CN103667376A - Method for quickly acclimatizing active sludge mixed flora to prepare polyhydroxyalkanoate (PHA) by using aerobic dynamic drainage method - Google Patents
Method for quickly acclimatizing active sludge mixed flora to prepare polyhydroxyalkanoate (PHA) by using aerobic dynamic drainage method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 60
- 239000010802 sludge Substances 0.000 title claims abstract description 58
- 239000005014 poly(hydroxyalkanoate) Substances 0.000 title abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000005273 aeration Methods 0.000 claims abstract description 33
- 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
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000001556 precipitation Methods 0.000 claims abstract description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 10
- 230000003203 everyday effect Effects 0.000 claims abstract description 9
- 239000006228 supernatant Substances 0.000 claims abstract description 9
- 230000001580 bacterial effect Effects 0.000 claims description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- 239000001301 oxygen Substances 0.000 claims description 21
- 239000000126 substance Substances 0.000 claims description 12
- 230000014759 maintenance of location Effects 0.000 claims description 10
- 150000007524 organic acids Chemical class 0.000 claims description 9
- 239000000758 substrate Substances 0.000 claims description 9
- 239000011259 mixed solution Substances 0.000 claims description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims description 8
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 7
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 7
- 239000011574 phosphorus Substances 0.000 claims description 7
- 239000002244 precipitate Substances 0.000 claims description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims description 2
- 150000004648 butanoic acid derivatives Chemical class 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 claims description 2
- 229920000903 polyhydroxyalkanoate Polymers 0.000 abstract description 59
- 230000015572 biosynthetic process Effects 0.000 abstract description 16
- 238000003786 synthesis reaction Methods 0.000 abstract description 16
- 238000002474 experimental method Methods 0.000 abstract description 3
- 229920000704 biodegradable plastic Polymers 0.000 abstract description 2
- 239000013589 supplement Substances 0.000 abstract description 2
- 235000015097 nutrients Nutrition 0.000 abstract 2
- 239000007788 liquid Substances 0.000 abstract 1
- 238000012163 sequencing technique Methods 0.000 abstract 1
- 230000002194 synthesizing effect Effects 0.000 abstract 1
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 description 54
- 238000012017 passive hemagglutination assay Methods 0.000 description 54
- 239000000243 solution Substances 0.000 description 29
- 239000011573 trace mineral Substances 0.000 description 6
- 235000013619 trace mineral Nutrition 0.000 description 6
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 241000894006 Bacteria Species 0.000 description 4
- 238000012216 screening Methods 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 238000011081 inoculation Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 238000012279 drainage procedure Methods 0.000 description 2
- 230000003834 intracellular effect Effects 0.000 description 2
- 230000000050 nutritive effect Effects 0.000 description 2
- 230000002572 peristaltic effect Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 235000001674 Agaricus brunnescens Nutrition 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
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- 230000000813 microbial effect Effects 0.000 description 1
- 230000007269 microbial metabolism Effects 0.000 description 1
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
- 235000019796 monopotassium phosphate Nutrition 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 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 description 1
- 238000011160 research Methods 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
Landscapes
- Activated Sludge Processes (AREA)
Abstract
The invention discloses a method for quickly acclimatizing active sludge mixed flora to prepare polyhydroxyalkanoate (PHA) by using an aerobic dynamic drainage method and relates to a method for preparing the PHA. The invention solves the problems that the acclimatization time for synthesizing PHA through active sludge mixed flora is long, a reactor works unstably and the synthesized PHA is low in content in the prior art. The method comprises the following steps: 1, active sludge is put into a sequencing batch reactor (SBR); 2, 6-12 hours are taken as a cycle of operation, in the cycle of operation, two-time water introduction, precipitation and drainage are carried out, the drainage rate is 1:1, during the first water introduction, a carbon source and various nutrients are introduced, and during the second water introduction, only the supplement of nitrogen nutrient is carried out; 3, 2-4 cycles are operated every day, the sludge detention time is 1-10 days and sludge-water mixed liquid is collected; 4, batch experiments are carried out, half supernatant is discharged, equivalent carbon source is supplemented, aeration, precipitation and drainage are carried out, and the process is repeated for 6 to 8 times. The invention belongs to the field of biodegradable plastic synthesis.
Description
Technical field
The invention belongs to the synthetic field of the municipal sludge utilization of resources and biodegradable plastic, be specifically related to adopt the domestication of SBR aerobic process to there is the active sludge mixed bacterial of PHA (PHAs) synthesis capability.
Background technology
Poly hydroxyalkanoate (Polyhydroxyalkanoates, be called for short PHAs or PHA) be that a class is synthetic under unbalanced nutritional condition by multiple prokaryotic micro-organisms, and be stored in intracellular lipid aggregate thing, in microbial metabolism, play accumulation carbon source, the effect of the inside and outside ion of statocyte.Its chemistry, physical properties are similar to chemosynthesis plastics, and PHA can decompose utilization by microorganism completely at occurring in nature, are a kind of very promising and novel environment friendly materials that exploitation is worth, are expected to solve current ubiquitous white pollution problems.
The production of PHA at present mainly be take sterile culture fermentation as main, and often take high purity carbohydrate as matrix, and culture condition is harsh, causes PHA production cost high.Activated sludge process is the core process in the biological treatment of municipal sewage plant, and active sludge is the system that has comprised bacterium, fungi, protozoon, metazoal complicated microorganism.There are some researches show in the technique of active sludge sewage disposal to possess the mushroom ubiquity of PHA synthesis capability, illustrated that utilizing mixed bacterial to carry out PHA synthesizes feasible.Utilize the synthetic PHA of active sludge mixed bacterial effectively to reduce costs, but also exist long, reactor fluctuation of service of domestication time simultaneously and the limitation such as synthetic PHA content is low, become the bottleneck that its industrialization is produced.In the present invention, adopt the method for rapid precipitation dynamic drainage, principle is the flora based on having PHA synthesis capability, in the full stage of substrate, can absorb fast substrate and be stored in cell with PHA form, therefore must be better than not possessing PHA synthesis capability or the weak PHA enrichment bacterium of synthesis capability at the settling property that fills this type of flora in latter stage.
Summary of the invention
The production method cost that the object of the invention is to solve existing PHA is high, and adopt the synthetic PHA of active sludge mixed bacterial to exist domestication time length, reactor fluctuation of service and the synthetic low circumscribed problem of PHA content, and provide aerobic dynamic drainage method for quick acclimated activated sludge mixed bacterial, to prepare the method for PHA, its cost that not only can save time, and improved the content of PHA in mixed bacterial.
Aerobic dynamic drainage method of the present invention is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, concrete steps are as follows:
One, get in the sbr reactor device that active sludge is 10:1 in aspect ratio, make sludge concentration in reactor reach 3000～5000mg/L;
Two, take 6～12h as a cycle of operation, operation sbr reactor device, the operational process of described sbr reactor device one-period is as follows: intake first for the first time, after having intake for the first time, in the temperature of sbr reactor device, be under 20 ℃～25 ℃ conditions, start aeration, in sbr reactor device, dissolved oxygen is from 2～3mg/L increases in a leap 6～7mg/L, stop aeration, then precipitate after 3～5min draining; Intake for the second time again, continue aeration 5～11h, after precipitation 30min, draining; Wherein, the water entering for the first time contains carbon source, nitrogenous source and phosphorus source, and its chemical oxygen demand (COD) is 1000～5000mg/L, and the concentration of substrate carbon, nitrogen and phosphoric meets C:N:P=(110～90): (7～5): 1; Secondary water inlet only contains nitrogenous source not carbonaceous sources and phosphorus source; Wherein, described carbon source is small molecular organic acid, and the draining ratio of described draining is 1:1;
Three, by the cycle of operation operation of step 2, with 2～4 cycles of operation of every day, operation sbr reactor device, sludge retention time is 1～10 day, collects the muddy water mixed solution of discharging every day;
Four, the muddy water mixed solution of collection is placed in batch reactor standing after, remove the supernatant liquor of batch half volume of reactor, collecting precipitation thing, add and remove the isopyknic carbon source of supernatant liquor, then carry out aeration, in reactor, dissolved oxygen content increases in a leap to 6～7mg/L from 2～3mg/L, stops aeration;
Five, the operation 6～8 times of repeating step four, completes the method that quick domestication mixed active mud is prepared PHA.
Described active sludge is municipal sludge;
Described small molecular organic acid is acetic acid, propionic acid or butyric acid;
Carbon source described in step 4 is small molecular organic acid.
The present invention compares with the technique of the synthetic PHA of existing mixed bacterial, has the following advantages:
The present invention is after inoculation of activated-sludge, and the active domestication of active sludge is synchronizeed and carried out with the screening enrichment of PHA bacterium, does not need to consider separately mud decubation, thereby has shortened the cycle of synthetic PHA; The present invention is once intake precipitation and draining to realize the quick domestication in PHA enrichment stage by monitoring dissolved oxygen and increase at normal temperatures, thereby active sludge is forced to screening, and the cycle is many, resultant velocity is fast, contributes to realize the resource utilization of mud.
The present invention is in the process of the synthetic PHA technique of activated sludge acclimatization, propose to adopt aerobic dynamic drainage method, in the i.e. cycle of operation, utilize the self-characteristic of microorganism intracellular organic matter storage PHA to carry out twice water inlet, the operational mode of precipitation and draining, solved the long difficult problem of the synthetic PHA acclimation period of mixed bacterial, having realized the two of time cost and input/output ratio improves, move after 15 days PHA synthesis capability higher than 50%, move PHA synthesis capability after 30 days and surpass 70%, the synthesis capability that can reach higher than conventional P HA synthesis technique far away also significantly shortens the domestication time, retain the lower strong target flora of PHA synthesis capability, the synthetic commercial application of further promotion PHA is played an important role.
Accompanying drawing explanation
Fig. 1 is that in sbr reactor device operation one-period of the present invention, the different time of water inlet, aeration, precipitation and draining arranges schematic diagram; Wherein, 1. for carrying out, be 2. aeration, be 3. precipitation, be 4. draining;
Fig. 2 is the operating performance figure of PHA resultant quantity in the present invention; Wherein,
pHA resultant quantity histogram for SBR;
for PHA resultant quantity histogram in batch experiment.
Embodiment
Embodiment one: the aerobic dynamic drainage method of present embodiment is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, concrete steps are as follows:
One, get in the sbr reactor device that active sludge is 10:1 in aspect ratio, make sludge concentration in reactor reach 3000～5000mg/L;
Two, take 6～12h as a cycle of operation, operation sbr reactor device, the operational process of described sbr reactor device one-period is as follows: intake first for the first time, after having intake for the first time, in the temperature of sbr reactor device, be under 20 ℃～25 ℃ conditions, start aeration, in sbr reactor device, dissolved oxygen is from 2～3mg/L increases in a leap 6～7mg/L, stop aeration, then precipitate after 3～5min draining; Intake for the second time again, continue aeration 5～11h, after precipitation 30min, draining; Wherein, the water entering for the first time contains carbon source, nitrogenous source and phosphorus source, and its chemical oxygen demand (COD) is 1000～5000mg/L, and the concentration of substrate carbon, nitrogen and phosphoric meets C:N:P=(110～90): (7～5): 1; Secondary water inlet only contains nitrogenous source not carbonaceous sources and phosphorus source; Wherein, described carbon source is small molecular organic acid, and the draining ratio of described draining is 1:1;
Three, by the cycle of operation operation of step 2, with 2～4 cycles of operation of every day, operation sbr reactor device, sludge retention time is 1～10 day, collects the muddy water mixed solution of discharging every day;
Four, the muddy water mixed solution of collection is placed in batch reactor standing after, remove the supernatant liquor of batch half volume of reactor, collecting precipitation thing, add and remove the isopyknic carbon source of supernatant liquor, then carry out aeration, in reactor, dissolved oxygen content increases in a leap to 6～7mg/L from 2～3mg/L, stops aeration;
Five, the operation 6～8 times of repeating step four, completes the method that quick domestication mixed active mud is prepared PHA.
Water inlet for the first time described in present embodiment step 2, except containing carbon source, nitrogenous source and phosphorus source, also has MgSO
4solution, CaCl
2solution, EDTA solution and trace element;
In the water that every 1L enters for the first time, contain the MgSO that concentration is 40mg/L
4the CaCl that solution, concentration are 30mgL
2solution and concentration are the EDTA solution of 20mg/L;
The trace element that contains 1mL in the water that every 1L enters for the first time, the H that described trace element is is 0.3mg/L by concentration
3bO
3the CoCl that solution, concentration are 0.3mg/L
2the CuSO that solution, concentration are 0.06mg/L
4the FeCl that solution, concentration are 3mg/L
36H
2the ZnSO that O solution, concentration are 0.24mg/L
47H
2the MnCl that O is molten, concentration is 0.24mg/L
2h
2o solution and concentration are the Na of 0.12mg/L
2moO
42H
2o solution preparation forms.
Chemical oxygen demand (COD) described in present embodiment step 2 is the chemical oxygen demand (COD) that 1000～5000mg/L refers to carbon source.
Sbr reactor device described in present embodiment also needs to meet the following conditions: in sbr reactor device bottom, aerating apparatus is installed and mud discharging mouth is set, the upstream producing by bottom aeration is realized muddy water and is mixed, water port is established at middle part, and water-in is established at top, adopts the water inlet of peristaltic pump continuously pumping.Must use magnetic valve water-freeing arrangement, guarantee in drainage procedure, the selection of active sludge to be pressed, the ratio of each draining/water inlet is 50%.
Present embodiment is after inoculation of activated-sludge, and the active domestication of active sludge is synchronizeed and carried out with the screening enrichment of PHA bacterium, does not need to consider separately mud decubation, thereby has shortened the cycle of synthetic PHA; Present embodiment is once intake precipitation and draining to realize the quick domestication in PHA enrichment stage by monitoring dissolved oxygen and increase at normal temperatures, thereby active sludge is forced to screening, and the cycle is many, resultant velocity is fast, contributes to realize the resource utilization of mud.
Present embodiment is in the process of the synthetic PHA technique of activated sludge acclimatization, propose to adopt aerobic dynamic drainage method (ADD), in the cycle of operation, according to the synthesising law of PHA in microbe, carry out twice water inlet, the operational mode of precipitation and draining, solved the long difficult problem of the synthetic PHA acclimation period of mixed bacterial, having realized the two of time cost and input/output ratio improves, move after 15 days PHA synthesis capability higher than 50%, move PHA synthesis capability after 30 days and surpass 70%, the synthesis capability that can reach higher than conventional P HA synthesis technique far away also significantly shortens the domestication time, retain the lower strong target flora of PHA synthesis capability, the synthetic commercial application of further promotion PHA is played an important role.
Embodiment two: present embodiment and embodiment one difference are: the temperature at reactor described in step 2 is under 23 ℃ of conditions, starts aeration.Other is identical with embodiment one.
Embodiment three: present embodiment and embodiment one or two differences are: described carbon source is small molecular organic acid.Other is identical with embodiment one or two.
Embodiment four: one of present embodiment and embodiment one to three difference is: the small molecular organic acid described in step 2 is acetate, propionic salt or butyrates.Other is identical with one of embodiment one to three.
Embodiment five: one of present embodiment and embodiment one to four difference is: take 8～10h as a cycle of operation described in step 2.Other is identical with one of embodiment one to four.
Embodiment six: one of present embodiment and embodiment one to five difference is: take 9h as a cycle of operation described in step 2.Other is identical with one of embodiment one to five.
Embodiment seven: one of present embodiment and embodiment one to six difference is: the chemical oxygen demand (COD) described in step 2 is 1000～4000mg/L.Other is identical with one of embodiment one to six.
Embodiment eight: one of present embodiment and embodiment one to seven difference is: the chemical oxygen demand (COD) described in step 2 is 1000～3000mg/L.Other is identical with one of embodiment one to seven.
Embodiment nine: one of present embodiment and embodiment one to eight difference is: the chemical oxygen demand (COD) described in step 2 is 2000mg/L.Other is identical with one of embodiment one to eight.
Embodiment ten: one of present embodiment and embodiment one to nine difference is: the carrying out described in step 2 intake for the second time, continues aeration 6～10h.Other is identical with one of embodiment one to nine.
Embodiment 11: one of present embodiment and embodiment one to ten difference is: the carrying out described in step 2 intake for the second time, continues aeration 7～9h.Other is identical with one of embodiment one to ten.
Embodiment 12: one of present embodiment and embodiment one to 11 difference is: the carrying out described in step 2 intake for the second time, continues aeration 8h.Other is identical with one of embodiment one to 11.
Embodiment 13: one of present embodiment and embodiment one to 12 difference is: the concentration of substrate carbon, nitrogen and the phosphoric described in step 2 meets C:N:P=100:6:1.Other is identical with one of embodiment one to 12.
Embodiment 14: one of present embodiment and embodiment one to 13 difference is: the sludge retention time described in step 3 is 1～8 day.Other is identical with one of embodiment one to 13.
Embodiment 15: one of present embodiment and embodiment one to 14 difference is: the sludge retention time described in step 3 is 1～6 day.Other is identical with one of embodiment one to 14.
Embodiment 16: one of present embodiment and embodiment one to 15 difference is: the sludge retention time described in step 3 is 1～4 day.Other is identical with one of embodiment one to 15.
Embodiment 17: one of present embodiment and embodiment one to 16 difference is: the sludge retention time described in step 3 is 1～3 day.Other is identical with one of embodiment one to 16.
Embodiment 18: one of present embodiment and embodiment one to 17 difference is: the sludge retention time described in step 3 is 2 days.Other is identical with one of embodiment one to 17.
Content of the present invention is not limited only to the content of the respective embodiments described above, and the combination of one of them or several embodiments equally also can realize the object of invention.
By following examples, verify beneficial effect of the present invention:
The aerobic dynamic drainage method of the present embodiment is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, concrete steps are as follows:
One, the second pond mud of getting Wenchang sewage work, in aspect ratio is 10:1, the effective volume sbr reactor device that is 4L, makes sludge concentration in reactor reach 3000～5000mg/L; Described sbr reactor device also needs to meet the following conditions: in sbr reactor device bottom, aerating apparatus is installed and mud discharging mouth is set, the upstream producing by bottom aeration is realized muddy water and is mixed, water port is established at middle part, and water-in is established at top, adopts the water inlet of peristaltic pump continuously pumping.Must use magnetic valve water-freeing arrangement, guarantee in drainage procedure, the selection of active sludge to be pressed, the ratio of each draining/water inlet is 50%;
Two, take 6～12h as a cycle of operation, operation sbr reactor device, described sbr reactor device operational process is as follows: enter for the first time sodium acetate solution, ammonium chloride solution, potassium dihydrogen phosphate, MgSO
4solution, CaCl
2after solution, EDTA solution and trace element complete, temperature at reactor is under 20 ℃～25 ℃ conditions, start aeration, reactor enters the full stage of substrate, dissolved oxygen (DO) content in Real-Time Monitoring reactor, and dissolved oxygen in sbr reactor device (DO) content increases suddenly, from starting 2～3mg/L of aeration, reach 6～7mg/L, stop aeration, carry out after rapid precipitation 4min draining immediately; Then intake for the second time, continue aeration 5～11h, draining after precipitation 30min; Wherein, the chemical oxygen demand (COD) of water inlet is 1000～2000mg/L for the first time, and the concentration of substrate carbon, nitrogen and phosphoric meets C:N:P=100:6:1; Water inlet for the second time supplements and only to contain nitrogen element the tap water of carbonaceous sources is not required to maintain microorganism growth, guarantees can not suppress microbial growth because discharging for the first time nitrogen; Wherein, described draining ratio is 1:1;
Three, with 2～4 cycles of operation of every day, operation sbr reactor device, sludge retention time (SRT) is 10 days, collects the muddy water mixed solution of discharging every day;
Four, the muddy water mixed solution of collection is inserted standing in 500mL beaker after, after precipitation, discharge supernatant liquor 250mL, add 250mL carbon source (carbon source is small molecular organic acid, not containing N, P nutritive substance), start aeration and consumed the nutritive substance in reactor, wait to exhaust, remove supernatant liquor, add carbon source, then carry out aeration, in batch reactor, dissolved oxygen content increases in a leap suddenly and reaches 6～7mg/L from 3mg/L left and right, stops aeration;
Five, the operation 6～8 times of repeating step four, completes the method that quick domestication mixed active mud is prepared PHA.
MgSO in water inlet for the first time described in the present embodiment step 2
4solution, CaCl
2solution, EDTA solution and micro-add-on and proportioning are as follows:
In the water that every 1L enters for the first time, contain the MgSO that concentration is 40mg/L
4the CaCl that solution, concentration are 30mgL
2solution and concentration are the EDTA solution of 20mg/L;
The trace element that contains 1mL/L in the water that every 1L enters for the first time, the H that described trace element is is 0.3mg/L by concentration
3bO
3the CoCl that solution, concentration are 0.3mg/L
2the CuSO that solution, concentration are 0.06mg/L
4the FeCl that solution, concentration are 3mg/L
36H
2the ZnSO that O solution, concentration are 0.24mg/L
47H
2the MnCl that O is molten, concentration is 0.24mg/L
2h
2o solution and concentration are the Na of 0.12mg/L
2moO
42H
2o solution preparation forms;
As shown in Figure 2, wherein the unit of PHA content is the per-cent (wt%) that PHA dry weight accounts for dry cell weight to the operating performance figure of the PHA resultant quantity of the present embodiment.By the technique in the present embodiment, in batch experiment, can make more than PHA output starts to be significantly increased to 50wt% in latter 15 days of inoculation, move PHA output after 20 days and surpass 60%, and within latter 30 days, reach stable in moving, more than PHA content reaches 70wt%.
Claims (10)
1. aerobic dynamic drainage method is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that its concrete steps are as follows:
One, get in the sbr reactor device that active sludge is 10:1 in aspect ratio, make sludge concentration in reactor reach 3000～5000mg/L;
Two, take 6～12h as a cycle of operation, operation sbr reactor device, the operational process of described sbr reactor device one-period is as follows: intake first for the first time, after having intake for the first time, in the temperature of sbr reactor device, be under 20 ℃～25 ℃ conditions, start aeration, in sbr reactor device, dissolved oxygen is from 2～3mg/L increases in a leap 6～7mg/L, stop aeration, then precipitate 3～5min, draining; Intake for the second time again, continue aeration 5～11h, after precipitation 30min, draining; Wherein, the water entering for the first time contains carbon source, nitrogenous source and phosphorus source, and its chemical oxygen demand (COD) is 1000～5000mg/L, and the concentration of substrate carbon, nitrogen and phosphoric meets C:N:P=(110～90): (7～5): 1; Secondary water inlet only contains nitrogenous source not carbonaceous sources and phosphorus source; Wherein, described carbon source is small molecular organic acid, and the draining ratio of described draining is 1:1;
Three, by the cycle of operation operation of step 2, with 2～4 cycles of operation of every day, operation sbr reactor device, sludge retention time is 1～10 day, collects the muddy water mixed solution of discharging every day;
Four, the muddy water mixed solution of collection is placed in batch reactor standing after, remove the supernatant liquor of batch half volume of reactor, collecting precipitation thing, add and remove the isopyknic carbon source of supernatant liquor, then carry out aeration, in reactor, dissolved oxygen content increases in a leap to 6～7mg/L from 2～3mg/L, stops aeration;
Five, the operation 6～8 times of repeating step four, completes the method that quick domestication mixed active mud is prepared PHA.
2. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the active sludge described in step 1 is municipal sludge.
3. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the temperature at sbr reactor device described in step 2 is under 23 ℃ of conditions, starts aeration.
4. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the small molecular organic acid described in step 2 is acetate, propionic salt or butyrates.
5. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that take 8～10h as a cycle of operation described in step 2.
6. aerobic dynamic drainage method according to claim 5 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that take 9h as a cycle of operation described in step 2.
7. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the chemical oxygen demand (COD) described in step 2 is 2000～4000mg/L.
8. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the carrying out described in step 2 intake for the second time, continues aeration 7～9h.
9. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the concentration of substrate carbon, nitrogen and the phosphoric described in step 2 meets C:N:P=100:6:1.
10. aerobic dynamic drainage method according to claim 1 is prepared the method for PHA for quick acclimated activated sludge mixed bacterial, it is characterized in that the sludge retention time described in step 3 is 3～7 days.
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| CN103834697A (en) * | 2014-03-18 | 2014-06-04 | 哈尔滨工业大学 | Method of synthesizing biodegradable plastic by adopting aerobic granular sludge |
| CN104031906A (en) * | 2014-06-27 | 2014-09-10 | 天津大学 | Screening and domestication method of bacteria colony for producing polyhydroxyalkanoate by using xylose |
| CN104098177A (en) * | 2014-07-09 | 2014-10-15 | 中山大学 | Wastewater treatment method capable of realizing sulfur synergy denitrification simultaneous nitrogen and phosphorous removal |
| CN104031906B (en) * | 2014-06-27 | 2016-11-30 | 天津大学 | A kind of screening utilizing xylose to produce PHA flora and acclimation method |
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