CN106978346A - A kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity - Google Patents
A kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity Download PDFInfo
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- 241000894006 Bacteria Species 0.000 title claims abstract description 71
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 50
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000000758 substrate Substances 0.000 claims abstract description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 25
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 25
- 230000012010 growth Effects 0.000 claims abstract description 11
- 238000003860 storage Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 238000005273 aeration Methods 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 9
- 150000007524 organic acids Chemical class 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 6
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerol Natural products OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 6
- 244000005700 microbiome Species 0.000 claims description 6
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 claims description 4
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims description 4
- 235000016709 nutrition Nutrition 0.000 claims description 4
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- 235000011187 glycerol Nutrition 0.000 claims description 3
- 230000035764 nutrition Effects 0.000 claims description 3
- 244000039328 opportunistic pathogen Species 0.000 claims description 2
- 229910052698 phosphorus Inorganic materials 0.000 claims description 2
- 235000019260 propionic acid Nutrition 0.000 claims description 2
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 claims description 2
- 229940005605 valeric acid Drugs 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims 1
- 235000005985 organic acids Nutrition 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 238000012549 training Methods 0.000 abstract description 6
- 230000008569 process Effects 0.000 abstract description 5
- 238000012216 screening Methods 0.000 abstract description 3
- 238000003780 insertion Methods 0.000 abstract description 2
- 230000037431 insertion Effects 0.000 abstract description 2
- 230000011218 segmentation Effects 0.000 abstract description 2
- 230000000087 stabilizing effect Effects 0.000 abstract description 2
- 239000005014 poly(hydroxyalkanoate) Substances 0.000 description 71
- 229920000903 polyhydroxyalkanoate Polymers 0.000 description 71
- 230000001580 bacterial effect Effects 0.000 description 7
- 239000002028 Biomass Substances 0.000 description 6
- 238000011068 loading method Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000003834 intracellular effect Effects 0.000 description 3
- 235000015097 nutrients Nutrition 0.000 description 3
- 230000003321 amplification Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000003199 nucleic acid amplification method Methods 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 230000007480 spreading Effects 0.000 description 2
- 238000003892 spreading Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229920000704 biodegradable plastic Polymers 0.000 description 1
- 239000003225 biodiesel Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000010261 cell growth Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 238000011534 incubation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 235000013379 molasses Nutrition 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000010893 paper waste Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
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- 238000011160 research Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
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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
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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
- 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
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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
- 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
- C02F3/348—Biological treatment of water, waste water, or sewage characterised by the microorganisms used characterised by the way or the form in which the microorganisms are added or dosed
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Abstract
The invention discloses a kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity, methods described is using the PHA synthesis bacteriums of PHA synthesis bacteriums output section sbr reactor device discharge as bacterium source, carry out substrate segmentation and add the expansion culture of realizing PHA synthesis bacteriums, entering back into the phase III completes PHA synthesis and then the significantly overall PHA yield of lifting process and volume yield.Present invention introduces " carbon source storage/endogenous growth " expand training mode assume responsibility for higher technical load; the screening stage of production PHA floras can be enable to realize stably and controllable operation in relatively low substrate load range; process stabilizing operation and high yield PHA contradiction are solved, the scale application of mixed bacterium PHA synthesis can be effectively pushed.The overall PHA yield of technique can be obviously improved after " carbon source storage/endogenous growth " proposed by the present invention is expanded into the traditional three-stage technique of training mode insertion, its maximum PHA yield is about 80 times of former technique.
Description
Technical field
The invention belongs to biodegradable plastic synthesis and waste resource recovery technology field, it is related to a kind of based on Mixed Microbes
Group expands the high yield PHA technique of culture.
Background technology
Polyhydroxyalkanoate（Polyhydroxyalkanoate, PHA）It is a kind of Biopolvester, it is microorganism in born of the same parents
The material of a kind of storage energy of interior synthesis, for resisting unbalanced external environment pressure.PHA is similar in physical property
Traditional thermoplastic, therefore its alternative traditional chemical synthesis plastics, mitigate increasingly serious " white pollution " problem.
At present, biosynthesis degradation plastic（PHA）Commercialization promote based on sterile fermentation, but of a relatively high raw material cost
The scale application that expense limits PHA is isolated and purified with, disinfection cost and microorganism.And mix flora production PHA technique conducts
A kind of complete open zymotechnique, sterilizes without substrate and strict living contaminants is taken precautions against, and can utilize waste carbon
Source, the focus of technical research is just turned on the basis of waste water produces sour control technique.
Three stage of mixed bacterial PHA synthesis techniques are generally divided into the three below stage：
1）The sour section of substrate production：Complicated organic substrates are fermented into small molecular organic acid；
2）PHA synthesis bacteriums output section：Carbon source is made in sequence bioreactor with small molecular organic acid（Sequence Batch
Reactor, SBR）Middle domestication PHA synthesis bacteriums, periodically discharge the PHA synthesis strains tamed, at this moment discharge after SBR stable operations
PHA synthesis bacteriums have PHA synthesis capabilities but internal PHA contents are low, can in vivo be accumulated under high organic loading and aerobic condition
Tired PHA；
3）PHA synthesis stages：Using small molecular organic acid as substrate, the PHA synthesis bacteriums discharged using second stage is bacterium muds, aerobic condition
Under add organic acid substrate in batches, complete the PHA synthesis in PHA synthesis bacteriums.
In the above three stage, second stage is particularly critical, because only that SBR completes the domestication of PHA synthesis bacteriums, and can be steady
Surely the discharge PHA synthesis bacteriums more than, trying one's best, the phase III could synthesize more PHA using organic acid substrate.Second stage
Domestication is generally used "-starvation of being satiated with food " under aerobic condition（Feast-Famine, FF）Pattern, i.e., under the conditions of aerobic reaction
It is that mixed bacterial builds a kind of " nutritious-poor nutritional " growth conditions with reaction process.Three-stage mixing based on FF
Flora technique, it is possible to achieve the screening of PHA synthesis bacteriums, this bacterium has higher PHA contents in the phase III, has been achieved for connecing
The level of sterile fermentation PHA contents is bordering on, but in order to maintain PHA synthesis bacteriums to be tamed and dociled in second stage stable emissions, flora
The change stage（Second segment）Organic loading need control in relatively low scope, this directly results in for PHA synthesize mixing
Flora yield is too low, and then limits the lifting of technique totality PHA yield.Compared to the pure bacterium for generally putting into commercial operation
PHA synthesis techniques, possess economy of resources and environmental benefit mixed bacterial technique scale application it is sluggish not before, it is relatively low
PHA yields are one of key reasons.Therefore it is the operational mode that PHA synthesis bacteriums tame section to improve second stage, keeps SBR
Stabilization and lift PHA synthesis bacterium discharge capacitys, PHA total outputs will be obviously improved, this to mixed bacterial PHA synthesize scale should
With the important progradation of generation.
The content of the invention
There is provided one kind lifting PHA synthesis in order to change the low defect of PHA synthesis bacteriums output section strain output quantity by the present invention
The method of bacterium output section strain discharge capacity, this method is using the PHA synthesis bacteriums of PHA synthesis bacteriums output section sbr reactor device discharge as bacterium
Source, carries out substrate segmentation and adds the expansion culture of realizing PHA synthesis bacteriums, enters back into the phase III and completes PHA synthesis and then big
The overall PHA yield of amplitude lifting process and volume yield.
The purpose of the present invention is achieved through the following technical solutions：
A kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity, comprises the following steps：
First, bacterium mud is set up to spread cultivation system：The bacterium mud system that spreads cultivation is made up of N number of bacterium mud reactor that spreads cultivation, and each bacterium mud spreads cultivation
The operation of reactor is divided into the n batch repeated along the time, and each batch is divided into two sections of n-1 and n-2；
2nd, each bacterium mud in step one spread cultivation reactor start-up when, a certain amount of three-stage that is derived from is mixed into bacterium PHA techniques PHA
Bacterium mud in synthesis bacterium output section is placed in bacterium mud and spread cultivation in reactor, and using " carbon source storage/endogenous growth ", spread cultivation pattern, i.e.,：
Appropriate substrate A is added at n-1 sections, controls the mass ratio of substrate A and microorganism to be not higher than 6.4 g COD/g VSS/d, it
Backward mixed liquor aeration, monitors the dissolved oxygen levels of reaction system, it is not less than 3 mg/L；When dissolved oxygen levels reach in system
During to saturation state, stopping was aerated into the heavy stage in meditation, and the supernatant for certain volume of draining enters the n-2 sections of this batch；Xiang Yuan
Bacterium mud, which spreads cultivation, to be added and drains in reactor the substrate B of supernatant same volume, is aerated to mixed liquor and is monitored reaction system
Dissolved oxygen levels, make it be not less than 3 mg/L；After treating that ammonium ion is exhausted in system, reaction stops into heavy rank in meditation
Section, supernatant of draining enters the operation of next batch：Enter substrate A → aeration → quiet heavy → draining → and enter substrate B → aeration → quiet
Heavy → draining；So circulation and gradient increase carbon source additional amount, until the biological total amount/initial biological total amount that spreads cultivation be in 40 ~
Between 60g/g.
It is of the invention compared with existing mixed bacterium PHA, have the following advantages that：
1st, " carbon source storage/endogenous growth " proposed by the present invention expands training mode and can significantly increased realizing production PHA biomass
The PHA synthesis capabilities of flora are effectively kept while growing（Fig. 3）；
2nd, can after " carbon source storage/endogenous growth " proposed by the present invention being expanded into the traditional three-stage technique of training mode insertion
To be obviously improved the PHA yield that technique is overall, its maximum PHA yield is about 80 times of former technique（Fig. 4）；
3rd, from technique on the whole, present invention introduces " carbon source storage/endogenous growth " expand training mode assume responsibility for it is higher
Technical load, can enable the screening stage of production PHA floras realize stably and controllable operation in relatively low substrate load range, solve
Process stabilizing operation and high yield PHA contradiction, can effectively push the scale application of mixed bacterium PHA synthesis；
4th, the carbon source used in the present invention can be the high concentration organic waste carbon source of nitrogen stress or nitrogen-free, and such as molasses containing waste water is acidified
Liquid, paper waste acidifying solution and crude glycerine（Biodiesel byproduct product）, while resource reclaim is realized using discarded carbon source,
Also certain environmental benefit can be brought by cutting down biochemical oxygen demand (BOD).
Brief description of the drawings
Fig. 1 spreads cultivation the operational mode figure of reactor for bacterium mud in the present invention；
Fig. 2 is embedded in traditional three-stage PHA synthesis technique schematic diagrames to will be enlarged by training mode；
Fig. 3 expands biomass amplification situation and the tool of the evolution with distance of mixed bacterial PHA synthesis capabilities in incubation for reflection
Body example, black heavy line represents the effective swept volume of batch reactor that spreads cultivation, and solid black square represents mixed bacterial
Intracellular maximum PHA synthesizes ratio, and black empty circles represent mixed bacterial biomass；
Technique PHA is produced in the section operational mode signals of expansion culture process and actual motion of the Fig. 4 for continuous output PHA in the present invention
Amount contrast, by taking 11 days production cycles as an example, C1 represents first bacterium mud and spread cultivation batch reactor, by that analogy；
In figure, the PHA yield values of ordinate are calculated according to the actual running results to be obtained.
Embodiment
Technical scheme is further described below in conjunction with the accompanying drawings, but is not limited thereto, it is every to this
Inventive technique scheme is modified or equivalent substitution, without departing from the spirit and scope of technical solution of the present invention, all should be covered
In protection scope of the present invention.
The invention provides a kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity, comprise the following steps that：
First, bacterium mud is set up to spread cultivation system：The bacterium mud system that spreads cultivation is made up of N number of bacterium mud reactor that spreads cultivation, as shown in figure 1, often
Individual bacterium mud spread cultivation reactor operation along the time be divided into n repeat batch（Batch 1, batch 2 ..., batch n）, each batch
It is divided into two sections along the time（N-1 and n-2）, accordingly use to two kinds of substrates, substrate A：Mainly with not Nitrogen element or limit nitrogen
With small molecular organic acid（Acetic acid, propionic acid, butyric acid, valeric acid）Or the carbon source based on glycerine；Substrate B：For the strain of not carbonaceous sources
The relative scale of carbon source should meet following condition in N, P element and substrate A in nutrient solution, strain nutrition：COD（Carbon source）/ N
/ P =100 / （6~10） / （1~1.5）（Mass ratio）, while magnesium, calcium and trace element should be added to meet the life of microorganism
Long demand.
2nd, each bacterium mud in step one spread cultivation reactor start-up when, a certain amount of three-stage that is derived from is mixed into bacterium PHA techniques
Bacterium mud in PHA synthesis bacteriums output section is placed in reactor, and using " carbon source storage/endogenous growth ", spread cultivation pattern, i.e.,：First
Appropriate substrate A is added in 1-1 sections of batch, 6.4 g COD/g should be not higher than by controlling the mass ratio of substrate A and microorganism
VSS/d, backward mixed liquor aeration, monitor the dissolved oxygen levels of reaction system, it is not less than 3 mg/L, produce PHA Mixed Microbes
Group this stage mainly by extracellular carbon source be converted into PHA particles be stored in it is intracellular（Carbon source canned paragraphs）.When dissolved oxygen in system
When level reaches saturation state, stopping was aerated into the heavy stage in meditation, and the supernatant for certain volume of draining enters the 1-2 sections of this batch
In.Add and drain to opportunistic pathogen mud reactor in 1-2 sections of batch the substrate B of supernatant same volume, to mixed liquor aeration simultaneously
The dissolved oxygen levels of reaction system are monitored, it is not less than 3 mg/L, production PHA floras utilize the carbon source that intracellular is stored in the stage
The growth of cell is carried out with the nutrient of free state（Endogenous growth section）.After treating that ammonium ion is exhausted in system, instead
It should stop into the heavy stage in meditation, supernatant of draining enters in 2-1 sections of next batch, bacterium mud spreads cultivation one complete batch of reactor
Operation should include " enter substrate A → aeration → quiet heavy → draining → and enter substrate B → aeration → quiet heavy → draining " action, so circulation
（As shown in Figure 1）.When biomass rises to a certain degree in system, the sludge loading of reaction system is less than 1.6 g COD/g
During VSS/d, the additional amount of substrate A is increased in carbon source canned paragraphs, makes sludge loading close to 6.4 g COD/g VSS/d, it is interior
The nutrient concentration of source growth section compares Synchronous lifting according to the quality in step one with carbon source.To prevent inertia biomass from accumulating
It is tired, a certain amount of bacterium mud mixed liquor of being drained before the precipitation per a batch of second segment can be selected during the reaction that spreads cultivation, with daily
Discharge 1/10 ~ 1/20 mixed liquors（Account for cumulative volume ratio）It is advisable.The batch number Ying Yiman that one complete cycle of spreading cultivation includes
Sufficient biomass amplification times（Biological total amount at the end of spreading cultivation/spread cultivation initial biological total amount, g/g）It is between 40 ~ 60
Preferably.
3rd, the pattern that spreads cultivation is embedded in traditional three-stage PHA synthesis techniques, i.e., the spoil disposal of enrichment reactor is collected and used
In after the reaction that spreads cultivation, end cycle, the bacterium mud that bacterium mud spreads cultivation in system is all for carrying out subsequent third stage PHA synthesis
（Fig. 2）.PHA production cycle（In terms of day）It should be spread cultivation cycle and follow-up PHA production times comprising complete.According to second step
Described in technology pattern run multiple batch reactors that spread cultivation successively, the number of the batch that spreads cultivation reactor is equal to a complete production
The number of days in cycle, if there is decimal, rounds up（As shown in Figure 4）.By the time in the cycle that spreads cultivation, technique integrally can be with
It is the continuous output that least unit realizes PHA.
Claims (5)
1. a kind of method of lifting PHA synthesis bacteriums output section strain discharge capacity, it is characterised in that methods described step is as follows：
First, bacterium mud is set up to spread cultivation system：The bacterium mud system that spreads cultivation is made up of N number of bacterium mud reactor that spreads cultivation, and each bacterium mud spreads cultivation
The operation of reactor is divided into the n batch repeated along the time, and each batch is divided into two sections of n-1 and n-2；
2nd, each bacterium mud in step one spread cultivation reactor start-up when, three-stage will be derived from and mix bacterium PHA technique PHA synthesis bacteriums
Bacterium mud in output section is placed in bacterium mud and spread cultivation in reactor, and using " carbon source storage/endogenous growth ", spread cultivation pattern, i.e.,：At n-1 sections
Add substrate A, the mass ratio of control substrate A and microorganism is not higher than 6.4 g COD/g VSS/d, the exposure of backward mixed liquor
Gas, monitors the dissolved oxygen levels of reaction system, it is not less than 3 mg/L；When dissolved oxygen levels reach saturation state in system
When, stopping was aerated into the heavy stage in meditation, and the supernatant for certain volume of draining enters the n-2 sections of this batch；Spread cultivation instead to opportunistic pathogen mud
The substrate B for supernatant same volume of adding and drain in device is answered, the dissolved oxygen levels of reaction system are aerated and monitored to mixed liquor,
It is set to be not less than 3 mg/L；After treating that ammonium ion is exhausted in system, reaction stopped into the heavy stage in meditation, supernatant of draining
Into the operation of next batch：Enter substrate A → aeration → quiet heavy → draining → and enter substrate B → aeration → quiet heavy → draining；So
Circulate and gradient increase carbon source additional amount, until the biological total amount/initial biological total amount that spreads cultivation is between 40 ~ 60g/g.
2. the method for lifting PHA synthesis bacteriums output section strain discharge capacity according to claim 1, it is characterised in that the bottom
Thing A is the carbon source based on small molecular organic acid or glycerine with not Nitrogen element or limit nitrogen.
3. the method for lifting PHA synthesis bacteriums output section strain discharge capacity according to claim 2, it is characterised in that described small
Molecular organic acids are acetic acid, propionic acid, butyric acid, valeric acid.
4. the method for the lifting PHA synthesis bacteriums output section strain discharge capacity according to claim 1,2 or 3, it is characterised in that
The substrate B is the strain nutrition of not carbonaceous sources, and the relative scale of carbon source expires in N, P element and substrate A in strain nutrition
It is enough lower condition：COD/ N / P =100 / （6~10） / （1~1.5）（Mass ratio）.
5. the method for lifting PHA synthesis bacteriums output section strain discharge capacity according to claim 1, it is characterised in that the step
In rapid two, per a batch of second segment it is quiet it is heavy before drain a certain amount of bacterium mud mixed liquor, daily discharge rate is bacterium mud mixed liquor
Of the total volume 1/10 ~ 1/20.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108484356A (en) * | 2018-03-23 | 2018-09-04 | 世界家庭用具制品厂有限公司 | A kind of purification process of crude glycerine and application thereof obtained from kitchen garbage |
| CN112226400A (en) * | 2019-07-15 | 2021-01-15 | 上饶师范学院 | Mixed bacterium oriented breeding method and device capable of degrading benzene compounds and synthesizing PHA (polyhydroxyalkanoate) |
| CN112961766A (en) * | 2021-02-02 | 2021-06-15 | 清华大学 | Reaction system for synthesizing polyhydroxyalkanoate from organic waste and using method thereof |
| CN115261231A (en) * | 2022-08-02 | 2022-11-01 | 哈尔滨工业大学（深圳） | Method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US20100200498A1 (en) * | 2009-02-12 | 2010-08-12 | Simon Olof Harald Bengtsson | Process for Maximizing PHA Production in Glycogen Accumulating Organisms |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100200498A1 (en) * | 2009-02-12 | 2010-08-12 | Simon Olof Harald Bengtsson | Process for Maximizing PHA Production in Glycogen Accumulating Organisms |
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| CN108484356A (en) * | 2018-03-23 | 2018-09-04 | 世界家庭用具制品厂有限公司 | A kind of purification process of crude glycerine and application thereof obtained from kitchen garbage |
| CN112226400A (en) * | 2019-07-15 | 2021-01-15 | 上饶师范学院 | Mixed bacterium oriented breeding method and device capable of degrading benzene compounds and synthesizing PHA (polyhydroxyalkanoate) |
| CN112961766A (en) * | 2021-02-02 | 2021-06-15 | 清华大学 | Reaction system for synthesizing polyhydroxyalkanoate from organic waste and using method thereof |
| CN112961766B (en) * | 2021-02-02 | 2022-11-11 | 清华大学 | Reaction system for synthesizing polyhydroxyalkanoate by organic waste and using method thereof |
| CN115261231A (en) * | 2022-08-02 | 2022-11-01 | 哈尔滨工业大学（深圳） | Method for efficiently enriching PHA (polyhydroxyalkanoate) producing flora from activated sludge |
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