16-120rpm, and depositing separation area sets the swinging swash plate of adjustable angle, tiltedly
Plate angle degree adjusting range is -60 °~60 °, is respectively 10 × 10 in the GT values of each a quarter circulation journey of water (flow) direction4~8
×104、8×104~5 × 104、4×104~1 × 104、0.01×104~0.1 × 104, wherein G is velocity gradient, when T is
Between；The sludge part that EAO dams in pond is back to devulcanization AnV reactor origin or beginnings, partly drains into sludge condensation as excess sludge
Pond.Further technical scheme is to set length to be the 1/8~1/4 of inner circle width firing angle on the outside of the outer shroud in described EAO ponds, wide
The mixing pit for 0.8m~1.8m is spent, described mixing pit is hybrid for vertical crossing type baffling, mixing pit hydraulic detention time
For 5min~15min, flow velocity is 0.2m/s~0.6m/s；And divergent contour centrum knot is set at mixing pit entrance 1.5m~5m
Structure, to form jet, improves the gradient of current, strengthens mixed effect；Divergent contour vertebral body structure diameter at butt end is 0.5~1.7m,
Top diameter is 0.2m~0.5m.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be institute
Floating stuffing fixed bed is set in the NNIT ponds stated, and to fix Nitrosomas, wherein temperature control is in 14 DEG C~38 DEG C, pH value control
System is 7.2~8.8, and dissolved oxygen is controlled in 0~2.0mg/L.
The efficient desulfurizing denitrification method of devulcanization Anammox of the present invention, its further technical scheme can also be institute
The REGSB reactors stated are shading closed reactor, and the ammonia nitrogen loading in REGSB ponds is 7.5~20kg N m-3d-1；Temperature control
At 23 DEG C~45 DEG C；PH value control 6.7~8.6；Absolute anaerobic environment, when starting to start, first exposes nitrogen or argon gas deoxygenation,
When dissolved oxygen content is less than 0.05mg/L, stop deoxygenation；And water inlet nitrite and REGSB inside reactors ammonia density and
Nitrite concentration is below 1000mg/L；Phosphate concn is less than 2500mg/L.
In the present invention：AnV reactors are devulcanization ammoniation reactor, mainly carry out devulcanization and ammonification to waste water；EAO ponds
For advanced oxidation depositing reservoir, mainly make to remove sulfate devulcanization before anaerobic biological system is entered；REGSB reactors are to change
Type anaerobic expanded granular sludge bed reactor；NNIT ponds are nitrosation reactor.
Beneficial effects of the present invention are as follows：
1st, the present invention sets up two independent reactors, by the control of distinctive structure of reactor and service condition, protects
Demonstrate,prove two major class population bacteriums and optimal growth conditions is obtained in respective reactor, whole system is reached higher processing
Power and operation stability.AnV reactors ensure that SRB is dominant bacteria in pre- devulcanization pond, and environmental oxidation reduction potential must be low
Sulfate in -100mV, efficient reducing waste water, is sulfide by its devulcanization.By adding desulfurizing agent formation S2-Salt sinks
Form sediment, core reaction is S2-S is generated with reactive desulfurizing agent2-Reactant salt, while reduction sulfate and sulfide, it is ensured that follow-up raw
The stabilization of change system, efficiently run.
2nd, acid fermentation bacterium can restrain oneself higher sulfide concentration than MPB, so acid fermentation effect can be with sulfate
Reduction is carried out simultaneously, does not interfere with acid process.
3rd, in high-sulfur, high ammonia nitrogen, high COD Industrial Wastewater Treatments, the purpose of devulcanization is prevented under conditions of anaerobism,
Sulfide generation has hydrogen sulfide, thioether, the mercaptan of suppression and toxic action to acid-producing bacteria and methane backeria.Secondly, devulcanization is excellent
Carried out prior to ammonification and carburizing reagent, and be carbonized and be suppressed substantially, in a dormant state.In AnV reactors after first devulcanization
Ammonification, makes full use of the synergy of devulcanization and ammonification, is that desulfurizing denitrification is pre-processed in subsequent handling.Utilizing this hair
Bright technology significantly can reach desulfurizing denitrification simultaneously, reduce the interference that sulphur and nitrogen are degraded under anaerobic to high concentration COD
And inhibitory action, it is ensured that the efficiency and effect of follow-up aerobic treatment.
4th, nitrosation reaction is carried out in NNIT ponds, by nitrification control in Nitrification Stage, therefore 64% or so can be reduced
Aeration quantity, save power consumption.Simultaneously because the shortening in reaction time, it is possible to reduce hydraulic detention time (HRT), and then subtract
The volume and floor space of few reactor.
5th, Anammox reaction is carried out in REGSB reactors and carries out denitrogenation, denitrogenation elimination capacity is far above routine
Denitrification process, it is adaptable to the denitrogenation pretreatment of industrial waste water with high ammoniac nitrogen.And because the cell yield of anaerobic ammonia oxidizing bacteria is relatively low,
Sludge yield is also far below nitrification-denitrification technique in whole reactor, and this will substantially reduce the processing and disposal of excess sludge
Cost.
6th, the precipitating reagent and desulfurizing agent selected by the devulcanization sulfur removal technology that the present invention is provided are commercially available material, and price is low
It is honest and clean, choose convenient, can directly buy.
7th, the SO that the sludge quantity that is produced during whole devulcanization is few, energy consumption is low, produce2- 4And S2O3 2-It is less, to vulcanization
Thing clearance is higher, reaction rate is fast, recyclable S2-Salt, avoid sulfate is discharged into environment.
8th, present invention is generally directed to the anaerobism sulphur removal of sulfur-bearing chemical industry, pharmacy waste water.
Brief description of the drawings
Accompanying drawing 1 is present invention process schematic flow sheet
Accompanying drawing 2 is AnV reactor floor map
Accompanying drawing 3 is EAO ponds floor map
Accompanying drawing 4 is EAO ponds profile A-A
Accompanying drawing 5 is EAO ponds profile B-B
Accompanying drawing 6 is EAO ponds profile C-C
Accompanying drawing 7 is NNIT ponds floor map
Embodiment
The present invention is described in further detail with reference to embodiment.
As shown in figs. 1-7, its specific method step is as follows in embodiment：
The first step, raw water enter AnV reactors (i.e. devulcanization ammoniation reactor, also abbreviation AnV ponds) carry out devulcanization with
Aminating reaction, and by AnV reactor outlet water at tail end partial reflux to water inlet end, reacted raw water and AnV by water quality blender
Device recirculation water is mixed；Wherein AnV structure of reactor is many gallery plug flow reactors, is fixed in AnV reactors using suspending
SRB (i.e. sulfate reducing bacteria) is planted and fixed by bed process, it is ensured that the residence time of SRB kinds is more than its generation time；
Second step, the water outlet that AnV reactors are not flowed back adds desulfurizing agent by tubular static mixer, reacts AnV
Device goes out Sulfide in water and is sufficiently mixed with desulfurizing agent, AnV reactors is gone out Sulfide in water and desulfurizing agent formation S2-Salt is precipitated；
3rd step, through entering EAO ponds (i.e. advanced oxidation depositing reservoir) with the waste water after desulphurizer mixing, progress is flocculated anti-
Should；The water outlet of EAO ponds is divided into two strands, one enters NNIT ponds (i.e. nitrosation reactor) and carries out nitrosation reaction；
4th step, introduces REGSB reactors by another burst of water outlet of EAO ponds water outlet together with the water outlet in NNIT ponds and (changes
Type is anaerobic expanded granular sludge bed), Anammox reaction denitrogenation is carried out in REGSB reactors, while carrying out carburizing reagent；
NNIT ponds effluent recycling device is set in addition, and reflux ratio is：50%~2000%.
Wherein described desulfurizing agent is FeSO4、FeCl2Or FeSO4And FeCl2Mixture, wherein the sulphur added take off agent with
Sulphur is S in AnV reactor water outlets2-Mol ratio be (1~4)：1；The hydraulic detention time of AnV reactors described in the first step
For 8h~20h, water temperature control is at 30 DEG C~65 DEG C, and pH value is controlled between 6.5~7.5；AnV reactors described in the first step
Outlet water at tail end partial reflux is 100%~1800%, many its width of corridor of gallery plug flow reactor and water with the ratio not flowed back
The ratio between deep is 1：(1~3), return current ratio of the mixed liquid is 100%~1800%, and sets underwater propeller, power mixing intensity control
System is in 4~12w/m3；Use floating stuffing fixed bed described in the first step uses high density polyethylene (HDPE) material, and density is
0.95-0.98g/cm2, voidage is 95%, to fix sulfate reducing bacteria, while adding iron plate and reduction in suspension condiment
Iron powder；Described EAO ponds are the concentric structure of outer shroud inner circle, and outer shroud is water distribution, hybrid reaction area, and inner circle separates for precipitation
Area；Outer shroud is provided with impeller under water, and the rotating speed of impeller is 16-120rpm, and depositing separation area sets the revolution of adjustable angle
Formula swash plate, swash plate angle adjusting range is -60 °~60 °, is respectively 10 in the GT values of each a quarter circulation journey of water (flow) direction
×104~8 × 104、8×104~5 × 104、4×104~1 × 104、0.01×104~0.1 × 104, wherein G is velocity gradient,
T is the time；The sludge part that EAO dams in pond is back to devulcanization AnV reactor origin or beginnings, partly drains into sludge as excess sludge
Concentration basin.It is the 1/8~1/4 of inner circle width firing angle that length is set on the outside of the outer shroud in described EAO ponds, and width is 0.8m~1.8m's
Mixing pit, described mixing pit is hybrid for vertical crossing type baffling, and mixing pit hydraulic detention time is 5min~15min, stream
Speed is 0.2m/s~0.6m/s；And set divergent contour vertebral body structure, to form jet, improve at mixing pit entrance 1.5m~5m
The gradient of current, strengthens mixed effect；Divergent contour vertebral body structure diameter at butt end be 0.5~1.7m, top diameter be 0.2m~
0.5m；Floating stuffing fixed bed is set in described NNIT ponds, and to fix Nitrosomas, wherein temperature control is 14 DEG C~38
DEG C, pH value control is 7.2~8.8, and dissolved oxygen is controlled in 0~2.0mg/L；Described REGSB reactors are shading confined reaction
Device, the ammonia nitrogen loading in REGSB ponds is 7.5~20kg N m-3d-1；Temperature control is at 23 DEG C~45 DEG C；PH value control 6.7~
8.6；Absolute anaerobic environment, when starting to start, first exposes nitrogen or argon gas deoxygenation, when dissolved oxygen content is less than 0.05mg/L
When, stop deoxygenation；And the ammonia density and nitrite concentration of water inlet nitrite and REGSB inside reactors are below
1000mg/L；Phosphate concn is less than 2500mg/L.
Embodiment 1：Acrylic ester wastewater is tested
The first step, simulates above-mentioned technique and is tested in the lab, and whether sulphur removal is to subsequently detesting for contrast for test objective
The influence of oxygen reaction.Test group technique is first progress devulcanization anaerobic reaction, then by precipitating sulphur removal, last anaerobic reactor is high
Effect removes COD；Control group technique removes COD using direct anaerobic reactor.Test water produces for Jiangsu acrylate factory
Waste water is used after dilution, and waste water quality is as follows：COD8000mg/L-9000mg/L, SO4 2-1500-2000mg/L, pH value 7-8.
Test group simulation process technique as shown in figure 1, by devulcanization pond, water quality blender, temperature control strengthen sulfate reducing bacteria reactor,
Tube mixer, EAO ponds and REGSB reactors composition.
Second step, test group and control group are tamed by Low loading start up, are continuously run through 80d, and load is improved constantly, right
Than COD removal effects after domestication.
3rd step, test group temperature control strengthens sulfate reducing bacteria reactor running temperature by water-bath thermal-stable 55
DEG C, pH is stable in 7-8, and sulfuric acid salt load is up to 4kg/ (m3D), sludge concentration is about 5500mg/L, desulfurizing agent dosage
5mg/L.Tube mixer desulfurizing agent dosage 1000mg/L.
After the completion of domestication, control group COD stable water outlets are in 5600-6400mg/L, and clearance is 29%-38%；Test group
Temperature control reinforcing sulfate reducing bacteria reactor water outlet sulphates content stabilization is 64%- in 550mg/L-600mg/L clearances
70%, REGSB water outlet COD are stable in 1500mg/L-3000mg/L, and clearance is 66%-83%.By Experimental Comparison, pass through
After devulcanization anaerobic technique and precipitation sulphur removal, anaerobic reactor reaction efficiency improves nearly 220%.
Embodiment 2：Yangzhou auxiliary agent factory production waste water
The first step；Devulcanization anaerobic reaction technology is first carried out using above-mentioned technique, then by precipitating the technology of sulphur removal, waste water
For the waste water produced in Yangzhou auxiliary reagent factory process of producing product, water quality is as follows：COD15000mg/L-25000mg/L；SO4 2-
2000-3000mg/L, pH value 6-8.Handling process is as shown in figure 1, by devulcanization pond, water quality blender, temperature control reinforcing SRB reactions
Device, tube mixer, EAO ponds and remodeling REGSB reactor compositions.
Second step,；Temperature control reinforcing SRB reactors running temperature is 30-60 DEG C, and pH is stable in 6.5-8, hydraulic detention time
18h, sludge concentration is about 6000mg/L, desulfurizing agent dosage 3mg/L.
3rd step,；Tube mixer desulfurizing agent dosage 1500mg/L, EAO pond HRT5h, REGSB reactors design volume
Load 5kgCOD/ (m3D), using two-stage REGSB reactor tandem compound modes.
Temperature control reinforcing desulfuration agent reactor sulfate clearance is stable to be gone in 65%-70%, single-stage REGSB reactors COD
Except rate is stable in 60%-65%.
Claims (9)
1. a kind of efficient desulfurizing denitrification method of devulcanization Anammox, it is characterised in that comprise the following steps：
The first step, raw water enters AnV reactors and carries out devulcanization and aminating reaction, and AnV reactor outlet water at tail end part is returned
Water inlet end is flowed to, raw water and AnV reactors recirculation water is mixed by water quality blender；Wherein AnV structure of reactor is many corridors
Road plug flow reactor, is fixed SRB kinds using suspension fixed-bed process in AnV reactors, it is ensured that the residence time of SRB kinds
More than its generation time；
Second step, the water outlet that AnV reactors are not flowed back adds desulfurizing agent by tubular static mixer, goes out AnV reactors
Sulfide in water is sufficiently mixed with desulfurizing agent, AnV reactors is gone out Sulfide in water and desulfurizing agent formation S2-Salt is precipitated；
3rd step, through entering EAO ponds with the waste water after desulphurizer mixing, carries out flocculation reaction；The water outlet of EAO ponds is divided into two strands,
One enters NNIT ponds and carries out nitrosation reaction；
4th step, REGSB reactors are introduced by another burst of water outlet of EAO ponds water outlet together with the water outlet in NNIT ponds, anti-in REGSB
Answer and Anammox reaction denitrogenation is carried out in device, while carrying out carburizing reagent；NNIT ponds effluent recycling device, backflow are set in addition
Than for：50%~2000%；
Wherein AnV reactors be devulcanization ammoniation reactor referred to as, SRB kinds be sulfate reduction strain referred to as, EAO ponds be senior
Oxidation depositing reservoir referred to as, NNIT ponds be nitrosation reactor referred to as, REGSB reactors be the anaerobic expanded granular sludge bed letter of remodeling
Claim.
2. according to the method described in claim 1, it is characterised in that described desulfurizing agent is FeSO4、FeCl2Or FeSO4And FeCl2
Mixture, wherein the desulfurizing agent added and sulphur i.e. S in AnV reactors i.e. devulcanization ammoniation reactor water outlet2-Mol ratio for 1~
4：1.
3. according to the method described in claim 1, it is characterised in that AnV reactors described in the first step is devulcanization aminating reaction
The hydraulic detention time of device is 8h~20h, and water temperature control is at 30 DEG C~65 DEG C, and pH value is controlled between 6.5~7.5.
4. according to the method described in claim 1, it is characterised in that the AnV reactors described in the first step are that devulcanization ammonification is anti-
The ratio answered device outlet water at tail end partial reflux and do not flowed back is 100%~1800%, many its width of corridor of gallery plug flow reactor
It is 1 with the ratio between the depth of water：1~3, return current ratio of the mixed liquid is 100%~1800%, and sets underwater propeller, power mixing intensity
Control is in 4~12w/m3。
5. according to the method described in claim 1, it is characterised in that the floating stuffing fixed bed described in the first step is using highly dense
Polyethylene material is spent, density is 0.95-0.98g/cm2, voidage is 95%, to fix sulfate reducing bacteria, while suspending
Iron plate and reduced iron powder are added in filler.
6. according to the method described in claim 1, it is characterised in that described EAO ponds are that advanced oxidation depositing reservoir is outer shroud inner circle
Concentric structure, outer shroud be water distribution, hybrid reaction area, inner circle is depositing separation area；Outer shroud is provided with impeller under water, plug-flow
The rotating speed of device is 16-120rpm, and depositing separation area sets the swinging swash plate of adjustable angle, and swash plate angle adjusting range is -60 °
~60 °, be respectively 10 × 10 in the GT values of each a quarter circulation journey of water (flow) direction4~8 × 104、8×104~5 × 104、
4×104~1 × 104、0.01×104~0.1 × 104, wherein G is velocity gradient, and T is the time；EAO ponds are advanced oxidation clarification
The sludge part that pond is dammed is back to devulcanization AnV reactors i.e. devulcanization ammoniation reactor origin or beginning, partly as excess sludge
Drain into sludge concentration tank.
7. method according to claim 6, it is characterised in that described EAO ponds are on the outside of the outer shroud of advanced oxidation depositing reservoir
It is the 1/8~1/4 of inner circle width firing angle to set length, and width is 0.8m~1.8m mixing pit, and described mixing pit is vertically to turn over
More formula baffling is hybrid, and mixing pit hydraulic detention time is 5min~15min, and flow velocity is 0.2m/s~0.6m/s；And in mixing
Divergent contour vertebral body structure is set at pond entrance 1.5m~5m, to form jet, the gradient of current is improved, strengthens mixed effect；Expand
It is 0.5~1.7m to dissipate shape vertebral body structure diameter at butt end, and top diameter is 0.2m~0.5m.
8. according to the method described in claim 1, it is characterised in that described NNIT ponds are setting suspension in nitrosation reactor
Filler fixed bed, to fix Nitrosomas, wherein temperature control is at 14 DEG C~38 DEG C, and pH value is controlled in 7.2~8.8, dissolved oxygen
Control is in 0~2.0mg/L.
9. according to the method described in claim 1, it is characterised in that described REGSB reactors are that remodeling anaerobic expanded granular is dirty
Mud bed is shading closed reactor, and REGSB ponds are that the anaerobic expanded granular sludge bed ammonia nitrogen loading of remodeling is 7.5~20kg N
m-3d-1；Temperature control is at 23 DEG C~45 DEG C；PH value control 6.7~8.6；Absolute anaerobic environment, when starting to start, first exposes
Nitrogen or argon gas deoxygenation, when dissolved oxygen content is less than 0.05mg/L, stop deoxygenation；And water inlet nitrite and REGSB reactions
Device is that the retrofit ammonia density and nitrite concentration of anaerobic expanded granular sludge bed inside is below 1000mg/L；Phosphate concn
Less than 2500mg/L.
Priority Applications (1)
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