CN111484133A - Reaction system and treatment method for enhancing micro-aerobic methane-producing granular sludge - Google Patents

Reaction system and treatment method for enhancing micro-aerobic methane-producing granular sludge Download PDF

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CN111484133A
CN111484133A CN202010370263.7A CN202010370263A CN111484133A CN 111484133 A CN111484133 A CN 111484133A CN 202010370263 A CN202010370263 A CN 202010370263A CN 111484133 A CN111484133 A CN 111484133A
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周鑫
葛大令
张伟
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Taiyuan University of Technology
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    • C02F3/00—Biological treatment of water, waste water, or sewage
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F3/2866—Particular arrangements for anaerobic reactors
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C02F3/2873—Particular arrangements for anaerobic reactors with internal draft tube circulation
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract

The invention discloses a reaction system and a treatment method for enhancing micro-aerobic methanogenic granular sludge, wherein the reaction system comprises: the system comprises a water inlet adjusting tank (1), a water inlet peristaltic pump (2), an expanded granular sludge bed biomembrane reactor (16), an internal circulating pump (11) and an air compressor (12); the expanded granular sludge bed biofilm reactor (16) comprises a main reaction zone (17) and a three-phase separator (6), and the volume ratio is 1-1.2: 1; the lower part of the main reaction zone (17) is provided with a granular sludge bed (4), the top of the main reaction zone (17) is provided with a fixed packed bed (5), and the fixed packed bed (5) accounts for 20-30% of the volume of the main reaction zone (17); the main reaction zone (17) and the three-phase separator (6) are both provided with a sampling port (9) and an observation port. The invention realizes high-efficiency treatment and energy recovery of high-concentration organic wastewater and has good practical application value.

Description

Reaction system and treatment method for enhancing micro-aerobic methane-producing granular sludge
Technical Field
The invention belongs to the technical field of biological treatment of wastewater, and particularly relates to a reaction system and a treatment method for enhancing micro-aerobic methanogenic granular sludge.
Background
The biochemical treatment is an economic and efficient treatment method commonly adopted by high-concentration organic wastewater. Through the effect of anaerobic microorganisms, not only can get rid of COD in the waste water, can also retrieve biogas (methane). The main methanogenic reaction systems developed so far are: anaerobic activated sludge, an anaerobic biological filter, an Anaerobic Sequencing Batch Reactor (ASBR), an anaerobic folded plate reactor (ABR), an Upflow Anaerobic Sludge Blanket (UASB) and the like. However, methanogens belong to strict anaerobes, and have very slow growth rate and very strict requirements on water inlet conditions and environment; on the other hand, the methanogenic system has competition and mutual operation relations among microorganism populations such as methanogenic bacteria, hydrolytic acidogenic bacteria and acetogenic bacteria, and if the methanogenic system is improperly operated, the methanogenic efficiency can be inhibited, so that the start time of methanation is prolonged and even the methanation fails.
In recent years, the technology of enhancing anaerobic methanogenesis has become the focus of research on sewage treatment. Many studies have shown that: under the condition of micro-oxygen, the facultative microorganisms can quickly convert organic matters into intermediate products of low-molecular fatty acid (acetic acid), so that favorable conditions are created for quick methanation formation. The hypoxia condition has the advantages of high oxygen utilization rate, low aeration energy consumption, low residual sludge yield, high COD removal rate, strong impact load resistance, removal of substances difficult to biodegrade and the like, and the micro-aerobic biological treatment technology has wide application prospect in the aspect of fast start of methanogenesis, however, the DO in the reactor is easily increased by the conventional micro-aerobic reaction device and operation mode, so that the anaerobic microenvironment is damaged, and in addition, the hypoxia condition easily causes filamentous expansion of sludge, so that the sludge loss phenomenon is caused, and the methanogenesis efficiency is easily reduced. The granular sludge is a high-efficiency sewage biological treatment technology, the impact of bad conditions on methanogens can be reduced by the formation of the granular sludge, a good protection effect can be achieved, and in addition, the granular sludge with larger grain size has large grain size and good sludge settling performance, and the problem of sludge floating or loss caused by gas production can be avoided.
At present, the research on the aerobic granular sludge in a batch operation reactor is mature, but the research on a continuous flow reactor and a culture method thereof is less. Therefore, the development of a stable continuous flow reaction device and the establishment of a corresponding operation method to ensure the rapid realization of methanogenic aerobic granular sludge is of great significance to the stable and efficient operation of high-concentration organic wastewater.
Disclosure of Invention
Aiming at the problem of low methane production efficiency caused by the traditional micro-aerobic condition, the invention provides a reaction system and a treatment method for producing methane granular sludge by using enhanced micro-aerobic so as to realize high-efficiency treatment and energy recovery of high-concentration organic wastewater.
The invention is realized by adopting the following technical scheme:
an enhanced micro-aerobic methanogenic granular sludge reaction system, comprising: a water inlet adjusting tank, a water inlet peristaltic pump, an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), an internal circulating pump and an air compressor.
The expanded granular sludge bed biofilm reactor comprises a main reaction zone and a three-phase separator, and the volume ratio of (1-1.2) to (1); the lower part of the main reaction zone is provided with a granular sludge bed, the top of the main reaction zone is provided with a fixed packed bed, and the fixed packed bed accounts for 20-30% of the volume of the main reaction zone; the main body reaction zone and the three-phase separator are both provided with a sampling port and an observation port.
Polyurethane sponge is filled in the fixed packed bed, the polyurethane sponge is 8-25 mm square, the inner hole diameter is 2-7 mm, and the filling rate of the carrier (polyurethane sponge) is 20% -30%.
The granular sludge bed adopts mixed sludge of sludge in a concentration tank of an urban sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is (2-3): 1, and the inoculation volume accounts for 40% of the main reaction zone.
The outlet pipeline of the air compressor is provided with a mass flow meter and then is introduced into a water inlet regulating reservoir, the outlet at the bottom of the water inlet regulating reservoir is connected with the inlet at the bottom of a main reaction zone of the expanded granular sludge bed biofilm reactor through a water inlet peristaltic pump, a triangular effluent weir of a three-phase separator of the expanded granular sludge bed biofilm reactor is communicated with the inlet at the bottom of the main reaction zone through an internal circulating pump, and the triangular effluent weir is additionally connected with a water outlet; and a gas collection port of the three-phase separator is provided with a wet gas flowmeter.
A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge comprises the following steps:
(1) and establishing the reaction system.
(2) Culturing the microorganism
The sludge bed directly adopts the mixed sludge of the sludge in the concentration tank of the municipal sewage treatment plant and the sludge in the aerobic aeration tank as the inoculation sludge, the mixing mass ratio is (2-3): 1, and the inoculation volume accounts for 40% of the main reaction zone.
And inoculating the mixed sludge onto a polyurethane sponge filler by a sequencing batch reactor in a sludge discharge and biofilm formation method to form a biological carrier filler, and then putting the biological carrier filler into a fixed packed bed, wherein the inoculation step comprises the steps of mixing the mixed sludge and simulated wastewater of 1.5L, pumping the mixed sludge into a 5L SBR reactor (the filler is put into the reactor), standing for 24 hours, aerating for 8-10 hours after the microorganisms are inoculated onto the filler, standing for 14-16 hours, discharging 0.5L supernatant, replacing the new simulated wastewater by 0.5L, standing for 15-20 hours, then discharging 0.5L supernatant again, replacing the new simulated wastewater by 0.5L, standing for 15-20 hours, repeating the steps for 5-7 days, forming the biological carrier filler after a layer of biological membrane is formed on the surface of the sponge by naked eyes, then taking out the biological carrier filler from the SBR reactor, and putting the biological carrier filler into a system packed bed.
The ratio of C to N to P of inlet water (self-prepared simulated wastewater) is 200:5:1, the carbon source is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, and the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate.
Through aeration, intermittent water feeding and continuous small-flow water feeding, the culture time is 3.5-8.5 days, and the cultured sludge bed M L SS is 8-10 g/L.
Wherein, the feed water is also added with a microelement stock solution, and the microelement stock solution comprises the following components: FeCl3·4H2O（2000mg/L），CoCl2·6H2O（2000mg/L），MnCl2·4H2O（500mg/L），CuCl2·2H2O（30mg/L），ZnCl2（50mg/L），H3BO3（50mg/L），(NH4)6Mo7O24·4H2O（90mg/L），Na2SeO3（100mg/L），NiCl2·6H2O（50mg/L），EDTA（1000mg/L）；
The specific processes of stuffy aeration, intermittent water inflow and continuous small-flow water inflow are as follows: firstly, filtering to remove insoluble impurities, and carrying out stuffy aeration for 24 hours; then mixing the sludge and the simulated wastewater in an equal volume ratio, putting the mixture into a reactor, and standing for 12 hours; aerating for 12h after the sludge is inoculated on the biological carrier filler, discharging 1/3 supernatant, then adding simulated wastewater 1/3, aerating for 12h, discharging 1/3 supernatant, and repeating the process for 1-3 days; and finally, continuously feeding water with small flow (HRT is 4 days) to fill the reactor to recover the sludge activity, and continuously feeding water with small flow for 1-4 days.
(3) After the microorganism culture, the normal water-feeding continuous operation is started
The method comprises the following steps that inflow water (self-prepared simulation wastewater) flows into an inflow regulating reservoir, the wastewater is aerated in the inflow regulating reservoir through an air compressor, the aerated wastewater enters an expanded granular sludge bed biofilm reactor, the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L (calculated by calcium carbonate).
(4) The aeration sewage in the water inlet regulating tank is pumped into the bottom of a main body reaction area through a water inlet peristaltic pump, flows through a granular sludge bed and a fixed packed bed in sequence, and is finally discharged from a triangular water outlet weir of a three-phase separator, wherein a part of outlet water is mixed with inlet water through an internal circulating pump and enters the bottom of the main body reaction area again, the internal reflux ratio is 20-50% (the other part of outlet water can be directly discharged), dissolved oxygen DO in the reactor is controlled to be 0.15-0.35 mg/L, oxidation-reduction potential ORP is controlled to be-300-350 mv, the water temperature of a system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a temperature, pH, DO and ORP multi-parameter online monitor is arranged in the reactor to monitor the water inlet pH and micro-oxygen environment in real time.
(5) The Hydraulic Retention Time (HRT) is gradually shortened, the rapid methane production is realized through three operation processes, the HRT in the three operation processes are respectively set for 3 days, 2.5 days and 2 days, each HRT continuously operates for 15-20 days, the average methane yield of the system is 500-550 m L/d after 45-60 days, the COD removal rate is 92-95%, and the organic load is 0.4-2.5 kgCOD/m3·d。
（6）、On the basis of methanation realization, 20-50 mg/L of Ca is added into inlet water2+And 20-50 Mg/L Mg2+And promoting sludge granulation, rapidly and gradually shortening the HRT after continuously running for 25-40 days to accelerate the formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced from 2 days to 1 day, 12 hours and 6 hours, and each HRT runs for 8-12 days.
(7) After the process target of producing the methane aerobic granular sludge is achieved, the sludge at the bottom of the reactor is in a faint yellow rice grain shape, the sludge concentration M L SS is 16-20 g/L, the average sludge particle size is 1.0-2.5 mm, the sludge sedimentation ratio SV is 15-30%, the gas yield of the upper sludge is 300-1200M L/d, and the COD removal rate is more than 90%.
The method adopts a pre-aeration means, reduces the influence on the methanation activity of a methane-producing system, adds a fixed biological filler in the high-efficiency Sludge Expanded bed Reactor EGSB to form an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), utilizes the advantages of the Biofilm Reactor to effectively avoid the Sludge floating problem, can also improve the total microbial quantity of the Reactor, provides a good living microenvironment for anaerobic methane bacteria, and ensures that the start-up time of methane production of the Reactor is accelerated; on the basis of stable operation of a process system, the formation of aerobic granular sludge is accelerated by gradually shortening the hydraulic retention time and increasing the internal reflux.
The invention has the following beneficial effects:
1. by utilizing the mode of water inflow and pre-aeration, the novel reactor filled with the high-efficiency sludge expanded bed biomembrane of the porous sponge is adopted, and the COD in the organic wastewater can be effectively removed and the methane can be recovered through the formed high-efficiency methanogenic granular sludge.
2. The processing operation method is simple and the running time is short. The stable operation of the process can be realized only by temperature, pH, DO control and HRT regulation, and the total normal operation days is about 60-100 days.
3. The system has high methanation and COD removal efficiency, and the particle size of the generated sludge is large.
4. The granular sludge is compact, the sludge yield is low, and the system does not need to discharge sludge. The sewage and the sludge are easy to separate, and the phenomena of sludge expansion and loss can not occur.
The invention has reasonable design and good practical application value.
Drawings
FIG. 1 shows a schematic diagram of an enhanced micro-aerobic methanogenic granular sludge reaction system.
In the figure: 1-water inlet adjusting tank, 2-water inlet peristaltic pump, 3-water inlet, 4-granular sludge bed, 5-fixed packed bed, 6-three-phase separator, 7-gas collecting port, 8-triangular water outlet weir, 9-sampling port, 10-sludge discharging port, 11-internal circulating pump, 12-air compressor, 13-mass flow meter, 14-wet gas flow meter, 15-temperature controller, 16-Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), 17-main reaction zone and 18-water outlet.
Detailed Description
The following detailed description of specific embodiments of the invention refers to the accompanying drawings.
As shown in fig. 1, an enhanced micro-aerobic methanogenic granular sludge reaction treatment system is established, comprising: the system comprises a water inlet adjusting tank 1, a water inlet peristaltic pump 2, an expanded granular sludge bed biofilm reactor 16 (EGSBBR), an internal circulating pump 11, an air compressor 12, a water outlet tank and the like.
The expanded granular sludge bed biofilm reactor 16 comprises a main reaction zone 17 and a three-phase separator 6, wherein the volume ratio of (1-1.2) to (1); the three-phase separator 6 is positioned at the top of the reactor and mainly has the functions of precipitating sludge, separating the treated wastewater and collecting methane gas; the main body reaction zone 17 is provided with a temperature controller 15, the bottom of the main body reaction zone 17 is provided with a sludge discharge port 10, the lower part of the main body reaction zone 17 is provided with a granular sludge bed 4, the top of the main body reaction zone 17 is provided with a fixed packed bed 5, and the fixed packed bed 5 accounts for 20-30% of the volume of the main body reaction zone 17; the main reaction zone 17 and the three-phase separator 6 are provided with a sampling port 9 and a viewing port.
Polyurethane (PU) sponge is filled in the fixed packed bed 5, the polyurethane sponge is 8-25 mm cube, the inner hole diameter is 2-7 mm, the polyurethane sponge and the inner hole diameter are mutually communicated, and the carrier filling rate is 20% -30%.
The granular sludge bed 4 adopts mixed sludge of concentrated tank sludge of an urban sewage treatment plant and sludge of an aerobic aeration tank as inoculation sludge, the mass ratio of the mixed sludge to the aerobic aeration tank is (2-3): 1, and the inoculation volume accounts for 40% of that of the main reaction zone 17.
A mass flow meter 13 is arranged on an outlet pipeline of an air compressor 12 and then the outlet pipeline is introduced into a water inlet adjusting tank 1, an outlet at the bottom of the water inlet adjusting tank 1 is connected with an inlet at the bottom of a main body reaction zone 17 of an expanded granular sludge bed biomembrane reactor 16 through a water inlet peristaltic pump 2, a triangular water outlet weir 8 of a three-phase separator 6 of the expanded granular sludge bed biomembrane reactor 16 is communicated with the inlet at the bottom of the main body reaction zone 17 through an internal circulating pump 11, and the triangular water outlet weir 8 is additionally connected with a water outlet 18; the gas collection port 7 of the three-phase separator 6 is provided with a wet gas flowmeter 14.
Example 1
A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge comprises the following steps:
(1) establishing a reaction system, which mainly comprises: the system comprises a water inlet adjusting tank, a water inlet pump, an air compressor, an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), an internal circulating pump and a water outlet tank;
the EGSBBR comprises a main reaction zone and a three-phase separator, and the volume ratio is (1-1.2): 1; the lower part of the main reaction zone is provided with a granular sludge bed, and the top of the main reaction zone is provided with a fixed packed bed which accounts for 25 percent of the volume of the main reaction zone; the two areas are provided with a sampling port and an observation port, the three-phase separator is positioned at the top of the reactor and has the main functions of precipitating sludge, separating treated wastewater and collecting methane gas;
polyurethane (PU) sponge is filled in a fixed packed bed, the sponge is 8-25 mm square, the inner hole diameter is 2-7 mm, the sponge is communicated with each other, and the carrier filling rate is controlled to be 20%.
(2) Culturing the microorganism
The sludge bed directly adopts mixed sludge of sludge in a concentration tank of an urban sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 2:1, the inoculation volume accounts for 40% of a main reaction zone, and the mixed sludge is poured into a reactor from top to bottom.
And inoculating the mixed sludge onto a polyurethane sponge filler by a sludge discharge and film hanging method through a sequencing batch reactor to form a biological carrier filler, and then putting the biological carrier filler into a fixed filler bed.
The ratio of inlet water C, N and P is 200:5:1, the carbon source is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate, and the inlet water is also added with trace element stock solution of 1m L.
The method comprises the steps of carrying out closed aeration, intermittent water feeding and continuous small-flow water feeding for 5.5 days, wherein the cultured sludge bed M L SS is 8-9 g/L, wherein the closed aeration, the intermittent water feeding and the continuous small-flow water feeding are carried out by filtering to remove insoluble impurities for 24h, then mixing the sludge and the fed water in an equal volume ratio, placing the mixture into a reactor, standing the mixture for 12h, carrying out aeration for 12h after the sludge is inoculated on a biological carrier filler, discharging 1/3 supernatant, adding the fed water, repeating the process for 2 days, finally filling the reactor with the continuous small-flow water feeding (HRT is 4 days) to recover the sludge activity, and then carrying out the continuous small-flow water feeding for 2 days.
(3) After the microorganism culture, the normal water-feeding continuous operation is started
Inflow water (COD of high-concentration organic wastewater is about 2000 mg/L) flows into an inflow adjusting tank, the wastewater is aerated in the inflow adjusting tank through an air compressor, the quality of the inflow water (C: N: P ratio is 200:5:1, N is 50 mg/L), the ratio of air to water (air amount to inflow amount ratio) is controlled to be 1.5:1, the aerated sewage enters an expanded granular sludge bed biomembrane reactor, the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L (calculated by calcium carbonate).
(4) The aeration sewage in the water inlet regulating tank is pumped into the bottom of a main reaction area through a water inlet peristaltic pump, flows through a granular sludge bed and a fixed packed bed in sequence, and is finally discharged from a triangular water outlet weir of a three-phase separator, wherein a part of outlet water is mixed with inlet water through an internal circulating pump and enters the bottom of the main reaction area again, the internal reflux ratio is 25 percent (the other part of outlet water can be directly discharged), Dissolved Oxygen (DO) in the reactor is controlled to be 0.15-0.35 mg/L, oxidation-reduction potential (ORP) is controlled to be-300 to-350 mv, the water temperature of the system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a temperature, pH, DO and ORP multi-parameter online monitor is arranged in the reactor to monitor the pH and the micro-oxygen environment of inlet water in real time.
(5) The Hydraulic Retention Time (HRT) is gradually shortened, the rapid methane production is realized through three operation processes, the HRT in the three operation processes are respectively set for 3 days, 2.5 days and 2 days, each HRT continuously operates for 15 days (the average methane yield of the system is 500-550 m L/d after 45 days, the highest methane yield can reach 600m L/d), the COD removal rate is 92-95%, and the organic load is 0.67-1.0 kgCOD/m3·d。
(6) On the basis of methanation, adding 20-25 mg/L of Ca in the inlet water2+And 20-30 Mg/L Mg2+And promoting sludge granulation, rapidly and gradually shortening HRT after continuously running for 40 days to accelerate formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced to 1 day, 12 hours and 6 hours from 2 days, each HRT runs for 3 days, and the corresponding flow velocity of ascending water flow is increased to 5.5-6.0 m/h finally.
(7) The simulated organic wastewater is treated by the reaction treatment method for producing the methane granular sludge by using the enhanced micro-oxygen, after the process target of producing the methane aerobic granular sludge is reached, the COD of the inlet water is 2000 mg/L, the total time is about 98 days, the sludge at the bottom of the reactor is in a faint yellow rice shape, the sludge concentration M L SS is 16-20 g/L, the average sludge particle size is 1.6mm, the sludge sedimentation ratio SV is 15-30%, the gas production rate of the sludge at the upper part is good, the average methane yield is 400-600M L/d, and the COD removal rate reaches 94%.
Example 2
A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge comprises the following steps:
(1) establishing a reaction system, which mainly comprises: the system comprises a water inlet adjusting tank, a water inlet pump, an air compressor, an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), an internal circulating pump and a water outlet tank;
the EGSBBR comprises a main reaction zone and a three-phase separator, and the volume ratio is (1-1.2): 1; the lower part of the main reaction zone is provided with a granular sludge bed, and the top of the main reaction zone is provided with a fixed packed bed which accounts for 30 percent of the volume of the main reaction zone; the two areas are provided with a sampling port and an observation port, the three-phase separator is positioned at the top of the reactor and has the main functions of precipitating sludge, separating treated wastewater and collecting methane gas;
polyurethane (PU) sponge is filled in a fixed packed bed, the sponge is 8-25 mm cube, the inner hole diameter is 2-7 mm, the sponge is communicated with each other, and the carrier filling rate is controlled to be 30%.
(2) Culturing the microorganism
The sludge bed directly adopts mixed sludge of sludge in a concentration tank of an urban sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 3:1, the inoculation volume accounts for 40% of a main reaction zone, and the mixed sludge is poured into a reactor from top to bottom.
And inoculating the mixed sludge onto the polyurethane sponge filler by a sludge discharge and film hanging method through a sequencing batch reactor to form a biological carrier filler, and then putting the biological carrier filler into a fixed filler bed.
The ratio of inlet water C, N and P is 200:5:1, the carbon source is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate, and the inlet water is also added with trace element stock solution of 1m L.
The method comprises the steps of carrying out closed aeration, intermittent water feeding and continuous small-flow water feeding for 8.5 days, and carrying out culture on a cultured sludge bed M L SS at a ratio of 8-9 g/L, wherein the closed aeration, the intermittent water feeding and the continuous small-flow water feeding are carried out by filtering to remove insoluble impurities for 24h, then mixing the sludge and the fed water in an equal volume ratio, placing the mixture into a reactor, standing for 12h, carrying out aeration for 12h after the sludge is inoculated on a biological carrier filler, discharging 1/3 supernatant, adding water for repeating the process, continuously operating for 3 days, finally filling the reactor with small-flow (HRT for 4 days) continuous flow water feeding to recover the sludge activity, and continuously operating for 4 days with small-flow water feeding.
(3) After the microorganism culture, the normal water-feeding continuous operation is started
Inflow water (COD of high-concentration organic wastewater is about 4000-5000 mg/L) flows into an inflow adjusting tank, the inflow adjusting tank aerates the wastewater through an air compressor, the quality of the inflow water (C: N: P ratio is 200:5:1, N is 100-125 mg/L) and the ratio of air to water is 1.5:1, the aerated sewage enters an expanded granular sludge bed biomembrane reactor, the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L (calculated by calcium carbonate).
(4) The aeration sewage in the water inlet regulating tank is pumped into the bottom of a main body reaction area through a water inlet peristaltic pump, flows through a granular sludge bed and a fixed packed bed in sequence, and is finally discharged from a triangular water outlet weir of a three-phase separator, wherein a part of outlet water is mixed with inlet water through an internal circulating pump and enters the bottom of the main body reaction area again, the Dissolved Oxygen (DO) in the reactor with the internal reflux ratio of 50% is controlled to be 0.15-0.35 mg/L, the oxidation-reduction potential (ORP) is controlled to be-300-350 mv, the water temperature of the system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a temperature, pH, DO and ORP multi-parameter online monitor is arranged in the reactor to monitor the pH and micro-oxygen environment of inlet water in real time.
(5) The Hydraulic Retention Time (HRT) is gradually shortened, the rapid methane production is realized through three operation processes, the HRT in the three operation processes are respectively set for 3 days, 2.5 days and 2 days, each HRT continuously operates for 20 days (the average methane yield of the system is 500-550 m L/d after 60 days, the highest methane yield can reach 600m L/d), the COD removal rate is 92-95%, and the organic load is 1.34-2.5 kgCOD/m3·d。
(6) On the basis of methanation, adding 40-50 mg/L of Ca in the feed water2+And 45-50 Mg/L Mg2+And promoting sludge granulation, rapidly and gradually shortening HRT after continuously running for 60 days to accelerate formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced to 1 day, 12 hours and 6 hours from 2 days, each HRT runs for 3 days, and the corresponding flow velocity of ascending water flow is increased to 5.5-6.0 m/h finally.
(7) The simulated organic wastewater is treated by the reaction treatment method for producing the methane granular sludge by using the enhanced micro-oxygen, after the process target of producing the methane aerobic granular sludge is reached, the COD of inlet water is 4000-5000 mg/L, and the total period is about 137 days, at the moment, the sludge at the bottom of the reactor is in a faint yellow rice shape, the concentration of the sludge is M L SS: 16-20 g/L, the average particle size of the sludge is 2.2mm, the sludge sedimentation ratio SV is 15-30%, the gas production rate of upper sludge is good, the average methane yield is 900-1200M L/d, and the removal rate of the COD is 97%.
Example 3
A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge comprises the following steps:
(1) establishing a reaction system, which mainly comprises: the system comprises a water inlet adjusting tank, a water inlet pump, an air compressor, an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), an internal circulating pump and a water outlet tank;
the EGSBBR comprises a main reaction zone and a three-phase separator, and the volume ratio is (1-1.2): 1; the lower part of the main reaction zone is provided with a granular sludge bed, and the top of the main reaction zone is provided with a fixed packed bed which accounts for 20 percent of the volume of the main reaction zone; the two areas are provided with a sampling port and an observation port, the three-phase separator is positioned at the top of the reactor and has the main functions of precipitating sludge, separating treated wastewater and collecting methane gas;
polyurethane (PU) sponge is filled in a fixed packed bed, the sponge is 8-25 mm cube, the inner hole diameter is 2-7 mm, the sponge is communicated with each other, and the carrier filling rate is controlled to be 25%.
(2) Culturing the microorganism
The sludge bed directly adopts mixed sludge of sludge in a concentration tank of an urban sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 2:1, the inoculation volume accounts for 40% of a main reaction zone, and the mixed sludge is poured into a reactor from top to bottom.
And inoculating the mixed sludge onto a polyurethane sponge filler by a sludge discharge and film hanging method through a sequencing batch reactor to form a biological carrier filler, and then putting the biological carrier filler into a fixed filler bed.
The ratio of inlet water C, N and P is 200:5:1, the carbon source is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate, and the inlet water is also added with trace element stock solution of 1m L.
The method comprises the steps of carrying out closed aeration, intermittent water feeding and continuous small-flow water feeding for 3.5 days, wherein the culture time of a cultured sludge bed M L SS is 8-9 g/L, wherein the closed aeration, the intermittent water feeding and the continuous small-flow water feeding are carried out by filtering to remove insoluble impurities for 24h, then mixing the sludge and the fed water in an equal volume ratio, placing the mixture into a reactor, standing the mixture for 12h, carrying out aeration for 12h after the sludge is inoculated on a biological carrier filler, discharging 1/3 supernatant, adding the fed water, repeating the process for 1 day, finally filling the reactor with the continuous small-flow water feeding (HRT is 4 days) to recover the sludge activity, and then carrying out the continuous small-flow water feeding for 24 h.
(3) After the microorganism culture, the normal water-feeding continuous operation is started
Inflow water (COD of high-concentration organic wastewater is about 2000-3000 mg/L) flows into an inflow adjusting tank, the inflow adjusting tank aerates the inflow water through an air compressor, the quality of the inflow water (C: N: P ratio is 200:5:1, N is 50-75 mg/L) and the ratio of air to water is 1.5:1, the aerated sewage enters an expanded granular sludge bed biomembrane reactor, the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L (calculated by calcium carbonate).
(4) The aeration sewage in the water inlet regulating tank is pumped into the bottom of a main reaction area through a water inlet peristaltic pump, flows through a granular sludge bed and a fixed packed bed in sequence, and is finally discharged from a triangular water outlet weir of a three-phase separator, wherein a part of outlet water is mixed with inlet water through an internal circulating pump and enters the bottom of the main reaction area again, the internal reflux ratio is 30 percent (the other part of outlet water can be directly discharged), Dissolved Oxygen (DO) in the reactor is controlled to be 0.15-0.35 mg/L, oxidation-reduction potential (ORP) is controlled to be-300 to-350 mv, the water temperature of the system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a temperature, pH, DO and ORP multi-parameter online monitor is arranged in the reactor to monitor the pH and the micro-oxygen environment of inlet water in real time.
(5) The Hydraulic Retention Time (HRT) is gradually shortened, the rapid methane production is realized through three operation processes, the HRT in the three operation processes are respectively set for 3 days, 2.5 days and 2 days, each HRT is continuously operated for 18 days (the average methane yield of the system is 500-550 m L/d after 54 days, the highest methane yield can reach 600m L/d), the COD removal rate is 92-95%, and the organic load is 0.67-1.5 kgCOD/m3·d。
(6) On the basis of methanation, adding 30-40 mg/L of Ca in the feed water2+And 30-40 Mg/L Mg2+Promoting sludge granulation, rapidly and gradually shortening HRT after continuously running for 44 days to accelerate formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced to 1 day, 12 hours and 6 hours from 2 days, each HRT runs for 3 days, the corresponding flow velocity of ascending water flow is increased to 5.5-6.2 m/h finally.0m/h。
(7) The simulated organic wastewater is treated by the reaction treatment method for producing methane granular sludge by using the enhanced micro-oxygen, after the process target of producing methane aerobic granular sludge is reached, the COD of inlet water is 2000-3000 mg/L, the total period is about 110 days, at the moment, the sludge at the bottom of the reactor is in a faint yellow rice shape, the sludge concentration M L SS is 16-20 g/L, the average sludge particle size is 1.2mm, the sludge sedimentation ratio SV is 15-30%, the gas production rate of upper sludge is good, the average methane yield is 600-800M L/d, and the removal rate of the COD is 95%.
Example 4
A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge comprises the following steps:
(1) establishing a reaction system, which mainly comprises: the system comprises a water inlet adjusting tank, a water inlet pump, an air compressor, an Expanded Granular Sludge Bed Biofilm Reactor (EGSBBR), an internal circulating pump and a water outlet tank;
the EGSBBR comprises a main reaction zone and a three-phase separator, and the volume ratio is (1-1.2): 1; the lower part of the main reaction zone is provided with a granular sludge bed, and the top of the main reaction zone is provided with a fixed packed bed which accounts for 25 percent of the volume of the main reaction zone; the two areas are provided with a sampling port and an observation port, the three-phase separator is positioned at the top of the reactor and has the main functions of precipitating sludge, separating treated wastewater and collecting methane gas;
polyurethane (PU) sponge is filled in a fixed packed bed, the sponge is 8-25 mm square, the inner hole diameter is 2-7 mm, the sponge is communicated with each other, and the carrier filling rate is controlled to be 20%.
(2) Culturing the microorganism
The sludge bed directly adopts mixed sludge of sludge in a concentration tank of an urban sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 2.5:1, the inoculation volume accounts for 40% of the main reaction zone, and the mixed sludge is poured into the reactor from top to bottom.
And inoculating the mixed sludge onto a polyurethane sponge filler by a sludge discharge and film hanging method through a sequencing batch reactor to form a biological carrier filler, and then putting the biological carrier filler into a fixed filler bed.
The ratio of inlet water C, N and P is 200:5:1, the carbon source is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate, and the inlet water is also added with trace element stock solution of 1m L.
The method comprises the steps of carrying out closed aeration, intermittent water feeding and continuous small-flow water feeding, wherein 8-9 g/L of cultured sludge bed M L SS is cultured for 5.5 days, wherein the closed aeration, the intermittent water feeding and the continuous small-flow water feeding are carried out by filtering to remove insoluble impurities for 24 hours, then mixing the sludge and the fed water in an equal volume ratio, placing the mixture into a reactor, standing the mixture for 12 hours, carrying out aeration for 12 hours after the sludge is inoculated on a biological carrier filler, discharging 1/3 supernatant, adding the fed water, repeating the process for 2 days, finally filling the reactor with the continuous small-flow (HRT is 4 days) water to restore the sludge activity, and then carrying out continuous small-flow water feeding for 2 days.
(3) After the microorganism culture, the normal water-feeding continuous operation is started
Inflow water (COD of high-concentration organic wastewater is about 1200-2000 mg/L) flows into an inflow adjusting tank, the inflow adjusting tank aerates the inflow water through an air compressor, the quality of the inflow water (C: N: P ratio is 200:5:1, N is 30-50 mg/L) and the ratio of air to water is 1.5:1, the aerated sewage enters an expanded granular sludge bed biomembrane reactor, the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L (calculated by calcium carbonate).
(4) The aeration sewage in the water inlet regulating tank is pumped into the bottom of a main reaction area through a water inlet peristaltic pump, flows through a granular sludge bed and a fixed packed bed in sequence, and is finally discharged from a triangular water outlet weir of a three-phase separator, wherein a part of outlet water is mixed with inlet water through an internal circulating pump and enters the bottom of the main reaction area again, the internal reflux ratio is 45 percent (the other part of outlet water can be directly discharged), Dissolved Oxygen (DO) in the reactor is controlled to be 0.15-0.35 mg/L, oxidation-reduction potential (ORP) is controlled to be-300 to-350 mv, the water temperature of the system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a temperature, pH, DO and ORP multi-parameter online monitor is arranged in the reactor to monitor the pH and the micro-oxygen environment of inlet water in real time.
(5) Gradually shortening Hydraulic Retention Time (HRT), realizing rapid methane production through three operation processes, and realizing three operation processes of HRTSetting 3 days, 2.5 days and 2 days respectively, continuously operating each HRT for 15 days (the average methane yield of the system is 500-550 m L/d and can reach 600m L/d after 45 days), wherein the COD removal rate is 92-95%, and the organic load is 0.4-1.0 kgCOD/m3·d。
(6) On the basis of methanation realization, adding 35-45 mg/L of Ca in the inlet water2+And 40-45 Mg/L Mg2+And promoting sludge granulation, rapidly and gradually shortening HRT after continuously running for 41 days to accelerate formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced to 1 day, 12 hours and 6 hours from 2 days, each HRT runs for 3 days, and the corresponding flow velocity of ascending water flow is increased to 5.5-6.0 m/h finally.
(7) The simulated organic wastewater is treated by the reaction treatment method for producing methane particle sludge by using the enhanced micro-oxygen, after the process target of producing methane aerobic particle sludge is reached, the COD of the inlet water is 1200-2000 mg/L, the total period is about 110 days, the sludge at the bottom of the reactor is in a faint yellow rice shape, the sludge concentration M L SS is 16-20 g/L, the average particle size of the sludge is 1.1mm, the sludge sedimentation ratio SV is 15-30%, the gas production rate of the sludge at the upper part is good, the average methane yield is 300-400M L/d, and the removal rate of the COD is 93%.
While specific embodiments of the invention have been described above, it will be appreciated by those skilled in the art that the above examples are not intended to limit the invention in any way and that any arrangement which is calculated to achieve the above objectives, such as variations, modifications, equivalents, or equivalent arrangements, will fall within the scope of the invention.

Claims (6)

1. A reaction treatment method for enhancing micro-aerobic methanogenic granular sludge is characterized by comprising the following steps: the method comprises the following steps:
(1) establishing a reaction system comprises: the system comprises a water inlet adjusting tank (1), a water inlet peristaltic pump (2), an expanded granular sludge bed biomembrane reactor (16), an internal circulating pump (11) and an air compressor (12);
the expanded granular sludge bed biofilm reactor (16) comprises a main reaction zone (17) and a three-phase separator (6), and the volume ratio is 1-1.2: 1; the lower part of the main reaction zone (17) is provided with a granular sludge bed (4), the top of the main reaction zone (17) is provided with a fixed packed bed (5), and the fixed packed bed (5) accounts for 20-30% of the volume of the main reaction zone (17); the three-phase separator (6) is positioned at the top of the reactor, and the main reaction zone (17) and the three-phase separator (6) are both provided with a sampling port and an observation port;
polyurethane sponge is filled in the fixed packed bed (5), the polyurethane sponge is 8-25 mm cube, the inner aperture is 2-7 mm, and the carrier filling rate is 20% -30%;
(2) culturing the microorganism
The sludge bed directly adopts mixed sludge of sludge in a concentration tank of a municipal sewage treatment plant and sludge in an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 2-3: 1, and the inoculation volume accounts for 40% of the main reaction zone;
inoculating the mixed sludge to polyurethane sponge filler by a sludge discharge and film hanging method through a sequencing batch reactor to form biological carrier filler, and then putting the biological carrier filler into a fixed packed bed (5);
feeding water with the ratio of C to N to P being 200:5:1, carrying out closed aeration, intermittent water feeding and continuous small-flow water feeding, wherein the culture time is 3.5-8.5 days, and the cultured sludge bed M L SS is 8-10 g/L;
(3) after the microorganism culture, the normal water-feeding continuous operation is started
The method comprises the following steps that inflow water flows into an inflow adjusting tank (1), the inflow water is aerated in the inflow adjusting tank (1) through an air compressor (12), the aerated sewage enters an expanded granular sludge bed biofilm reactor (16), the pH value of the inflow water is 7.0-7.3, and the alkalinity is 500-800 mg/L;
(4) the aeration sewage in the water inlet regulating tank (1) is pumped into the bottom of a main reaction area (17) through a water inlet peristaltic pump (2), sequentially flows through a granular sludge bed (4) and a fixed packed bed (5), and is finally discharged from a triangular water outlet weir (8) of a three-phase separator (6), wherein a part of the outlet water is mixed with inlet water through an internal circulating pump (11) and enters the bottom of the main reaction area (17) again, the internal reflux ratio is 20-50%, dissolved oxygen DO in the reactor is controlled to be 0.15-0.35 mg/L, oxidation reduction potential ORP is controlled to be-300-350 mv, the water temperature of a system is guaranteed to be 35 +/-2 ℃ through a heating temperature controller, and a multi-parameter monitor for monitoring the pH and the DO of the inlet water and the micro-oxygen environment is arranged in the reactor in real time;
(5) the hydraulic retention time HRT is gradually shortened, the rapid methane production is realized through three operation processes, the three operation processes HRT are respectively set for 3 days, 2.5 days and 2 days, and each HRT continuously operates for 15-20 days; at this time, the COD removal rate is 92-95%, and the organic load is 0.4-2.5 kgCOD/m3·d；
(6) On the basis of methanation, adding 20-50 mg/L of Ca into the feed water2+And 20-50 Mg/L Mg2+Promoting sludge granulation, and rapidly and gradually shortening HRT after continuously running for 40-60 days to accelerate formation of aerobic granular sludge in a mode of increasing the flow velocity of ascending water flow, wherein the HRT is respectively reduced from 2 days to 1 day, 12 hours and 6 hours, and each HRT runs for 3-5 days;
(7) after the process target of producing the methane aerobic granular sludge is achieved, the sludge at the bottom of the reactor is in a faint yellow rice grain shape, the sludge concentration M L SS is 16-20 g/L, the average sludge particle size is 1.0-2.5 mm, the sludge sedimentation ratio SV is 15-30%, the gas yield of the upper sludge is 300-1200M L/d, and the COD removal rate is more than 90%.
2. The method for treating the micro-aerobic methanogenic granular sludge through the reaction of the micro-aerobic methanogenic granular sludge as claimed in claim 1, wherein: in the step (2), the carbon source in the inlet water is glucose or sodium acetate, the nitrogen source is ammonium chloride, ammonium sulfate or urea, and the phosphorus source is potassium dihydrogen phosphate or potassium hydrogen phosphate.
3. The method for treating the micro-aerobic methanogenic granular sludge through the reaction of the micro-aerobic methanogenic granular sludge as claimed in claim 2, wherein: in the step (2), a trace element stock solution is also added into the inlet water, and the trace element stock solution is as follows:
FeCl3·4H2O：2000mg/L，CoCl2·6H2O：2000mg/L，MnCl2·4H2O：500mg/L，CuCl2·2H2O：30mg/L，ZnCl2：50mg/L，H3BO3：50mg/L，(NH4)6Mo7O24·4H2O：90mg/L，Na2SeO3：100mg/L，NiCl2·6H2O：50mg/L，EDTA：1000mg/L。
4. the method for treating the micro-aerobic methanogenic granular sludge reaction enhancement according to claim 3, wherein: in the step (2), the stuffy aeration, the intermittent water inflow and the continuous small-flow water inflow are specifically as follows:
firstly, filtering to remove insoluble impurities, and carrying out stuffy aeration for 24 hours; then mixing the sludge and inlet water in equal volume proportion, placing the mixture into a reactor, and standing for 12 hours; aerating for 12 hours after the sludge is inoculated on the biological carrier filler, draining 1/3 supernatant, adding inflow water, and repeating the process for 1-3 days; and finally, filling the reactor with small-flow continuous inflow water to restore the sludge activity, and continuously operating the reactor for 1-4 days with small-flow inflow water.
5. The method for treating the micro-aerobic methanogenic granular sludge reaction enhancement according to claim 4, wherein: the small flow rate of inlet water is HRT for 4 days.
6. A reaction system for strengthening micro-aerobic methanogenic granular sludge is characterized in that: the method comprises the following steps: the system comprises a water inlet adjusting tank (1), a water inlet peristaltic pump (2), an expanded granular sludge bed biomembrane reactor (16), an internal circulating pump (11) and an air compressor (12);
the expanded granular sludge bed biofilm reactor (16) comprises a main reaction zone (17) and a three-phase separator (6), and the volume ratio is 1-1.2: 1; the lower part of the main reaction zone (17) is provided with a granular sludge bed (4), the top of the main reaction zone (17) is provided with a fixed packed bed (5), and the fixed packed bed (5) accounts for 20-30% of the volume of the main reaction zone (17); the main reaction zone (17) and the three-phase separator (6) are both provided with a sampling port (9) and an observation port;
polyurethane sponge is filled in the fixed packed bed (5), the polyurethane sponge is 8-25 mm cube, the inner aperture is 2-7 mm, and the carrier filling rate is 20% -30%;
the granular sludge bed (4) adopts mixed sludge of concentrated tank sludge of an urban sewage treatment plant and sludge of an aerobic aeration tank as inoculation sludge, the mixing mass ratio is 2-3: 1, and the inoculation volume accounts for 40% of that of the main reaction zone (17);
a mass flow meter (13) is mounted on an outlet pipeline of the air compressor (12) and then the outlet pipeline is introduced into the water inlet adjusting tank (1), an outlet at the bottom of the water inlet adjusting tank (1) is connected with an inlet at the bottom of a main body reaction zone (17) of the expanded granular sludge bed biofilm reactor (16) through a water inlet peristaltic pump (2), a triangular water outlet weir (8) of a three-phase separator (6) of the expanded granular sludge bed biofilm reactor (16) is communicated with an inlet at the bottom of the main body reaction zone (17) through an internal circulating pump (11), and a water outlet (18) is additionally connected to the triangular water outlet weir (8); a wet gas flowmeter (14) is installed on a gas collecting port (7) of the three-phase separator (6).
CN202010370263.7A 2020-05-06 2020-05-06 Reaction system and treatment method for enhancing micro-aerobic methane-producing granular sludge Pending CN111484133A (en)

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