CN115261231A - Method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge - Google Patents
Method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 61
- 239000010802 sludge Substances 0.000 title claims abstract description 37
- 239000005014 poly(hydroxyalkanoate) Substances 0.000 title abstract description 50
- 229920000903 polyhydroxyalkanoate Polymers 0.000 title abstract description 50
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 50
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 238000005273 aeration Methods 0.000 claims abstract description 18
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- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 18
- 239000001301 oxygen Substances 0.000 claims abstract description 18
- 230000004060 metabolic process Effects 0.000 claims abstract description 16
- 239000000126 substance Substances 0.000 claims abstract description 14
- 239000000203 mixture Substances 0.000 claims abstract description 13
- 235000015097 nutrients Nutrition 0.000 claims abstract description 12
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- 238000007599 discharging Methods 0.000 claims abstract description 10
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000012544 monitoring process Methods 0.000 claims abstract description 6
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- 235000013379 molasses Nutrition 0.000 claims description 5
- 229910000402 monopotassium phosphate Inorganic materials 0.000 claims description 4
- 235000019796 monopotassium phosphate Nutrition 0.000 claims description 4
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 claims description 4
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- 238000005728 strengthening Methods 0.000 abstract description 3
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- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- -1 ammonium ions Chemical class 0.000 description 2
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1263—Sequencing batch reactors [SBR]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/004—Apparatus and plants for the biological treatment of water, waste water or sewage comprising a selector reactor for promoting floc-forming or other bacteria
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
Abstract
The invention provides a method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge, which comprises the following steps: putting activated sludge into a sequencing batch reactor, setting each reaction period to be 12 hours, feeding water, operating the reactor, putting a carbon source and a biological metabolism nutrient substance, and adding thiourea to inhibit the nitrification process in the reactor, so that the reactor is in a continuous aerobic aeration state; monitoring the dissolved oxygen concentration in the reactor, and when the dissolved oxygen concentration is suddenly changed to be more than 2 times of the last monitoring result, adding a nitrogen source to ensure that the C/N ratio in the solution in the reactor is 100 to 6; and discharging part of the mud-water mixture when the periodic reaction time is over, then supplementing carbon sources and biological metabolism nutrient substances, and entering the next reaction period. The technical scheme of the invention adopts a method of 'strengthening anabolism-growth metabolism' alternate operation, compared with the traditional process, under the conditions of the same time, carbon source and the like, the synthesis capacity of PHA is improved by 2 times, and the enrichment is more stable.
Description
Technical Field
The invention belongs to the field of sludge recycling and waste resource recovery, and particularly relates to a method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge.
Background
The treatment and utilization of activated sludge and the recycling of waste resources are important rings for realizing closed-loop carbon circulation in the field of sewage treatment, and are important ways for realizing carbon neutralization. The activated sludge contains a large amount of aerobic microorganisms with strong adaptability, the microorganisms can perform metabolic activities related to cell growth and propagation by taking various wastes as carbon sources, and part of flora has the capacity of producing polyhydroxyalkanoate in the metabolic process. The polyhydroxyalkanoate is biological polyester with good physicochemical properties, has good biocompatibility, biodegradability and other properties, is widely concerned as a biological product capable of replacing the traditional petroleum-based plastics, omits an expensive sterilization process of pure bacteria production by using activated sludge as a matrix and combining waste as a carbon source substrate for production, saves the cost of the carbon source substrate, and is a high-value production method.
PHA production is traditionally carried out by adopting a three-stage reaction, which relates to three processes: substrate fermentation process, PHA-producing flora enrichment process and PHA batch reaction synthesis. The equipment relates to an anaerobic fermentation and aerobic sequencing batch reactor and an aerobic batch feed supplement fermentation reactor. The core of the process is an enrichment process of PHA-producing floras, the process runs based on an alternate 'satiation-starvation' mode, microorganisms realize cell growth in a satiation stage and utilize a part of carbon source to produce PHA, the process enters a starvation stage after the consumption of carbon source substrate is finished, floras which do not have PHA-producing capacity lose competitive capacity and are gradually eliminated due to long-term starvation due to lack of nutrition in the stage, the structure of floras in a reactor is changed, and the floras which have PHA-producing capacity gradually become dominant bacteria. And when the PHA is enriched to a certain abundance, performing batch synthesis production of PHA by using bacterial sludge produced by the enrichment reactor as a matrix. In the batch synthesis reactor, the microbial metabolic process is continuously maintained in the direction of accumulation metabolism by adding carbon sources in batches for multiple times to produce PHA. However, the whole operation process needs to be operated by three sets of independent devices, the equipment and operation cost is high, and the highest cost is the enrichment reactor. In addition, the traditional ADF process is relatively slow in enrichment process, long in stable operation time, special in substrate concentration, incapable of directly using high-concentration substrates, and needs to dilute high-concentration carbon source substrates, so that the waste of water resources and substrates is serious. Based on the above, a two-step synthesis method in a single reactor has been developed, but conditions are not perfect, so that the biomass content is not improved, and the yield is difficult to improve.
Disclosure of Invention
In view of the above, the invention discloses a method for efficiently enriching PHA-producing flora from activated sludge, which adopts integrated equipment and is based on a C/N non-coupled process, accelerates the process of enriching PHA-producing flora, and solves the problems that the enrichment process in the prior art is long in time and the biomass yield is difficult to improve.
In contrast, the technical scheme adopted by the invention is as follows:
a method for efficiently enriching PHA-producing flora from activated sludge, comprising:
putting activated sludge into a sequencing batch reactor, setting each reaction period to be 12 hours, feeding water, operating the reactor, putting a carbon source and a biological metabolism nutrient substance, and adding thiourea to inhibit the nitrification process in the reactor, so that the reactor is in a continuous aerobic aeration state;
monitoring the concentration of dissolved oxygen in the reactor, and adding a nitrogen source when the concentration of the dissolved oxygen is more than 2 times of the last monitoring result, so that the C/N ratio in the solution in the reactor is 100-100; and discharging part of the mud-water mixture when the periodic reaction time is over, then supplementing carbon sources and biological metabolism nutrient substances, and entering the next reaction period.
By adopting the technical scheme, the single reaction period is divided into two stages, wherein the first stage is a metabolite accumulation stage, and the second stage is a microorganism proliferation stage. Sufficient carbon sources and nutrient substances necessary for biological metabolism are initially added in a metabolite accumulation period, thiourea is added to inhibit a nitrification process in the reactor, and the reactor is in a continuous aerobic aeration state, so that microorganisms continuously obtain the carbon sources and convert the carbon sources into energy storage substances such as PHA (polyhydroxyalkanoate). When the dissolved oxygen concentration is suddenly increased, marking the reactor to enter a second stage, namely a microorganism multiplication stage, and supplementing a nitrogen source into the reactor at the beginning of the microorganism multiplication stage. And discharging part of the mud-water mixture when the periodic reaction time is over, and then supplementing sufficient carbon sources and nutrient elements to enter the next reaction period. The operation can peel off two processes of PHA accumulation by the microorganisms and growth of the microorganisms, so that the two processes are independent from each other and form a continuous process, the microorganisms accumulate PHA in a metabolite accumulation period, and then the endogenous substances are utilized to replicate and increase the value after the substrate is completely consumed in the second stage, so that the enrichment speed of the PHA flora can be effectively improved.
As a further improvement of the invention, 1L of carbon source with a COD concentration of 4000mg/L is added.
As a further improvement of the invention, the carbon source substrate is a high COD concentration substrate containing no or less nitrogen; further, the COD of the carbon source substrate: ammonia nitrogen >100:0.5.
further, the substrate of the carbon source is molasses wastewater, crude glycerol or cheese wastewater. By adopting the technical scheme, the molasses wastewater can be efficiently utilized, and anaerobic fermentation process devices are saved.
As a further improvement of the invention, the biological metabolism nutrient comprises substances containing Ca ions, mg ions and Zn ions.
As a further improvement of the invention, a nitrogen source is added so that the C/N ratio in the solution in the reactor is 100. By adopting the technical scheme, the enrichment speed of the PHA flora is high, and the biomass yield can be improved within the same time. Further, at the end of each reaction cycle, half of the total volume of the slurry mixture was discharged. By adopting the technical scheme, the concentration of the flora in the reactor can be improved, and the yield per unit volume can be improved. Such continuous operation can enrich large amount of PHA flora in a short time and improve the flora yield.
As a further improvement of the invention, a nitrogen source is added, the C/N ratio in the solution in the reactor is 100. By adopting the technical scheme, the retention time of the activated sludge can be controlled to be about 3 days, the content of the activated sludge in the reactor is increased, the yield of the biomass is improved by adjusting the C/N ratio to be 3, and the SRT is controlled to be 1 day.
As a further improvement of the invention, the nitrogen source comprises potassium dihydrogen phosphate or NH 4 Cl。
As a further improvement of the invention, after water is fed in, an aeration pump is started to work, the aeration rate is adjusted to ensure that the minimum dissolved oxygen of the solution in the reactor is more than 2mg/L, and the reactor is in a continuous aerobic aeration state, so that microorganisms continuously obtain a carbon source and convert the carbon source into energy storage substances such as PHA and the like.
Compared with the prior art, the invention has the beneficial effects that:
firstly, the technical scheme of the invention adopts an operation process method of 'strengthening anabolism-growth metabolism' alternation, so that compared with the traditional process, the synthesis capacity of PHA of the reactor is improved by 2 times under the conditions of the same time, carbon source and the like, and the enrichment stability effect is better. Aiming at the improvement of SRT, the yield of the activated sludge biomass in the reactor is improved by 4 times under other conditions of the same C/N ratio and the like in the C/N non-coupling process. In addition, the proper C/N ratio is adopted, so that the content of the activated sludge in the reactor is improved by 50 percent, the maximum PHA content is improved by one time, and the comprehensive unit volume yield is improved by 50 percent under the same SRT and other conditions in the C/N non-coupled process.
Secondly, by adopting the technical scheme of the invention, the used carbon source can be an organic carbon source without ammonium ions or ammonium ions, and the high-efficiency resource recovery of wastes can be realized. Meanwhile, the device can also be applied to industrial wastewater treatment and the like, and a large amount of activated sludge required by the device startup provides an effective way for sludge disposal of sewage plants.
Thirdly, the molasses wastewater can be used as a carbon source substrate in the technical scheme of the invention, so that the molasses wastewater can be efficiently utilized after the adaptation period, anaerobic fermentation process devices are saved, and the device cost is reduced again.
Drawings
FIG. 1 is a schematic structural view of a reaction apparatus used in an embodiment of the present invention.
FIG. 2 is a comparison of the ADF process after 30 days of operation of an embodiment of the present invention versus the maximum synthesis capacity of the present process.
Detailed Description
Preferred embodiments of the present invention are described in further detail below.
A method for efficiently enriching PHA-producing flora from activated sludge, comprising:
activated sludge from a water plant is put into a sequencing batch reactor, and the device realizes the control and regulation of the reactor by using an automatic control device based on PLC control, as shown in figure 1, a single reaction period is set to be 12h, and the single reaction period is divided into two stages. The first phase is a metabolite accumulation phase and the second phase is a microorganism proliferation phase. Sufficient carbon source and nutrient elements necessary for biological metabolism, such as Ca, mg, zn and other necessary ions are put into the initial stage of metabolite accumulation.
Thiourea is added to inhibit the nitrification process in the reactor, and the reactor is in a continuous aerobic aeration state, so that microorganisms continuously obtain a carbon source and convert the carbon source into energy storage substances such as PHA and the like. Detecting the dissolved oxygen concentration, and marking the microorganism proliferation stage when the dissolved oxygen concentration is suddenly increased. And (3) adding a nitrogen source after the jump to enable the microorganisms to enter a proliferation stage, wherein the nitrogen source can be prepared by adopting potassium dihydrogen phosphate or ammonium chloride.
The C/N ratio can be controlled to be 100, the hydraulic retention time is 1 day, and the sludge retention time is 1 day. And discharging a half of the muddy water mixture when the periodic reaction time is over, so that the one-period reaction is over. Then sufficient carbon source and nutrient elements are added to enter the next reaction period.
In order to improve the concentration of the flora in the reactor and finally improve the yield of unit volume, a plurality of parameters of the process are adjusted and operated, and the method comprises the following steps:
the biomass yield is improved by improving the SRT, the process operation conditions and parameters are basically controlled as above, the C/N ratio is controlled to be 100, the sludge-water mixture amount per period is changed to be 1/4 of the volume, the retention time of the activated sludge is controlled to be about 3 days, and the content of the activated sludge in the reactor is increased.
The biomass yield can also be improved by adjusting the C/N ratio, controlling the SRT to be 1 day, controlling the C/N ratio to be 100, the hydraulic retention time to be 1 day and the sludge retention time to be 1 day, and the process is found to improve the flora concentration in the reactor and improve the yield per unit volume. Such continuous operation can enrich large amount of PHA flora in a short time and improve the flora yield.
The following description will be given with reference to specific examples.
Example 1
The equipment startup period is as follows: the activated sludge from the secondary sedimentation tank of the water plant is put into the device, the device uses a 2L automatic sequencing batch reactor controlled based on a PLC controller, and the aeration pump, the water inlet and outlet pumps, the dosing pumps and the like are programmed and controlled by the PLC controller to realize autonomous operation, so that the purposes of automatic control and adjustment of the reactor are achieved. The reaction time of a single period in the reactor is set to be 12h, the hydraulic retention time is 1d, and the sludge age SRT is 1d. The reactor has a daily water inlet load of 4000mg COD/d/L, sufficient phosphorus source in the inlet water, potassium dihydrogen phosphate is used for configuration, and the total COD to P is about 100 to 1. Thiourea is added to the feed water to inhibit the nitration process in the reactor. The reaction period is divided into two stages. The first stage is a metabolite accumulation period, firstly, when the accumulation period starts, a water inlet pump is started, water containing a carbon source substrate enters 1L after the water inlet pump works for 10min, the concentration content of the substrate is 4000mg COD/L, a medicine adding pump is started while the substrate enters, 10ml of trace elements are added, and the concentration of a trace element solution is shown in Table 1:
TABLE 1
| 1 | Na 2 MoO 4 ·2H 2 O | 0.06g/L | 6 | CaCl 2 ·7H 2 O | 0.15g/L |
| 2 | H 3 BO 4 | 0.15g/L | 7 | ZnSO 4 ·7H 2 O | 0.12g/L |
| 3 | KI | 1.18g/L | 8 | MnCl 4 ·H 2 O | 0.12g/L |
| 4 | CuSO 4 ·5H 2 O | 0.03g/L | 9 | FeCl 3 ·6H 2 O | 1.5g/L |
| 5 | EDTA | 3g/ |
10 | MgSO 4 | 2.5g/L |
After water is fed, the aeration pump starts to work, the lowest dissolved oxygen is controlled to be more than 2mg/L by pre-adjusting the aeration amount to be 3L/min, the reactor is in a continuous aerobic aeration state, so that microorganisms continuously obtain a carbon source and convert the carbon source into energy storage substances such as PHA (polyhydroxyalkanoate), the dissolved oxygen concentration is suddenly increased from 2mg/L to more than 6mg/L after the substrate is completely consumed, and the mark metabolism accumulation period is ended. The dissolved oxygen burst signal is transmitted to a pre-programmed PLC controller through an RS485 communication bus, automatic control is triggered, a nitrogen source dosing pump is controlled to be started, 5ml of nitrogen source is added into the reactor, and NH is used as the nitrogen source 4 Cl was prepared at a concentration of 142g/L. So that the total cycle of reactor feed water C: n is maintained at 100: about 6. The periodic reaction is finished after the period of 11h50min from the beginning of water inlet is preset, the controller controls the peristaltic pump to start, sludge and water are discharged, the running time is 10min, half of the sludge-water mixture, namely 1L, is discharged, and the reaction period is finished. The above control is repeated to proceed to the next cycle of reaction. The time of each cycle is: adding carbon source, feeding for 10min, and aerating for 10h30min, wherein when the oxygen concentration of the solution suddenly rises, adding 5ml of nitrogen source, discharging 1L of sludge-water mixture for 10min after the aeration time, and precipitating for 1h.
Because a trace amount of residual nitrogen source exists in the reactor at the end of the reactor period, the microorganisms at the beginning of the next enrichment operation period can utilize a certain nitrogen source to perform related protein synthesis activities, and the initial metabolic activity is higher than that of the traditional ADF process, thereby realizing the alternative screening process of 'strengthening anabolism-growth metabolism'.
Example 2
In addition to example 1, the amount of the nitrogen source to be added was changed so that the mass ratio of C to N was maintained at 100. The whole process is as follows: and (3) adding a carbon source, feeding for 10min, and aerating for 10h and 30min, wherein 2.5ml of nitrogen source is added after the oxygen concentration of the solution suddenly jumps, and discharging 1L of sludge-water mixture for 10min and precipitating for 1h after the aeration time expires.
Example 3
Based on example 1, the amount of the nitrogen source to be added was changed so that the mass ratio of C to N was maintained at 100. The whole process is as follows: adding carbon source, feeding for 10min, and aerating for 10h30min, wherein 2.5ml nitrogen source is added after the oxygen concentration of the solution suddenly jumps, discharging 330ml mud-water mixture for 10min after the aeration time is up, precipitating for 1h, and discharging water for 7min.
Comparative example
Compared with the prior art, the ADF method has the process conditions that a carbon source and a nitrogen source are fed simultaneously, the mass ratio of C to N is controlled to be 100, feeding is carried out for 10min, aeration is carried out for 10h and 30min, sludge is discharged for 10min after each reaction period, precipitation is carried out for 1h, and SRT is 1d.
Table 1 shows the operating kinetic parameters of examples 1 to 3 and comparative examples
Remarking: q. q.s s Specific uptake rate of substrate per unit time, q PHA Is the product ratio generation rate per flora per unit time, Y PHA/s For substrate/product conversion, V PHA Is the amount of PHA produced per day per unit volume of reactor.
The operation is carried out for 50 days for examples 1 to 3 and comparative example, and the obtained maximum PHA content ratio is shown in FIG. 2, and it can be seen that the maximum PHA content is higher than that of the comparative example by adopting the technical schemes of the examples 1 and 2.
At 50 days of the same enrichment, the method of example 1 (C: N100: 6SRT 1d) increased 1.6 times the maximum PHA content of the comparative ADF process (C: N100:3SRT1 d) and 1 time the conditions of the same C/N uncoupled process of example 2 (C: N100:3SRT1 d). Compared with the product obtained in the same process of example 3 (C: N100:3 SRT3d), the product is improved by 3 times.
Meanwhile, compared with example 2 under the same conditions (C: N100: 6SRT 1d) in the process, in example 1 (C: N100. As can be seen, example 3 had the highest biomass yield, while increasing the maximum intracellular content of PHA, with a combined unit volume yield of 6719.939mg COD PHA/L d. Next, example 2.
The comprehensive unit volume yield of example 3 is improved by 5 times compared with the yield of 1152.073mg COD PHA/L d of the comparative conventional ADF process under the same conditions, and is improved by 50% compared with the effect of 4134.167mg COD PHA/L d operated under the same process (C: N100.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions or substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (8)
1. A method for efficiently enriching PHA-producing flora from activated sludge, which is characterized by comprising the following steps:
putting activated sludge into a sequencing batch reactor, setting each reaction period to be 12 hours, feeding water, operating the reactor, putting a carbon source and a biological metabolism nutrient substance, and adding thiourea to inhibit the nitrification process in the reactor, so that the reactor is in a continuous aerobic aeration state;
monitoring the dissolved oxygen concentration in the reactor, and when the dissolved oxygen concentration is suddenly changed to be more than 2 times of the last monitoring result, adding a nitrogen source to ensure that the C/N ratio in the solution in the reactor is 100 to 6; and discharging part of the muddy water mixture when the periodic reaction time is over, then supplementing a carbon source and a biological metabolism nutrient substance, and entering the next reaction period.
2. The method for the efficient enrichment of PHA-producing flora from activated sludge according to claim 1, wherein the substrate of said carbon source is molasses wastewater, raw glycerol or cheese wastewater.
3. The method as recited in claim 1, wherein said biological nutrient comprises Ca, mg, zn containing substances.
4. The method for efficiently enriching PHA-producing flora from activated sludge according to claim 1, wherein: and (3) adding a nitrogen source to ensure that the C/N ratio in the solution in the reactor is 100.
5. The method of claim 4, wherein the PHA-producing flora is efficiently enriched in activated sludge, and the method comprises: at the end of each reaction cycle, half the total volume of the slurry mixture was discharged.
6. The method for efficiently enriching PHA-producing flora from activated sludge according to claim 1, wherein: and (3) adding a nitrogen source, wherein the C/N ratio in the solution in the reactor is 100, and discharging a muddy water mixture with the total volume of 1/4 at the end of each reaction period.
7. The method for efficiently enriching PHA-producing flora from activated sludge as claimed in any one of claims 1~6, wherein: the nitrogen source comprises potassium dihydrogen phosphate or NH 4 Cl。
8. The method for efficiently enriching PHA-producing flora from activated sludge as claimed in any one of claims 1~6, wherein: after the water is fed in, the aeration pump is started to work, the aeration amount is adjusted to ensure that the minimum dissolved oxygen of the reactor solution is more than 2mg/L, and when the dissolved oxygen concentration is increased from 2mg/L to more than 6mg/L, the nitrogen source is added.
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