CN1217866C - Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater - Google Patents
Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater Download PDFInfo
- Publication number
- CN1217866C CN1217866C CN031326005A CN03132600A CN1217866C CN 1217866 C CN1217866 C CN 1217866C CN 031326005 A CN031326005 A CN 031326005A CN 03132600 A CN03132600 A CN 03132600A CN 1217866 C CN1217866 C CN 1217866C
- Authority
- CN
- China
- Prior art keywords
- ethanol
- reactor
- sulfate
- acid
- days
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The present invention relates to an ethanol type fermentation biologic desulfurization method of sulfate organic waste water, particularly a desulphurization method for realizing the purposes of acid fermentation and sulfate reduction in the same structure, which is used for treating organic waste water with anaerobic microorganisms. The method comprises the following steps: (1)a tank type reactor for continuously complete mixing and agitation is adopted, and activated carbon stuffing is added into the reactor; (2) active sludge are acclimatized; and (3)when the ethanol type fermentation organic desulfurization reaction system is started, the feeding water prepared from treacle and sodium sulfate. COD is 3200 to 3600 mg/L and SO4<2-> is 640 to 680 mg/L. The process of starting is completed in 20 days; (4) the reactor can run stably when the PH value is controlled between 6.2 and 6.9, the alkalinity is between 1400 and 1600 mg/L and HRT is between 6.2 and 10.6h. The ethanol type fermentation biologic desulfurization method of sulfate organic waste water solves the problem of the difficulty for raising the processing capability of sulphate reducing bacteria during the treatment of sulfate organic waste water.
Description
Technical field:
The present invention relates to anaerobion and handle in the sulfate-containing organic wastewater, in same structures, realize acidogenic fermentation and be the sulfur method of purpose with the sulfate reduction.
Background technology:
Contain a large amount of vitriol and carbohydrate in the trade effluent of enterprises such as sugaring, pharmacy, food-processing, this type of sulfate wastewater is carried out method and the existing many reports of technology that microbial desulfurization is handled, and typical treatment process comprises traditional anaerobic digestion, two-phase, three-phase even four technology that is in series.In these treatment process, (Sulfate Reducing Bacteria, SRB) unit of sulphate reducing is the primary link of each technology to utilize sulphate reducing bacteria.To this link, the treatment process of simple economy is to utilize to produce the reduction that acid realizes vitriol mutually.Produce sour desulphurization reactor and on function, realized the reductive action of acidogenic fermentation and vitriol.In producing sour desulphurization system, mainly there are two big floras---and acid-producing bacteria (Acidogenes, AB) and sulphate reducing bacteria.After the waste water of sulfur-bearing hydrochlorate and carbohydrate entered and produces sour desulphurization system, acid-producing bacteria at first was small molecules product, sulphate reducing bacteria utilization some tunning sulphate reducing wherein then with the carbohydrate fermentation.The different fermented type of acid-producing bacteria can produce different tunnings in producing sour desulphurization system, and sulphate reducing bacteria utilizes different fermentations product (or claim substrate) and exists on the ability than big-difference, so, fermented type how to control acid-producing bacteria provides the problem of how suitable substrate to be reached for sulphate reducing bacteria, has become the bottleneck technology that improves the sulfate reduction effect.But, still there is not the research report that produces acid-producing bacteria fermented type in the sour desulphurization system at present, particularly control the acid-producing bacteria fermented type and more do not appear in the newspapers with the research that improves the sulphate reducing bacteria processing power.
Summary of the invention:
For solving at present in handling sulfate-containing organic wastewater, be difficult to improve the problem of sulphate reducing bacteria processing power, the invention provides a kind of sulfate-containing organic wastewater ethanol-type fermentation biological desulphurization method.Method of the present invention is carried out according to the following steps: (1) adopts Continuous Flow to mix stirred-tank reactor fully, and adds active carbon filler in reactor; (2) domestication of active sludge: the active sludge of selecting to contain facultative and anaerobion is kind of a mud, will plant mud and put into container and mixes with gac, cultivates with molasses and sodium sulfate water distribution and tames, and COD concentration is 2800～3200mg/L in the above-mentioned water distribution, SO
4 2-Concentration is 1800～2200mg/L, control pH value 4.5～5.3 in cultivating the domestication process, and every stirring in 3～5 days once, changed one time water every 5～10 days, taming has hydrogen sulfide to produce after 25～33 days, and the redox potential of muddy water mixed solution bottom is-200～-250mV, domestication is finished; (3) startup of ethanol-type fermentation biological desulphurization reactive system: during reactor start-up, water inlet is formulated with molasses and sodium sulfate, and COD is 3200～3600mg/L, SO
4 2-Be 640～680mg/L, keep COD/SO
4 2-=4～6:1, the 1st～10 day flooding velocity 9～11L/ days, hydraulic detention time was 25.9～21.2 hours; Improved flow to 20～24L/ days later in the 11st day, hydraulic detention time is 11.6～9.7 hours, after reactor ran to 20 days, redox potential was stabilized in-320～-300mV, SO
4 2-Clearance reaches 80～90%, S in the water outlet
2-Concentration reaches 1.8～2.2mmol/L, and water outlet pH value is 5.5～6.0, and reactor start-up is finished; (4) operation of reactor control: control pH value 6.2～6.9 and basicity 1400～1600mg/L under reactive system is moved, and the antiacid degree impact capacity of system is stronger; Control COD/SO
4 2-Be worth=2.5～3.5: 1 o'clock, substrate ethanol utilizes fully, guarantees that simultaneously the sulfate radical clearance reaches 80～90%; It is 6.2～10.6h that sulphate reducing bacteria makes full use of acidizing product alcoholic acid hydraulic detention time; Guaranteeing that the sulfate radical clearance was not less than at 80% o'clock, the COD volumetric loading of system can reach 21.72KgCOD/m
3D, SO
4 2-Volumetric loading can reach 7.58KgSO
4 2-/ m
3D.The gac that adds in the described reactor is a particulate state, particle diameter 0.3～0.5mm.In producing sour desulphurization system, by the acclimation method of control mud and the startup and the operational conditions of reactor, to produce acid and be controlled to be ethanol-type fermentation mutually, sulphate reducing bacteria utilizes ethanol-type fermentation product hydrogen and ethanol sulphate reducing, has reached the purpose that realizes acidogenic fermentation and sulfate reduction in structures.Utilize ethanol-type fermentation to carry out biological desulphurization two aspect advantages are arranged: 1. can make the Ecological Mechanism of producing acid-producing bacteria and sulphate reducing bacteria formation interdependence in the sour desulphurization system.On the one hand, acid-producing bacteria provides substrate for sulphate reducing bacteria.The feature of acid-producing bacteria ethanol-type fermentation is that tunning is a hydrogen and based on the volatile acid of ethanol, acetate, experiment shows, produce in the sour desulphurization system sulphate reducing bacteria the substrate of easy utilization be hydrogen, easily the substrate that utilizes is ethanol and lactic acid, difficulty utilize propionic acid, butyric acid and acetate (be that substrate utilization is in proper order: hydrogen＞ethanol, lactic acid＞＞propionic acid, butyric acid＞acetate).The acid-producing bacteria ethanol-type fermentation provides very suitable substrate---hydrogen and ethanol for sulphate reducing bacteria, so the acid-producing bacteria ethanol-type fermentation is the fermented type that sulphate reducing bacteria needs; On the other hand, sulphate reducing bacteria promptly utilizes the tunning of acid-producing bacteria, has reduced tunning to the active inhibition of acid-producing bacteria, is beneficial to acid-producing bacteria and keeps stable ethanol-type fermentation.Produce acid-producing bacteria and sulphate reducing bacteria in the sour desulphurization system and form the Ecological Mechanism of this interdependence, help producing the steady running of sour desulphurization system.2. sulphate reducing bacteria is an acetate with the product ethanol conversion of acid-producing bacteria ethanol-type fermentation, is the very suitable mutually substrate of follow-up product methane.
Description of drawings:
Fig. 1 produces acid-producing bacteria in the sour desulphurization system to produce the graphic representation that hydrogen and sulphate reducing bacteria utilize the hydrogen process; Fig. 2 produces in the sour desulphurization system sulphate reducing bacteria to alcoholic acid utilization and conversion figure; Fig. 3 produces in the sour desulphurization system sulphate reducing bacteria to the utilization and the conversion figure of lactic acid; Fig. 4 produces in the sour desulphurization system sulphate reducing bacteria to the utilization and the conversion figure of acetate; Fig. 5 produces in the sour desulphurization system sulphate reducing bacteria to the utilization and the conversion figure of propionic acid; Fig. 6 produces in the sour desulphurization system sulphate reducing bacteria to butyro-utilization and conversion figure; Fig. 7 is the ability that sulphate reducing bacteria utilizes different volatile acid sulphate reducings in the sour desulphurization system of product; Among Fig. 1: the 1st, do not add the empirical curve of vitriol in the reaction process, the 2nd, reaction just adds the empirical curve of vitriol, and the 3rd, reaction does not just add and reacts the empirical curve that carries out adding behind the 16h vitriol; A among Fig. 2 to Fig. 7 is that substrate does not add vitriol; B is that substrate adds vitriol; C is the substrate background values.
Embodiment:
The process of present embodiment is:
1, the reactor assembly of ethanol-type fermentation biological desulphurization reactive system employing: reaction unit adopts Continuous Flow to mix stirred-tank reactor (CSTR) fully, cubic capacity 22.0L, useful volume 9.7L increases biomass and reduces sludge loss by adding the active carbon filler mode.The muddy water of also can strengthening of gac mixes, and increases rate of mass transfer.Gac is a particulate state, particle diameter 0.3～0.5mm, proportion 1.41g/cm
3, bulk density 0.54g/cm
3, add gac 2.2L.Gas vulcanization hydrogen adopts the NaOH solution absorption.The reactor outer felt is around 35 ± 1 ℃ of heating unit controlled temperature.
2, the domestication of active sludge in the ethanol-type fermentation biological desulphurization reactive system: the kind mud of active sludge can be the long-pending thing of municipal sewage plant's second pond bottom mud or the rivers and canals portion of sinking to the bottom in the ethanol-type fermentation biological desulphurization reactive system.Contain a large amount of polytype microorganisms in the kind mud before the domestication, comprise aerobic, facultative and anaerobion (concrete flora is referring to " water pollution control microbiology ", and Ren Nanqi etc. write, Heilungkiang science tech publishing house, December in 1993 the 1st edition).The purpose of domestication is the microorganism species that will obtain based on needed acid-producing bacteria group and sulfate reduction flora, and the microorganism of other incompatible domestication condition comprises that aerobic microbiological, part aerobic-anaerobic microbe and part anaerobion (as methanogen etc.) are progressively eliminated.Acclimation method is: will plant mud and gac in the laboratory and mix, (COD concentration is 2800～3200mg/L, SO with molasses and sodium sulfate water distribution
4 2-Concentration is 1 800～2200mg/L) cultivation domestications, control pH value 4.5～5.3, and every stirring in 3～5 days once.Change water once in 5～10 days, and only outwelled 2/3 supernatant liquor when changing water, reduce mud aerial exposure duration as far as possible.Taming obviously has hydrogen sulfide to lead to a phenomenon (stink) after 25～33 days, the redox potential of muddy water mixed solution bottom is-200～-250mV about, domestication is finished.
3. the startup of ethanol-type fermentation biological desulphurization reactive system: the sludge seeding amount VSS11.7g/L during reactor start-up, water inlet adds sodium sulfate with waste molasses manually prepares, and control water inlet COD is 3200～3600mg/L, SO
4 2-Be 640～680mg/L, keep COD/SO
4 2-Value 4～6: 1.The 1st～10 day flooding velocity 9～11L/ days, hydraulic detention time was 25.9～21.2 hours; Improved flow to 20～24L/ days later in the 11st day, hydraulic detention time is 11.6～9.7 hours, after reactor ran to 20 days, redox potential was stabilized in-310mV about, the volatile acid total amount increases to 1500mg/L, SO
4 2-Clearance reaches more than 80%, S in the water outlet
2-Concentration also reaches 2.0mmol/L, the reactor start-up success.At this moment, the COD clearance is 15～20%, water outlet pH value is 5.5～6.0.
4. produce the sign of acid-producing bacteria ethanol-type fermentation in the sour desulphurization reaction system: being the feature of acid-producing bacteria in the representation system (hereinafter to be referred as AB), is that carbon source has been carried out intermittently contrast experiment with molasses, as Fig. 1.For the experimental system that does not add vitriol,, the electron transport chain of sulphate reducing bacteria (hereinafter to be referred as SRB) is blocked, so the activity of sulphate reducing bacteria is suppressed substantially because of sulfate radical-free.But AB is unaffected, and what this moment, reaction system showed is the characteristic (Fig. 1 ' 1 ') of AB.Accordingly, add vitriol system performance be the combined action result (Fig. 1 ' 2 ') of AB and sulphate reducing bacteria.Fig. 1 ' 3 ' in, what show before the 16h is the independent exercising result of AB, and has showed the sulphate reducing bacteria result of effect separately after the 16h.
By Fig. 1 ' 1 ' as seen, AB produces hydrogen, and initial reaction stage (in the 5h) hydrogen-producing speed is very fast, later hydrogen content changes gradually slow, behind the 16h owing to can be made hydrogen content basicly stable fully by the base consumption that AB utilizes.Produce hydrogen simultaneously at AB, sulphate reducing bacteria begins to utilize hydrogen (Fig. 1 ' 2 ').The initial reaction stage sulphate reducing bacteria utilizes the speed of hydrogen less than the AB hydrogen-producing speed, makes ' 2 ' the initial stage hydrogen content of Fig. 1 be increase trend.With the carrying out of reaction, the AB hydrogen-producing speed is gradually little, sulphate reducing bacteria consumption hydrogen speed increases.When product hydrogen equated with consumption hydrogen speed, the system hydrogen content was the highest, and peak value appears in ' 2 ' curve of Fig. 1.Because sulphate reducing bacteria is to the continuous consumption of hydrogen, hydrogen content is minimizing trend until consuming fully in the system.
The liquid phase volatile acid product of table 1 acid-producing bacteria fermentative action and sulphate reducing bacteria reductive action relatively
*
| Sequence number * | Volatile acid (mg/L) | SO 4 2-Clearance (%) | S 2- mg/L | |||||
| Ethanol | Acetate | Propionic acid | Butyric acid | Valeric acid | Total amount | |||
| 1 2 3 | 601.4 282.9 413.8 | 636.6 1035.0 933.8 | 171.9 223.9 218.6 | 224.3 181.8 224.9 | 54.1 28.1 43.2 | 1689.3 1753.7 1836.3 | - 96.7 72.4 | - 13.4 9.6 |
*The substrate molasses, COD=3000mg/L, sulfate concentration 600mg/L; Do not add vitriol in ' 1 ' reaction process, ' 2 ' reaction just adds vitriol, and ' 3 ' reaction does not just add and reacts and carry out adding vitriol behind the 16h.
The liquid phase volatile acid that produces behind the AB acidogenic fermentation is formed and be the results are shown in Table 1 experiment ' 1 ', and as seen, ethanol accounts for 35.6% in the liquid phase end products of AB, acetate accounts for 37.7%, should belong to ethanol-type fermentation according to ethanol, acetate proportion.
In the ethanol-type fermentation biological desulphurization reactive system sulphate reducing bacteria to the ability of utilizing of different substrates: be substrate with different volatile acids respectively, produce in the sour desulphurization reactor sulphate reducing bacteria and utilize different volatile acid sulphate reducings experiments, Fig. 2 to Fig. 6 is seen in different volatile acid utilizations and conversion results, the reduction result of vitriol is seen Fig. 7.
Ethanol and lactic acid are that the vitriol clearance is respectively 99.9% and 97.8% in the substrate system, and acetate, propionic acid and butyric acid are that the vitriol clearance only is 7.5%, 22.2%, 12.0% in the system of substrate.
The ethanol major part that ethanol consumes during for substrate is converted into acetate, and acetate accounts for 92.5% (Fig. 2) that generates the volatile acid total amount.Lactic acid is converted into acetate and propionic acid, accounts for 53.5% and 41.3% (Fig. 6) that generates the volatile acid total amount respectively.Acetate, propionic acid and butyric acid add or do not add that contained volatile acid total amount is respectively less than the background value content of original adding separately in 2 reaction systems of vitriol, and this is the result of microorganism growth assimilation.
To utilize the obvious illustration of hydrogen be the experiment ' 3 ' of Fig. 1 to sulphate reducing bacteria in the reactor, AB product hydrogen reaches the 16th hour adding vitriol after stablizing, sulphate reducing bacteria begins to play a role, and hydrogen is utilized the reduced sulphur acid group by sulphate reducing bacteria, and hydrogen content reduces gradually until being zero.By the experiment ' 3 ' of table 1 as seen, when reaction finishes, ethanol content is 413.8mg/L in the liquid phase end products, this value be higher than sulfate reduction carry out experiment ' 2 ' (ethanol content 282.9mg/L) and be lower than experiment ' 1 ' (acid-producing only taking place, ethanol content 601.4mg/L) more completely.The still remaining experimental result explanation of ethanol during the hydrogen completely consumed, sulphate reducing bacteria utilizes the ability of hydrogen to be higher than ethanol.The ethanol content of experiment ' 3 ' is less than experiment ' 1 ', illustrates that sulphate reducing bacteria also utilizes part ethanol when utilizing hydrogen.In the table 1 experiment ' 2 ' sulfate radical clearance up to 96.7%, sulfonium ion concentration is 13.4mg/L, experiment ' 3 ' sulfate radical clearance only is 72.4%, sulfonium ion concentration is 9.6mg/L, and how much relevant this difference to the sulfate radical reduction effect is with the ethanol amount of being utilized.
To sum up, in producing sour desulphurization reactor, sulphate reducing bacteria utilizes hydrogen, ethanol and lactic acid easily, and difficulty is utilized acetate, propionic acid and butyric acid.Sulphate reducing bacteria utilizes the order of substrate to be: hydrogen＞ethanol, lactic acid＞＞propionic acid, butyric acid and acetate, this thermodynamics rule with the reduced sulphur acid group is consistent.
Be converted into acetate after the tunning ethanol of AB is utilized, but sulphate reducing bacteria is extremely low to the transformation efficiency of acetate, occurs the accumulation of acetate in the reactive system, this provides optimum substrate mutually for follow-up product methane.
6. ethanol-type fermentation biological desulphurization reactive system operational parameter control: at first use NaHCO
3Regulate pH value and basicity, investigated the influence (seeing Table 2) of pH value, basicity the reactive system operating performance.Stable when determining pH value 6.2～6.9, basicity 1400～1600mg/L, operating performance good.Under this pH value and basicity condition, further investigated COD/SO then
4 2-Value, hydraulic detention time and volumetric loading be to the influence of reactive system operating performance, and the result sees Table 3 respectively, table 4 and table 5.
Table 2 pH value, basicity are to the influence of reactive system operating performance
*
| PH value scope | Basicity scope (mg/L) | SO 4 2-Clearance mean value (%) | Water outlet S 2-Mean value (mmol/L) | ORP (mV) | Operating performance and estimation of stability |
| 4.8-5.3 5.4-5.7 6.2-6.9 | 445-620 650-800 1400-1600 | 62.5 95.3 97.4 | 1.47 4.23 4.54 | -270—-275 -305—-315 -340—-355 | Weak effect, unstable effective, the edge stabilising effect is good, and is stable |
*HRT=10.6h, COD concentration 3200-3600mg/L, SO
4 2-Concentration 640-680mg/L.
Table 3 COD/SO
4 2-Value is to the influence of reactor operating performance
* *
| COD/SO 4 2-In the value () is measured value | SO 4 2-Clearance (%) | Water outlet S 2- mmol/L | Volatile acid is formed weight percent (%) | Water outlet pH | Go out alkalinity of water mg/L | ||
| Ethanol | Acetate | Propionic acid+butyric acid+valeric acid | |||||
| 5∶1(4.5∶1) 4∶1(3.6∶1) 3∶1(2.7∶1) 2∶1(1.9∶1) 1∶1(0.9∶1) | 97.4 97.1 88.3 65.0 38.8 | 4.54 6.35 7.15 8.19 8.10 | 10.8 4.7 0.0 0.0 0.0 | 60.1 70.6 70.6 71.5 73.6 | 29.1 24.7 29.4 28.5 26.4 | 6.2-6.9 | 1497 1608 1631 1883 1939 |
* *HRT=10.6h, fixation of C OD concentration (3200-3600mg/L), COD/SO
4 2-The variation of value is by changing SO
4 2-Concentration realizes.
Basicity is regulated in water inlet.
Table 4 HRT is to the influence (mean value) of reactor operating performance
* * *
| HRT (h) | SO 4 2-Clearance (%) | Water outlet S 2-mmol/L | Water outlet pH | Volatile acid is formed weight percent (%) | ||||
| Ethanol | Acetate | Propionic acid | Butyric acid | Valeric acid | ||||
| 10.6 8.1 6.2 5.2 | 88.3 85.7 80.7 70.6 | 7.15 6.70 6.09 5.11 | 6.34 6.51 6.47 6.28 | 0.00 0.00 0.00 9.15 | 70.25 68.18 66.95 57.39 | 11.39 9.76 9.61 8.99 | 16.19 19.79 20.94 21.52 | 2.18 2.27 2.51 2.96 |
* * *COD and sulfate concentration average out to 3222.0mg/L and 1213.1mg/L, COD/SO
4 2-Value=3: 1.
Table 5 volumetric loading is to the influence (mean value) of reactor operating performance
* * * *
| Water inlet COD (mg/L) | Water inlet SO 4 2- (mg/L) | HRT (h) | COD (the KgCOD/m that loads 3·d) | SO 4 2-Load (KgSO 4 2-/m 3·d) | SO 4 2-Clearance (%) | Water outlet S 2- (mmol /L) |
| 3222.0 4815.8 7906.7 | 1213.1 1760.7 2831.2 | 6.2 7.0 8.7 | 12.09 16.44 21.72 | 4.55 6.01 7.58 | 80.7 83.6 82.2 | 6.09 8.88 13.17 |
* * * *Keep COD/SO
4 2-Value=3: 1 changes water inlet COD and SO
4 2-Concentration.
The reactive system optimal operating parameter as can be seen from table 2 to table 5:
(1) under pH value 6.2～6.9 and basicity 1400～1600mg/L, can steady in a long-term move, and the antiacid degree impact capacity of system is stronger.
(2) COD/SO
4 2-Be worth=3: 1 o'clock, substrate ethanol utilizes fully, guarantees that simultaneously the sulfate radical clearance reaches 80～90%.
(3) to make full use of the minimum hydraulic detention time of acidizing product alcoholic acid be 6.2h to sulphate reducing bacteria.
(4) the sulfate radical clearance was not less than at 80% o'clock, the COD volumetric loading of system can reach 21.72KgCOD/m
3D, SO
4 2-Volumetric loading can reach 7.58KgSO
4 2-/ m
3D.
7. ethanol-type fermentation biological desulphurization reactive system microorganism species constitutes: producing sour desulphurization reaction system is a microbial ecosystem, mainly has acid-producing bacteria and sulphate reducing bacteria two big populations.The quantity of acid-producing bacteria is 3.5 * 10 in the reactor
12About/mL, the quantity of sulphate reducing bacteria is 1.2 * 10
8About/mL.We have carried out the separation and the evaluation of dominant population to this microflora, identify 5 of acid-producing bacteria dominant generas, and 4 of sulphate reducing bacteria dominant generas the results are shown in Table 6.
Table 6 ethanol-type acidogenic fermentation desulphurization reaction system microorganism dominant microflora
* * * * *
| Type | Dominant population (generic name) |
| Acid-producing bacteria (Acidogenes, AB) | Bacteroides (Baterroides) Fusobacterium (Fusobactenum) Clostridium (Bacterroides) Aeromonas (Aeromnas) Microbacterium (Dialister) |
| Sulphate reducing bacteria (Sulfate Reducing Bacteria, SRB) | Desulfovibrio (Desulfovibrio) Desulfobacter (Desulfobacterium) Desulfotomaculum (Desulfotomaculum) Desulfococcus (Desulfococcus) |
* * * * *According to " uncle's outstanding Bacteria Identification handbook (the 8th edition), Science Press.
Claims (2)
1, sulfate-containing organic wastewater ethanol-type fermentation biological desulphurization method is characterized in that it carries out according to the following steps: (1), adopt Continuous Flow to mix stirred-tank reactor fully, and in reactor, add active carbon filler; (2), the domestication of active sludge: the active sludge of selecting to contain facultative and anaerobion is kind of a mud, will plant mud and put into container and mixes with gac, cultivates with molasses and sodium sulfate water distribution and tames, and COD concentration is 2800～3200mg/L in the above-mentioned water distribution, SO
4 2-Concentration is 1800～2200mg/L, control pH value 4.5-5.3 in cultivating the domestication process, and every stirring in 3～5 days once, changed one time water every 5～10 days, taming has hydrogen sulfide to produce after 25～33 days, and the redox potential of muddy water mixed solution bottom is-200～-250mV, domestication is finished; (3), the startup of ethanol-type fermentation biological desulphurization reactive system: during reactor start-up, water inlet is formulated with molasses and sodium sulfate, and COD is 3200～3600mg/L, SO
4 2-Be 640～680mg/L, keep COD/SO
4 2-=4～6: 1, the 1～10 day flooding velocity 9～11L/ days, hydraulic detention time was 25.9～21.2 hours; Improved flow to 20～24L/ days later in the 11st day, hydraulic detention time is 11.6～9.7 hours, after reactor ran to 20 days, redox potential was stabilized in-320～-300mV, SO
4 2-Clearance reaches 80～90%, S in the water outlet
2-Concentration reaches 1.8～2.2mmol/L, and water outlet pH value is 5.5-6.0, and reactor start-up is finished; (4), the operation of reactor control: control pH value 6.2～6.9 and basicity 1400～1600mg/L under reactive system is moved; Control COD/SO
4 2-Be worth=2.5～3.5: 1 o'clock, substrate ethanol utilizes fully, guarantees that simultaneously the sulfate radical clearance reaches 80～90%; It is 6.2～10.6h that sulphate reducing bacteria makes full use of acidizing product alcoholic acid hydraulic detention time.
2, sulfate-containing organic wastewater ethanol-type fermentation biological desulphurization method according to claim 1 is characterized in that the gac that adds in the described reactor is a particulate state, particle diameter 0.3～0.5mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN031326005A CN1217866C (en) | 2003-09-04 | 2003-09-04 | Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN031326005A CN1217866C (en) | 2003-09-04 | 2003-09-04 | Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1522973A CN1522973A (en) | 2004-08-25 |
| CN1217866C true CN1217866C (en) | 2005-09-07 |
Family
ID=34286039
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN031326005A Expired - Fee Related CN1217866C (en) | 2003-09-04 | 2003-09-04 | Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1217866C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101746897B (en) * | 2008-12-08 | 2011-09-07 | 中国石油天然气股份有限公司 | Nutrient for inhibiting sulfate reducing bacteria in oilfield water and application of nutrient |
| CN101838083A (en) * | 2010-05-17 | 2010-09-22 | 浙江大学 | Method for treating organic chemical wastewater having high COD and high concentration of sulfate ions |
| CN105366890B (en) * | 2015-11-27 | 2017-08-25 | 北京首钢朗泽新能源科技有限公司 | A kind of steel mill's tail gas biofermentation ethanol method for processing organic wastewater |
| CN105967349B (en) * | 2016-06-28 | 2019-07-12 | 北京工业大学 | A kind of high organism utilization rate sulfate reduction desulphurization technological process |
| CN115124138A (en) * | 2022-06-09 | 2022-09-30 | 中南林业科技大学 | Method for promoting fuel ethanol wastewater to produce methane |
| CN115448852A (en) * | 2022-09-22 | 2022-12-09 | 爱森（中国）絮凝剂有限公司 | Preparation method of functional monomer etherified N-hydroxymethyl acrylamide |
-
2003
- 2003-09-04 CN CN031326005A patent/CN1217866C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1522973A (en) | 2004-08-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Chen et al. | Review on microaeration-based anaerobic digestion: State of the art, challenges, and prospectives | |
| Vossoughi et al. | Performance of anaerobic baffled reactor treating synthetic wastewater influenced by decreasing COD/SO4 ratios | |
| Lens et al. | The biological sulfur cycle: novel opportunities for environmental biotechnology | |
| US5076927A (en) | Biocatalyzed partial demineralization of acidic metal sulfate solutions | |
| CN102923853A (en) | Waste water treatment method of sulfur autotrophic denitrification-anaerobic ammonia oxidation coupling desulphuration denitrification | |
| Nakamura et al. | Fundamental studies on hydrogen production in the acid-forming phase and its bacteria in anaerobic treatment processes–the effects of solids retention time | |
| Boshoff et al. | The use of micro-algal biomass as a carbon source for biological sulphate reducing systems | |
| Zhao et al. | Effects of magnesium chloride on the anaerobic digestion and the implication on forward osmosis membrane bioreactor for sludge anaerobic digestion | |
| CN106986454B (en) | Method for treating low-C/N-ratio micro-polluted eutrophic water body by synchronous nitrification and denitrification | |
| Schneider et al. | Effect of bioaugmentation on anaerobic wastewater treatment in the dairy industry | |
| Yang et al. | Nitrogen metabolism in photosynthetic bacteria wastewater treatment: a novel nitrogen transformation pathway | |
| CN103112948B (en) | Method for rapidly culturing autotrophic nitrogen removal granule sludge under conditions of low substrate concentration and high ascending velocity | |
| CN1887737A (en) | Fast culture process in anaerobic grain sludge | |
| CN101264979A (en) | Method for realizing short distance deep denitrogenation under low temperature | |
| Sabba et al. | Impact of operational strategies on a sidestream enhanced biological phosphorus removal (S2EBPR) reactor in a carbon limited wastewater plant | |
| CN109019852B (en) | Method for reducing adverse effect of nano zinc oxide on anaerobic biological treatment of sewage | |
| CN1217866C (en) | Alcohol type fermenting organism desulfurization method for treating sulfate organic wastewater | |
| CN107337283B (en) | Method for rapidly culturing pig breeding sewage activated sludge | |
| CN107235553B (en) | Low-temperature aerobic granular sludge rapid culture method based on sludge incineration ash | |
| CN105441364A (en) | Microorganisms and method for rapid start of aniline wastewater | |
| CN106517716B (en) | A method of strengthening residual active sludge anaerobic digestion performance and desulfurization phosphorus removal property | |
| CN1242934C (en) | Microorganism metabolism type regulate and control method, in sulphate waste water treatment | |
| CN100417604C (en) | Fully biological treatment of wastewater of nitrobenzol or aniline or their mixture | |
| CN107162214A (en) | A kind of complex microorganism couples the sewage water treatment method of micron Zero-valent Iron denitrogenation dephosphorizing | |
| CN105110561B (en) | A kind of method that high ammonia-nitrogen wastewater is handled under low dissolved oxygen condition |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |