CN103951055B - The method of denitrification process low ratio of carbon to ammonium waste water while of methanation - Google Patents
The method of denitrification process low ratio of carbon to ammonium waste water while of methanation Download PDFInfo
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Abstract
The invention discloses the reactor of methanation simultaneously denitrification process low ratio of carbon to ammonium waste water, comprise cylindrical shell, and the triphase separator be positioned at above cylindrical shell, triphase separator comprises urceolus and the two-layer cylindrical shell of inner core, inner core is positioned at urceolus, equal opening bottom urceolus and inner core, connected epimere and hypomere is divided into bottom urceolus, bottom urceolus, epimere inwardly shrinks, bottom urceolus, hypomere expands outwardly and forms one baffle, the bottom of inner core expands outwardly and forms secondary baffle plate, the epimere of urceolus and hypomere stretch in cylindrical shell cavity, air chamber district is divided in triphase separator, gas slowly-releasing district, settling region and region, four, recirculating zone, urceolus is provided with peripheral weir being positioned at recirculating zone upper position on one week.The invention also discloses method of wastewater treatment, by controlling the C/N value in different steps, denitrification and methane phase can be realized in single reaction vessel simultaneously.Advantage of the present invention: the degree of depth can remove useless Organic substance in water and nitrogen, removal efficiency is high, and can produce energy methane simultaneously.
Description
Technical field
The present invention relates to industrial waste water treatment, the reactor of in particular methanation simultaneously denitrification process low ratio of carbon to ammonium waste water and method.This reactor can realize anaerobic methane and denitrification simultaneously.
Background technology
UASB (upflow anaerobic sludge blanket process, the english abbreviation of Up-flow Anaerobic Sludge Bed/Blanket, hereinafter referred to as UASB) be made up of sludge reaction district, gas-liquid-solid three-phase separator (comprising settling region) and air chamber three part.In reaction zone, bottom, retain a large amount of anaerobic sludge, sedimentation function and the good mud of cohesion performance form Sludge Bed in bottom.Waste water to be processed carries out mixing from the inflow of anaerobic mud bed bottom with mud Sludge Bed and contacts, and the organism in the microbial decomposition waste water in mud is converted into biogas.Biogas is constantly released with micro-bubble form, micro-bubble is in uphill process, continuous merging, form larger bubble gradually, rise on Sludge Bed top together with water enter triphase separator because the stirring of biogas forms the thinner mud of sludge concentration, when biogas encounters the reflector of separator bottom, be folded to the surrounding of reflector, then air chamber is entered through water layer, concentrate on air chamber biogas, derive with conduit, solid-liquid mixed solution enters the settling region of triphase separator through reflection, mud in waste water flocculates, particle increases gradually, and sedimentation under gravity.The mud be precipitated on skew wall slides back in anaerobic reaction district along skew wall, makes the mud that in reaction zone, accumulation is a large amount of, and the process water outlet after being separated with mud is overflowed from overflow weir top, settling region, then discharges Sludge Bed.Namely organic matter removal in waste water can be converted to biogas by this UASB.
In wastewater treatment process, anti-nitration reaction is NO
3 --N is converted into nitrogen N under the effect of denitrifying bacteria
2overflow from water.Most of denitrifying bacterium is heterotroph facultative anaerobic bacteria, and denitrification process needs a large amount of electron donor, and the denitrification stage is with NO
3 --N is electron acceptor(EA), and organism is as electron donor, and electron donor derives from external carbon source usually, research show the small molecules such as methyl alcohol, acetic acid not easily fermented organic more easily utilized by denitrifying bacteria, denitrifying capacity is relevant with the amount of available carbon source, i.e. C/N ratio.
Exist in nitrate and organic anaerobic system at the same time, complicated easily fermented organic can be hydrolyzed acid-producing bacteria and be converted into organic acid and alcohols, and the organic acid such as propionic acid, butyric acid and alcohols can be converted into acetic acid, H by hydrogen-producing acetogens
2and CO
2.Denitrifying bacteria can with above-mentioned various organism for carbon source reduces nitric nitrogen.Methanogen is then main with acetic acid, H
2and CO
2for substrate methane phase.Traditional theory is thought, NO
3 -the existence of-N can cause the competition of denitrifying bacteria and methanogen, and then produces suppression to methanation.The restraining effect of denitrifying bacteria to methanogen shows as three aspects: 1. denitrification flora occupies advantage in the competition of carbon substrate; 2. denitrification process causes anaerobic system internal oxidition reduction potential to raise, and is unfavorable for that methanogen grows; 3. anti-nitration reaction intermediate product produces toxic action to methanogen floras.
Therefore there is the shortcoming simultaneously can not removing useless Organic substance in water and nitrogen in existing UASB, namely in UASB single reaction vessel, denitrification and methanation reaction can not occur simultaneously.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide reactor and the method for a kind of methanation simultaneously denitrification process low ratio of carbon to ammonium waste water.By suitable control measures, add specific carbon source, control C/N values different in different steps, in single reaction vessel, denitrification and methane phase reaction can be realized simultaneously.
The present invention is achieved by the following technical solutions:
The reactor of denitrification process low ratio of carbon to ammonium waste water while of methanation, comprise the cylindrical shell as reactor body, and the triphase separator be positioned at above described cylindrical shell, described cylindrical shell outside is provided with temperature control unit, be cylindrical shell cavity in described cylindrical shell, described cylindrical shell cavity is sludge reaction district, bottom, described sludge reaction district is provided with anaerobic mud bed, described cylinder body bottom is provided with water-in, described water-in is connected to raw water box by water inlet pipe, described water inlet pipe is provided with intake pump, described triphase separator comprises urceolus and the two-layer cylindrical shell of inner core, described inner core is positioned at urceolus, equal opening bottom described urceolus and inner core, connected epimere and hypomere is divided into bottom described urceolus, bottom described urceolus, epimere inwardly shrinks, bottom described urceolus, hypomere expands outwardly and forms one baffle, the bottom of described inner core expands outwardly and forms secondary baffle plate, the epimere of described urceolus and hypomere stretch in described cylindrical shell cavity, air chamber district is divided in described triphase separator, gas slowly-releasing district, settling region and region, four, recirculating zone, the region of described urceolus high inside above inner core is air chamber district, the region of described inner core internal upper part is air chamber slowly-releasing district, the region that bottom described urceolus, epimere surrounds is settling region, gap area between described inner core and urceolus is recirculating zone, described urceolus is provided with peripheral weir being positioned at recirculating zone upper position on one week, described peripheral weir connects water outlet outward, described urceolus top seal and be provided with gas outlet being positioned at the position above air chamber district.
As the preferred implementation of above-mentioned reactor, between the inherent anaerobic mud bed and described water-in of described cylindrical shell cavity, be provided with the water distributor being uniformly distributed waste water.
As the preferred implementation of above-mentioned reactor, described temperature control unit is constant temperature water bath apparatus, and it is peripheral that described constant temperature water bath apparatus is arranged at described cylindrical shell.
As the preferred implementation of above-mentioned reactor, described cylindrical shell top is provided with thermometer, and described thermometer stretches in cylindrical shell cavity.
As the preferred implementation of above-mentioned reactor, described cylindrical shell is provided with multiple thief hole on different heights position, and described thief hole connects stopple coupon, and described stopple coupon is provided with sampling valve.
As the preferred implementation of above-mentioned reactor, described gas outlet is connected to gas collection vessel by escape pipe, and described escape pipe is provided with gas purifier and gas meter.
The invention also discloses the method for methanation simultaneously denitrification process low ratio of carbon to ammonium waste water, comprise the steps:
A, be seed sludge by the anaerobic sludge taken from bottom plant effluent treatment reactor, by seed sludge clean water totally to remove the residual waste water on its surface, then this seed sludge be inoculated in this reactor as anaerobic mud bed;
B, the waste water of low ratio of carbon to ammonium is added in raw water box, with the organism in waste water be carbon source, with SODIUMNITRATE for nitrogenous source, control reactor operating temperature by temperature control unit and remain on 34-36 DEG C, the pH value controlling waste water remains on 7.5-7.7, the water inlet flow velocity keeping waste water is 2.304L/d, and hydraulic detention time is 73h, start reactor, waste water enters the cylindrical shell cavity of reactor under the effect of intake pump by the water-in of reactor bottom, upwards flow through the anaerobic mud bed of seed sludge composition, the mud generation anaerobic reaction of waste water and Sludge Bed, produce biogas and cause sludge stirring, the upwelling forming solid-liquid-gas mixing continues to rise, one baffle position is lower, mud granule in the interception upwelling of energy greater efficiency, complete preliminary solid-liquid separation, upwelling after preliminary solid-liquid separation continues to rise through the mud granule in secondary baffle plate second time separation upwelling, complete second time solid-liquid separation, there is gas-liquid separation in gas slowly-releasing district in upwelling subsequently, and the gas of separation enters air chamber district, and the liquid of separation enters settling region by recirculating zone, and in the liquid of separation, supernatant liquor is crossed peripheral weir and discharged by water outlet,
C, reactor first 10 days of running, the nitrate that controls to intake in raw water box is 0; 11-31 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 75:1; 32-62 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 15:1; 63-98 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 7.5:1.
As the preferred implementation of aforesaid method, described step C is: control water inlet total organic carbon TOC concentration constant, the interim concentration improving water inlet nitric nitrogen.
As the preferred implementation of aforesaid method, described step C is specially: the total organic carbon TOC concentration that controls to intake in raw water box in 98 days that run at reactor remains 2250mg/L always; Reactor first 10 days of running, the nitrate that controls to intake in raw water box is 0; 11-31 days, nitrate of intaking in control raw water box is 30mg/L; 32-62 days, nitrate of intaking in control raw water box is 150mg/L; 63-98 days, nitrate of intaking in control raw water box is 300mg/L.
As the preferred implementation of aforesaid method, in described step B, the gas entering air chamber district enters escape pipe through gas outlet, purifies it through gas purifier, then carry out gas flow measurement by gas meter, finally enter gas collection vessel by collection and confinement of gases; By strength of fluid survey meter, measurement of concetration is carried out to the supernatant liquor of discharging from water outlet.
The present invention has the following advantages compared to existing technology:
In the inventive method, by suitable control measures, control water inlet TOC concentration constant, the interim concentration improving water inlet nitric nitrogen, the C/N value controlling different steps is different, can realize the object of denitrification and methane phase reaction simultaneously, draw by experiment in single reaction vessel, in UASB reactor, obtain the organic removal rate of more than 98.6% and the nitric nitrogen clearance of more than 99.1%.
The present invention adopts the organism in UASB reactor for treatment waste water, has that energy consumption is low, sludge yield is few, load advantages of higher; The present invention makes sewage treatment technology process greatly simplify, and makes full use of the carbon source denitrification in raw wastewater, achieves the wastewater treatment theory of " treatment of wastes with processes of wastes against one another ", reaches the object that the degree of depth simultaneously removes useless Organic substance in water and nitrogen, and can produce energy methane.In addition, the reactor used by the present invention, adopt the baffle plate of two-stage different heights position, can tackle the mud granule in upwelling more fully, twice solid-liquid separation makes solid-liquid separation more abundant; And the distinctive structure of its triphase separator, ensure by peripheral weir clarification of water out on the one hand, on the other hand, top is secondary baffle plate, below is the settling region that bottom urceolus, epimere inwardly shrinks formation, and volume is larger, mud can better be retained, facilitate sludge settling, the mud that final settling region is separated comes back in anaerobic mud bed reaction zone, thus does not need to establish settling tank and sludge reflux equipment etc., structure is simple, and three phase separation processing efficiency is high; Its temperature control unit adopts the constant temperature water bath apparatus be centered around outside cylindrical shell, ensure that reactor operating temperature is constant and stable; And cylindrical shell is provided with multiple thief hole on different heights position, can easily get different heights mud thus analyze wherein microorganism composition.
Accompanying drawing explanation
Fig. 1 is structure of reactor schematic diagram of the present invention.
Fig. 2 is total organic carbon TOC concentration and the clearance variation diagram in time of water outlet in method of the present invention.
Fig. 3 is the nitric nitrogen NO of Inlet and outlet water in method of the present invention
3--N concentration and clearance are schemed in time.
Fig. 4 is each gaseous fraction proportion variation diagram in time produced in reactor in method of the present invention.
Embodiment
Elaborate to embodiments of the invention below, the present embodiment is implemented under premised on technical solution of the present invention, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
Refer to Fig. 1, the reactor of denitrification process low ratio of carbon to ammonium waste water while of a kind of methanation provided by the invention, comprise the cylindrical shell 1 as reactor body and the triphase separator that is positioned at above cylindrical shell 1, cylindrical shell 1 outside is provided with temperature control unit, temperature control unit is constant temperature water bath apparatus 2, it is peripheral that constant temperature water bath apparatus 2 is arranged at cylindrical shell 1, and it controls the operating temperature of reactor by soak cycles water 21 in cylindrical shell 1 peripheral circulation.Be cylindrical shell cavity in cylindrical shell 1, cylindrical shell cavity is sludge reaction district, and bottom, sludge reaction district is provided with anaerobic mud bed 11, and cylinder body bottom is provided with water-in 12, is provided with the water distributor 13 being uniformly distributed waste water between cylindrical shell cavity inherent anaerobic mud bed 11 and water-in 12.Cylindrical shell 1 top is provided with thermometer 14, and thermometer 14 stretches in cylindrical shell cavity.Water-in 12 is connected to raw water box 16 by water inlet pipe, and water inlet pipe is provided with intake pump 15.Triphase separator comprises urceolus 3 and the two-layer cylindrical shell of inner core 4, inner core 4 is positioned at urceolus 3, equal opening bottom urceolus 3 and inner core 4, connected epimere 31 and hypomere 32 is divided into bottom urceolus 3, bottom urceolus 3, epimere 31 inwardly shrinks, bottom urceolus 3, hypomere 32 expands outwardly and forms one baffle, the bottom of inner core 4 expands outwardly and forms secondary baffle plate 41, the epimere 31 of urceolus 3 and hypomere 32 stretch in cylindrical shell cavity, air chamber district 51 is divided in triphase separator, gas slowly-releasing district 52, settling region 53 and region, 54 4, recirculating zone, the region of urceolus 3 high inside above inner core 4 is air chamber district 50, the region of inner core 4 internal upper part is air chamber slowly-releasing district 52, the region that bottom urceolus 3, epimere 31 surrounds is settling region 53, gap area between inner core 4 and urceolus 3 is recirculating zone 54, urceolus 3 is provided with peripheral weir 55 being positioned at recirculating zone 54 upper position on one week, peripheral weir 55 is outer connects water outlet 56, urceolus 3 top seal and be provided with gas outlet 33 being positioned at the position above air chamber district 51, gas outlet 33 is connected to gas collection vessel by escape pipe, escape pipe is provided with gas purifier and gas meter.Cylindrical shell 1 is provided with multiple thief hole 17 on different heights position, and thief hole 17 connects stopple coupon, and stopple coupon is provided with sampling valve.
Reactor used by the present invention, adopt the baffle plate of two-stage different heights position, can tackle the mud granule in upwelling more fully, twice solid-liquid separation makes solid-liquid separation more abundant; And the distinctive structure of its triphase separator, ensure by peripheral weir 55 clarification of water out on the one hand, on the other hand, top is secondary baffle plate 41, below is that bottom urceolus 3, epimere 31 inwardly shrinks the settling region 53 formed, and volume is larger, mud can better be retained, facilitate sludge settling, the mud that final settling region is separated comes back in anaerobic mud bed 11 reaction zones, thus does not need to establish settling tank and sludge reflux equipment etc., structure is simple, and three phase separation processing efficiency is high; Its temperature control unit adopts the constant temperature water bath apparatus 2 be centered around outside cylindrical shell 1, ensure that reactor operating temperature is constant and stable; And cylindrical shell 1 is provided with multiple thief hole 17 on different heights position, can easily get different heights mud thus analyze wherein microorganism composition.
The invention also discloses the method for methanation simultaneously denitrification process low ratio of carbon to ammonium waste water, comprise the steps:
A, be seed sludge by the anaerobic sludge taken from bottom plant effluent treatment reactor, the concentration of seed sludge is 20g/L, by its by clean water totally to remove the residual waste water on its surface, then this seed sludge is inoculated in this reactor as anaerobic mud bed 11;
B, the waste water of low ratio of carbon to ammonium is added in raw water box 16, with the organism sodium acetate in waste water be carbon source, with SODIUMNITRATE for nitrogenous source, control reactor operating temperature by temperature control unit and remain on 34-36 DEG C, the pH value controlling waste water remains on 7.5-7.7, the water inlet flow velocity keeping waste water is 2.304L/d, and hydraulic detention time is 73h, start reactor, waste water enters the cylindrical shell cavity of reactor under the effect of intake pump 15 by the water-in 12 of reactor bottom, upwards flow through anaerobic mud bed 11 of seed sludge composition, the mud generation anaerobic reaction of waste water and Sludge Bed, produce biogas and cause sludge stirring, the upwelling forming solid-liquid-gas mixing continues to rise, one baffle position is lower, mud granule in the interception upwelling of energy greater efficiency, complete preliminary solid-liquid separation, upwelling after preliminary solid-liquid separation continues to rise through the mud granule in secondary baffle plate 41 second time separation upwelling, complete second time solid-liquid separation, there is gas-liquid separation in gas slowly-releasing district 52 in upwelling subsequently, and the gas of separation enters air chamber district 51, and the liquid of separation enters settling region 53 by recirculating zone 54, and in the liquid of separation, supernatant liquor is crossed peripheral weir 55 and discharged by water outlet 56,
C, reactor first 10 days of running, the nitrate that controls to intake in raw water box 16 is 0; 11-31 days, carbon-nitrogen ratio C/N of intaking in control raw water box 16 is 75:1; 32-62 days, carbon-nitrogen ratio C/N of intaking in control raw water box 16 is 15:1; 63-98 days, carbon-nitrogen ratio C/N of intaking in control raw water box 16 is 7.5:1.
Wherein, in above-mentioned steps B, the gas entering air chamber district 51 enters escape pipe through gas outlet 33, purifies it through gas purifier, then carry out gas flow measurement by gas meter, finally enter gas collection vessel by collection and confinement of gases; By strength of fluid survey meter, measurement of concetration is carried out to the supernatant liquor of discharging from water outlet 56.
Wherein, in above-mentioned steps C, constant by control water inlet TOC concentration, stage improves the concentration of water inlet nitric nitrogen thus the water inlet carbon-nitrogen ratio C/N of control different steps.Be specially: the total organic carbon TOC concentration that controls to intake in raw water box 16 in 98 days that run at reactor remains 2250mg/L always; Reactor first 10 days of running, the nitrate that controls to intake in raw water box 16 is 0; 11-31 days, nitrate of intaking in control raw water box 16 is 30mg/L; 32-62 days, nitrate of intaking in control raw water box 16 is 150mg/L; 63-98 days, nitrate of intaking in control raw water box 16 is 300mg/L.
In order to verify the effect of method of the present invention, the applicant has specially done experiment embodiment.
In this experiment embodiment, in raw water box 16, water inlet adopts the mixed solution of sodium acetate, SODIUMNITRATE, micro-strong solution and tap water, carry out the composition of simulated wastewater, wherein following (mg/L): the TOC of each constituent concentration was 2250 (being equivalent to COD3000); NO
3 --N is 0 ~ 300; NH
4hCO
3first 10 days 2024, be 0 in following time; KH
2pO
43H
2o is 800; (NH
4)
6mo
7o
24be 15; MgCl
26H
2o is 100; MnCl
24H
2o is 5; NiCl
26H
2o is 5; CoC1
26H
2o is 5; CuC1
25H
2o is 5; CaCl
2be 50; NaCl is 10; FeCl
2be 25; H
3bO
4be 5; ZnCl is 25; A1C1
3be 2.5, do phosphorus source make COD:P=500:1 with phosphate buffered saline buffer, the pH regulating simulated wastewater water inlet with sodium bicarbonate is 7.6 ± 0.1.The seed sludge of experiment takes from the bottom of the anaerobic reactor of China Resources Snowflake Beer factory wastewater treatment, washes 3 times to remove the residual distillery waste of Sludge Surface before inoculation.
In reactor whole service process, control the carbon-nitrogen ratio C/N in each stage by adding specific carbon source and thin up to the water inlet of simulated wastewater.This experiment embodiment is in reactor whole service process, control reactor operating temperature by temperature control unit and remain on 34-36 DEG C, water inlet flow velocity is kept to be 2.304L/d, hydraulic detention time is 73h, in fixing water inlet, total organic carbon TOC concentration is that 2250mg/L is constant, improves water inlet nitric nitrogen NO stage by stage
3 --N concentration; Reactor first 10 days of running, the nitrate that controls to intake in raw water box 16 is 0; 11-31 days, nitrate of intaking in control raw water box 16 is 30mg/L; 32-62 days, nitrate of intaking in control raw water box 16 is 150mg/L; 63-98 days, nitrate of intaking in control raw water box 16 is 300mg/L.
Experimental result is see Fig. 2 to Fig. 4, and first 10 days of experiment beginning is the first stage, take sodium acetate as carbon source in simulated wastewater, NO of simultaneously intaking
3 --N concentration is 0, and this stage main purpose is that as seen from Figure 2, in this stage, the concentration of TOC of yielding water declines rapidly, and TOC clearance reaches 86.36% in order to make mud adapt to new waste water and ensure the activity of mud;
Within 11-31 days, be subordinate phase, NO in simulated wastewater
3 --N concentration is promoted to 30mg/L, and analysis chart 2 and Fig. 3 can find out simultaneously, and this stage reactors TOC of yielding water concentration still keeps downtrending, and water outlet NO
3 --N concentration is approximately zero, NO
3 --N clearance is up to more than 95%; To the 31st day TOC of yielding water concentration be 172.97mg/L, clearance is 92.31%, water outlet NO
3 --N concentration is 0.41mg/L, clearance is 98.65%.
Within 32-62 days, be the phase III, NO in simulated wastewater
3 --N concentration is promoted to 150mg/L, and analysis chart 2 and Fig. 3 can find out simultaneously, and this stage reactors TOC of yielding water clearance remains on more than 90%, and water outlet NO
3 -although-N concentration is slightly gone up but amplitude is very low ignores, and NO
3 --N clearance still remains on more than 95%; To the 62nd day TOC of yielding water concentration be 83.15mg/L, clearance is 96.30%, water outlet NO
3 --N concentration is 0.69mg/L, clearance is 99.54%.
Within 63-98 days, be fourth stage, NO in simulated wastewater
3 --N concentration is promoted to 300mg/L, and analysis chart 2 and Fig. 3 can find out simultaneously, and this stage reactors TOC of yielding water clearance remains on more than 95%, and water outlet NO
3 --N concentration comparatively the phase III again slightly go up but concentration progressively decline from 10.22mg/L, NO
3 --N clearance still remains on more than 95%; To the 98th day TOC of yielding water concentration be 29.505mg/L, clearance is 98.69%, water outlet NO
3 --N concentration is 2.42mg/L, clearance is 99.19%.
What Fig. 4 represented is in the synchronous methanation of structure and denitrification plant process, each gaseous fraction proportion variation diagram in time produced in reactor.Composition graphs 3 is analyzed, along with NO simultaneously
3 --N adds, the CH produced in reactor
4content reduces and N
2content and CO
2content starts to raise, N
2amplification is greater than CO
2amplification, this is because denitrifying process creates CO
2, and CO
2can be utilized by methane-producing bacteria again.Tend towards stability to aerogenic composition when the 98th day, wherein N
2account for about 40%, CH
4account for about 50%, CO
2account for about 10%.After reactor is stable, gas production rate is 0.08L/h, and through calculating, the ratio of reactor produces N
2speed is 31.07mL/ (gVSSh), than product CH
4speed is 38.83mL/ (gVSSh).
Synthesizing map 2, Fig. 3, Fig. 4, reactor is stable, and TOC clearance reaches 98.69%, NO
3 --N clearance reaches 99.19%, TOC and NO
3 -the clearance of-N is all very high, and gas produces stable components, achieves anaerobic methaneization denitrification simultaneously in single anaerobic reactor.
Experimental result shows, with UASB reactor for reaction vessel, sodium acetate is carbon source, SODIUMNITRATE is nitrogenous source, and water inlet TOC concentration controls as 2250mg/L, water inlet NO
3 -it is 0 ~ 300mg/L that-N concentration controls, and improves reactor water inlet NO by stage
3 -the concentration of-N, interim reduces carbon-nitrogen ratio C/N, can realize being coupled of methanation and anti-nitration reaction in single reaction vessel fast.
In the inventive method, by suitable control measures, control water inlet TOC concentration constant, interim raising water inlet nitrate, the C/N value controlling different steps is different, can realize the object of denitrification and methane phase reaction simultaneously, draw by experiment in single reaction vessel, in anaerobic UASB reactor, obtain the organic removal rate of more than 98.6% and the nitric nitrogen clearance of more than 99.1%.
The present invention adopts the organism in UASB reactor for treatment waste water, has that energy consumption is low, sludge yield is few, load advantages of higher; The present invention makes sewage treatment technology process greatly simplify, and makes full use of the carbon source denitrification in raw wastewater, achieves the wastewater treatment theory of " treatment of wastes with processes of wastes against one another ", reaches the object that the degree of depth simultaneously removes useless Organic substance in water and nitrogen, and can produce the energy.
These are only preferred embodiment of the present invention, not in order to limit the present invention, all any amendments done within the spirit and principles in the present invention, equivalent replacement and improvement etc., all should be included within protection scope of the present invention.
Claims (9)
1. the method for methanation simultaneously denitrification process low ratio of carbon to ammonium waste water, described method is used reactor and is comprised cylindrical shell as reactor body, and the triphase separator be positioned at above described cylindrical shell, described cylindrical shell outside is provided with temperature control unit, be cylindrical shell cavity in described cylindrical shell, described cylindrical shell cavity is sludge reaction district, bottom, described sludge reaction district is provided with anaerobic mud bed, described cylinder body bottom is provided with water-in, described water-in is connected to raw water box by water inlet pipe, described water inlet pipe is provided with intake pump, it is characterized in that: described triphase separator comprises urceolus and the two-layer cylindrical shell of inner core, described inner core is positioned at urceolus, equal opening bottom described urceolus and inner core, connected epimere and hypomere is divided into bottom described urceolus, bottom described urceolus, epimere inwardly shrinks, bottom described urceolus, hypomere expands outwardly and forms one baffle, the bottom of described inner core expands outwardly and forms secondary baffle plate, the epimere of described urceolus and hypomere stretch in described cylindrical shell cavity, air chamber district is divided in described triphase separator, gas slowly-releasing district, settling region and region, four, recirculating zone, the region of described urceolus high inside above inner core is air chamber district, the region of described inner core internal upper part is air chamber slowly-releasing district, the region that bottom described urceolus, epimere surrounds is settling region, gap area between described inner core and urceolus is recirculating zone, described urceolus is provided with peripheral weir being positioned at recirculating zone upper position on one week, described peripheral weir connects water outlet outward, described urceolus top seal and be provided with gas outlet being positioned at the position above air chamber district,
It is characterized in that, described method comprises the steps:
A, be seed sludge by the anaerobic sludge taken from bottom plant effluent treatment reactor, by seed sludge clean water totally to remove the residual waste water on its surface, then this seed sludge be inoculated in this reactor as anaerobic mud bed;
B, the waste water of low ratio of carbon to ammonium is added in raw water box, with the organism in waste water be carbon source, with SODIUMNITRATE for nitrogenous source, control reactor operating temperature by temperature control unit and remain on 34-36 DEG C, the pH value controlling waste water remains on 7.5-7.7, the water inlet flow velocity keeping waste water is 2.304L/d, and hydraulic detention time is 73h; Start reactor, waste water enters the cylindrical shell cavity of reactor under the effect of intake pump by the water-in of reactor bottom, upwards flow through the anaerobic mud bed of seed sludge composition, the mud generation anaerobic reaction of waste water and Sludge Bed, produce biogas and cause sludge stirring, the upwelling forming solid-liquid-gas mixing continues to rise, one baffle can tackle the mud granule in upwelling, complete preliminary solid-liquid separation, upwelling after preliminary solid-liquid separation continues to rise through the mud granule in secondary baffle plate second time separation upwelling, completes second time solid-liquid separation; There is gas-liquid separation in gas slowly-releasing district in upwelling subsequently, and the gas of separation enters air chamber district, and the liquid of separation enters settling region by recirculating zone, and in the liquid of separation, supernatant liquor is crossed peripheral weir and discharged by water outlet;
C, reactor run first 10 days, and nitrate of intaking in control raw water box is 0; 11-31 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 75:1; 32-62 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 15:1; 63-98 days, carbon-nitrogen ratio C/N of intaking in control raw water box is 7.5:1.
2. the method for methanation as claimed in claim 1 denitrification process low ratio of carbon to ammonium waste water simultaneously, is characterized in that: be provided with the water distributor being uniformly distributed waste water between the inherent anaerobic mud bed and described water-in of described cylindrical shell cavity.
3. the method for methanation as claimed in claim 1 denitrification process low ratio of carbon to ammonium waste water simultaneously, it is characterized in that: described temperature control unit is constant temperature water bath apparatus, it is peripheral that described constant temperature water bath apparatus is arranged at described cylindrical shell.
4. the method for methanation as claimed in claim 1 denitrification process low ratio of carbon to ammonium waste water simultaneously, is characterized in that: described cylindrical shell top is provided with thermometer, and described thermometer stretches in cylindrical shell cavity.
5. the method for the denitrification process low ratio of carbon to ammonium waste water simultaneously of the methanation as described in as arbitrary in Claims 1-4, it is characterized in that: described cylindrical shell is provided with multiple thief hole on different heights position, described thief hole connects stopple coupon, and described stopple coupon is provided with sampling valve.
6. the method for methanation as claimed in claim 5 denitrification process low ratio of carbon to ammonium waste water simultaneously, it is characterized in that: described gas outlet is connected to gas collection vessel by escape pipe, described escape pipe is provided with gas purifier and gas meter.
7. the method for methanation as claimed in claim 1 denitrification process low ratio of carbon to ammonium waste water simultaneously, it is characterized in that, described step C is: control water inlet total organic carbon TOC concentration constant, the interim concentration improving water inlet nitric nitrogen.
8. the method for methanation as claimed in claim 7 denitrification process low ratio of carbon to ammonium waste water simultaneously, it is characterized in that, described step C is specially: the total organic carbon TOC concentration that controls in 98 days that run at reactor to intake in raw water box remains 2250mg/L always; Reactor runs first 10 days, and nitrate of intaking in control raw water box is 0; 11-31 days, nitrate of intaking in control raw water box is 30mg/L; 32-62 days, nitrate of intaking in control raw water box is 150mg/L; 63-98 days, nitrate of intaking in control raw water box is 300mg/L.
9. the method for methanation as claimed in claim 6 denitrification process low ratio of carbon to ammonium waste water simultaneously, it is characterized in that, in described step B, the gas entering air chamber district enters escape pipe through gas outlet, through gas purifier, it is purified, then carry out gas flow measurement by gas meter, finally enter gas collection vessel by collection and confinement of gases; By strength of fluid survey meter, measurement of concetration is carried out to the supernatant liquor of discharging from water outlet.
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| CN107540085A (en) * | 2017-09-18 | 2018-01-05 | 华南理工大学 | It is a kind of to promote the anaerobism method that denitrification methane phase is efficiently carried out simultaneously |
| CN108693012B (en) * | 2018-04-11 | 2021-12-21 | 欧频 | Concentration device for water sample of radiochemical analysis of strontium-90 nuclide in water |
| CN109467184A (en) * | 2018-12-06 | 2019-03-15 | 景德镇陶瓷大学 | A kind of processing method of saliferous nitrate nitrogen organic wastewater |
| CN109851166B (en) * | 2019-01-30 | 2023-09-29 | 沈阳工业大学 | Internal circulation type anaerobic and denitrification methane-generating reactor and sewage treatment method |
| CN111233155A (en) * | 2020-03-31 | 2020-06-05 | 重庆科技学院 | Device for synchronously and efficiently removing organic matters, nitrogen and phosphorus in sewage |
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