CN106477842B - A method of excess sludge is handled using horizontal type anaerobic reactor - Google Patents
A method of excess sludge is handled using horizontal type anaerobic reactor Download PDFInfo
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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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- 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
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
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Abstract
The invention discloses a kind of methods using horizontal type anaerobic reactor processing excess sludge, belong to the technical field of organic solid waste processing disposition and residual sludge reduction.The present invention uses anaerobism horizontal reactor, pass through the insulation effect of solar sunlight house, the excess sludge for reaching 20% to solid content carries out anaerobic digestion, reliable guidance is provided for the processing disposition of actual sewage treatment plant excess sludge, treated that excess sludge improves dewatering for this equipment, and it is effectively reduced pathogenic microorganism, while reducing the stink of sludge.
Description
Technical field
The present invention relates to a kind of methods using horizontal type anaerobic reactor processing excess sludge, belong at organic solid waste
The technical field of reason disposition and residual sludge reduction.
Background technique
Excess sludge refers to be generated in primary sedimentation tank and second level, tertiary treatment process when sewage treatment plant handles waste water
Precipitating sludge object, particulate matter and floating material etc..With the fast development of Chinese society expanding economy and urbanization, town sewage
The quantity and scale of factory are being continuously increased.China's " the light mud of heavy water " problem present in specific resistance to filtration is extremely serious, right
Not enough, 80% sludge obtains stable processing disposition not yet for the attention of specific resistance to filtration and investment.Preresearch estimates " 12
During five ", national annual produces ten thousand tons of wet mud 3500-6000 of 80% moisture content, converts into ten thousand tons of dewatered sludge about 700-1200.
60,000,000 tons will be broken through to the year two thousand twenty sludge yield, being continuously increased for sludge yield brings huge pressure to environmental protection industry (epi).
Anaerobic digestion techniques are one of effective means of specific resistance to filtration, and anaerobic digestion can reduce sludge volume, surely
Determine sludge quality, improve the dehydrating effect of sludge, reduces sludge stench, improve the hygienic quality of sludge.Traditional sludge wet type disappears
Moisture percentage in sewage sludge is up to 95% in change, generates a large amount of reluctant biogas slurries, simultaneously because reaction system contain a large amount of water to
Temperature-increasing system brings very big difficulty, when processing big but effective digestion power that takes up space it is low.The high solid-state digestion of sludge overcomes
The deficiency of traditional anaerobism disposition, improves the treating capacity of unit organic matter, improves digestive efficiency, while greatly reducing biogas slurry
Yield.But there is also certain deficiencies for traditional vertical slaking apparatus, and since the viscosity and density of sludge are larger, anaerobism
Sludge is easy to be deposited in bottom when processing, causes local acidification, and mass-and heat-transfer is obstructed, and fermentation rate is slower etc..
Summary of the invention
To solve the above-mentioned problems, it the present invention provides a kind of excess sludge processing unit and provides a kind of using horizontal
The method that anaerobic reactor handles excess sludge efficiently avoids existing processing the insufficient of sludge of vertical reactor and asks
Topic.The present invention utilizes the horizontal reactor with pulling flow type agitating device, the excess sludge of anaerobic digestion solid content 20%.
The first purpose of the invention is to provide a kind of excess sludge processing unit, the excess sludge processing unit is main
It is dehydrated and fills including feeding device, horizontal type anaerobic reaction unit, collecting methane and purification device, warming solar energy device and biogas residue
It sets；The warming solar energy device is arranged in horizontal type anaerobic reaction unit outer layer；Feeding device and horizontal type anaerobic reaction unit
Feed inlet connection, biogas collection device are connected with horizontal type anaerobic reaction unit.
In one embodiment, the feeding device is screw conveyor.
In one embodiment, the generally Horizontal cylinder body of horizontal type anaerobic reaction unit, lateral diameters are long with tank body
Degree ratio is 1:5.
In one embodiment, the dischargeable capacity of horizontal type anaerobic reaction unit is 40m3。
In one embodiment, the volume of the horizontal reacting device is 50m3。
In one embodiment, pulling flow type agitating device is had in the horizontal type anaerobic reaction unit.
In one embodiment, the warming solar energy device is the sunlight board with ultraviolet-absorbing film, utilizes temperature
Reactor temperature can be improved 8 DEG C -10 DEG C by the insulation effect of room.
In one embodiment, the mud extraction of the horizontal type anaerobic reaction unit uses pneumatic diaphragm pump mud extraction；Biogas is received
Collection uses biogas film made of HDPE material, and draught fan matching and torch, it is ensured that the stable operation of device.
It is to utilize excess sludge of the invention a second object of the present invention is to provide a kind of method for handling excess sludge
Processing unit.
The method is that the excess sludge of solid content 20% is carried out Anaerobic Digestion using horizontal reactor.
In one embodiment, the pH of the excess sludge be 7.2~8.0, TS 18~22%, VS/TS 55~
60%, 20~26mg/kg of ammonia nitrogen, 135~160g/kg of total carbon, 25~30g/kg of total nitrogen, carbon-nitrogen ratio 5.0~5.5.
In one embodiment, the pH of the excess sludge is 7.6, TS 20%, VS/TS 55~60%, ammonia nitrogen
23.15mg/kg, total carbon 148.63g/kg, total nitrogen 27.84g/kg, carbon-nitrogen ratio 5.3.
In one embodiment, added by the way of continuous feed when the horizontal type anaerobic reaction unit starts
Material completes charging in the 1st day into 10 tons of excess sludge, 1 ton, 1 month of charging daily later, feeds 40 tons altogether, volume is 35 vertical
Side, methane phase strain is not added；It is periodically stirred daily after completing charging, speed of agitator 5r/min, start-up course is detested
Oxygen digestion time is 73d.
Beneficial effects of the present invention:
(1) horizontal reactor is generally used for food fermentation industry, the present invention to the length-width ratio of traditional horizontal reactor and
Heat preserving mode is improved.The length-width ratio of horizontal reactor is increased to 5:1 by the present invention, and it is longer that this structure has sludge
Digestion obtains better digestion effect along journey.The present invention also takes newly lagging facility other than using horizontal reactor
Design play the good result of energy saving temperature controlling by building heating protection device of the solar energy greenhouse glass sunlight house as reactor,
For glass sunlight house using channel steel and angle steel as skeleton, surrounding plays good temperature raising and maintaining effect with the sealing of PC undaform sunlight board.
(2) present invention is directed to the excess sludge of solid content 20%, carries out Anaerobic Digestion using horizontal reactor.It takes
The mode of continuous feed carries out the operation of reactor by warming solar energy system, and by operation in 3 months, sludge produced biogas
Rate reaches 274mL/gVS, methane content 58%, and VS conversion ratio reaches 46%, and protein and polysaccharide degradation rate are respectively
36.7% and 30.1%, VFA content maximum value is 2395mg/kg in digestion process, and maximum value appears in the 42nd day.Digestion process
Middle ammonia nitrogen concentration is slowly increased always, maximum value about 124.3mg/kg.
Detailed description of the invention
Fig. 1 is reactor assembly schematic diagram；
Fig. 2 is in a few days difference variation；
Fig. 3 is the variation of temperature in digestion process；
Fig. 4 is the variation of gas production and methane content；
Fig. 5 is the situation of change of VFA in anaerobic digestion；
Fig. 6 is the situation of change of ammonia nitrogen in anaerobic digestion process；
Fig. 7 is the variation of VS conversion ratio in anaerobic digestion；
Fig. 8 is the variation of protein in digestion process；
Fig. 9 is the variation of polyoses content；
Reactor is evenly distributed 4 sample taps, respectively No. 1 by along journey in above-mentioned figure, and No. 2, No. 3 and No. 4 sample taps divide
It Yong not R1, R2, R3 and R4 expression.
Specific embodiment:
Implementation column 1
Excess sludge is the mud extraction of sewage treatment plant's belt filter press, and sludge quality is shown in Table 1.
1 excess sludge property of table
The excess sludge processing unit that the present invention uses mainly includes feeding device, horizontal type anaerobic reaction unit, biogas receipts
Collection and purification device, warming solar energy device and biogas residue dehydration device；The warming solar energy device setting is anti-in horizontal type anaerobic
Answer device outer layer；Feeding device is connect with the feed inlet of horizontal type anaerobic reaction unit, and biogas collection device is reacted with horizontal type anaerobic
Device is connected.Horizontal type anaerobic reaction unit (i.e. reactor) designs be mounted with corollary equipment outside, for ultraviolet-absorbing film
Reactor temperature can be improved 8 DEG C -10 DEG C using the insulation effect in greenhouse by sunlight board.Device charging is filled using helical feed
Charging is set, tank body mud extraction uses pneumatic diaphragm pump mud extraction.Collecting methane uses biogas film made of HDPE material, and draught fan matching
And torch, it is ensured that the stable operation of device.Reactor dischargeable capacity is 40m3, reactor generally Horizontal cylinder body, side be straight
Diameter and length of tank ratio are 1:5.
The present invention is directed to the excess sludge of solid content 20%, carries out Anaerobic Digestion (Fig. 1) using horizontal reactor.It adopts
The mode for taking continuous feed carries out the operation of reactor by warming solar energy system, and by operation in 3 months, sludge produced natural pond
Gas rate reaches 274mL/gVS, methane content 58%, and VS conversion ratio reaches 46%, and protein and polysaccharide degradation rate are respectively
36.7% and 30.1%, VFA content maximum value is 2395mg/kg in digestion process, and maximum value appears in the 42nd day.Digestion process
Middle ammonia nitrogen concentration is slowly increased always, maximum value about 124.3mg/kg.VS of the reactor along 4 sample tap sludge of journey, protein
Apparent otherness is presented with polysaccharide degradation rate, in reactor the degradation rate of sludge with its locating for be positively correlated along journey distance.
By building solar energy greenhouse device, playing the role of raising and stablizing reactor temperature, reactor temperature is warm than outdoor
Degree can improve 10 DEG C or so, can be by the undulated control of reactor temperature at 4 DEG C -5 DEG C.Running gear of the invention mainly divides
For feeding device, horizontal type anaerobic reaction unit, collecting methane and purification device, warming solar energy device and biogas residue dehydration device
Deng.Excess sludge enters in storage tank, is transported to certain altitude by elevator, under the action of screw conveyor from top into
Enter in anaerobic fermentation tank, fermentor is horizontal type anaerobic fermentor, can monitor pressure, flow and liquid level etc. automatically, can supervise in real time
Control.
The biogas that anaerobic fermentation generates is by being dehydrated and being collected and utilize after desulfurizing and purifying.It discharges and fills provided with biogas residue
It sets, biogas residue is dehydrated by plate type pressure filter.In order to realize reactor whole year stable operation, overcome under winter or low temperature condition
The low problem of reaction efficiency, devises warming solar energy facility, can maintain the annual stable operation of reactor.Horizontal reacting device
Volume be 50m3.It is fed by the way of continuous feed when reactor start-up, the 1st day into 10 tons of excess sludge, after
Charging is completed in 1 ton, 1 month of charging daily, is fed 40 tons altogether, volume is 35 cubes, and methane phase strain is not added.Complete charging
It is periodically stirred daily afterwards, speed of agitator 5r/min, the anaerobic digestion time of start-up course is 73d.
Implementation column 2: heat preservation situation of the greenhouse to reactor
Temperature is to influence one of the key factor of anaerobic digestion effect, and different temperature corresponds to specific methane phase group,
The temperature fluctuation of anaerobic digestion cannot be too big, otherwise will affect the stability of methane phase effect.To investigate operation phase solar energy
The temperature control effect in greenhouse, has recorded in reactor, and the interior and outdoor temperature variations of greenhouse booth analyze April 20 days one
The situation of change (Fig. 2) of temperature in it；The data (Fig. 3) of 73 days temperature changes at the bottom of three months since have been had recorded simultaneously.From Fig. 2
Know that greenhouse temperature of shed is obviously higher by outdoor 10-12 DEG C, reactor temperature is higher by outdoor 6-9 DEG C, and reactor temperature
More stable, temperature fluctuation amplitude is small, and 26 DEG C of minimum temperature, 33.5 DEG C of maximum temperature, the reactor temperature difference is 7.5 DEG C, greenhouse booth
Interior temperature fluctuation is larger, and 38.2 DEG C of maximum temperature, 25.4 DEG C of minimum temperature, the temperature difference is 12.8 DEG C, and outside greenhouse maximum temperature 24.7
DEG C, 17.5 DEG C of minimum temperature outside greenhouse, the temperature difference reaches 7.4 DEG C.This show greenhouse not only to reactor have it is good heat effect,
And it plays a role to the stability of its temperature.
The case where Fig. 3 is temperature change in continuous 73 days, three inside and outside in early period reactor and greenhouse at temperature all in most
Low temperature is 10.2 DEG C, 15.1 DEG C and 11 DEG C respectively.Temperature is in maximum temperature in late reactor and three inside and outside greenhouse,
Respectively 30.8 DEG C, 41.2 DEG C and 37.2 DEG C.Canopy internal-external temperature difference is smaller when early period, outdoor temperature was minimum, and the temperature difference is 4.9 DEG C, in tank
Temperature and outdoor temperature difference only have 0.8 DEG C, and to the later period, when outdoor temperature highest, greenhouse inside and outside temperature difference is 10.4 DEG C, instead
It answers in device and outdoor temperature difference is 6.8 DEG C, it can thus be seen that greenhouse internal-external temperature difference is bigger when outdoor temperature is higher, temperature
Room to heat effect better.The second half section indoor/outdoor temperature-difference of start-up course is higher than reaction front half section.
Implementation column 3: the production gas situation of sludge in reactor operational process
Fig. 4 is the change curve that fermentor produces methane quantity and methane content, from figure it is found that reaction initial stage, reactor
Interior production gas effect is unobvious, but with the continuous progress of reaction, reactor daily output tolerance is constantly promoted, the speedup of initial stage daily gas
Relatively slowly, at the 25-55 days, reactor gas production was obviously improved, and produced tolerance daily from 3.9m3It is increased to 16m rapidly3, comparison diagram 3,
Temperature in this period reactor rises to 35 DEG C from 25 DEG C, and gas production and temperature improve rapidly, and the rising of temperature is significantly
The activity for improving methanogen improves digestive efficiency, when temperature of reactor reaches 35 DEG C, is conducive to the anaeration in normal temperature of sludge
Digestion.At the 55-65 days, reactor gas production rate maintained a higher level, by the 60th day after gas production declined,
This is mainly due to substrates most of in reactor to be utilized, and sufficient organic matter does not maintain higher anaerobism in system
Digestion rate, by the 73rd day, every gram of VS cumulative gas of sludge was 274mL in reactor.At 25 DEG C of outdoor temperature or so, greenhouse
Interior temperature is obviously higher by 10 DEG C or so of outdoor, and reactor temperature is higher by outdoor 7-8 DEG C, illustrates the raising with outdoor temperature, temperature
The temperature rise effect of room is become better and better.Initial stage produced methane in sewage gas amount known to the case where methane changes from figure is less, preceding
It is kept within 45 days a lower state, be continuously improved at the 45-60 days and reaches maximum value 58%, is kept at later
Between 40%-55%, gas production after corresponding 65 days produces the gas methane content in gas after a week that first peaks and peaks.
From methane quantity and methane content is produced analysis shows reactor anaerobic sludge digestion has carried out.
Implementation column 4: the situation of change of sludge VFA content in reactor operational process
In anaerobic fermentation process, organic matter is gradually volatile fatty acid (VFA) by microorganism conversion, and VFA can be used as production
The substrate of methane backeria is acted on by own metabolism and generates methane.But the VFA of higher concentration can cause fermentation system acidification, pH value
It reduces, microbial metabolism stagnation, fermentation process is caused to fail, Fig. 5 is 4 sample tap sludge VFA of startup stage fermentor
Situation of change, as can be seen from the figure VFA initial content is lower, and the 1st day to the 15th day, the content of VFA rapidly increased to
1500mg/kg, organic matter is decomposed into rapidly organic acid in this stage, and day VFA concentration slowly rises from the 15th day to the 42nd,
Reach maximum value 2395mg/kg at the 42nd day, day VFA concentration slowly rises from the 15th day to the 43rd, although this elementary reaction
Device temperature be continuously improved, but VFA content advance the speed and it is unhappy, the possible reason is methanogen utilize organic acid rate
It is continuously improved, the concentration to the 40th day organic acid is begun to decline, and is gradually decreased after fluctuation at the 40 to 55th day, 60 to 74
It, the amount of organic acid also reduces gradually, reduce in the 73rd day VFA content to 1800mg/kg or so, because sludge passes through 2 in tank
The content of organic matter is lower after digestion in a month, is metabolized without enough substrates for methanogen, gas production is caused to reduce.
Comparative reactor along the taken sludge of Cheng Si sample tap VFA concentration, due in reactor blender stirrer paddle have it is certain
Tilt angle, and reactor feed has shared about 30 days, can there is a plug-flow effect to sludge in reactor in charging, four groups of data
Variation tendency is almost the same.
Implementation column 5: in reactor operational process the case where the variation of ammonia nitrogen
Fig. 6 is the situation of change of ammonia nitrogen in start-up course, and as can be seen from the figure ammonia nitrogen concentration is from the beginning by the 60th day
All in the trend of rising, increase to 124.3mg/kg from the 49.9mg/kg of beginning, preceding 30 days ammonia nitrogens are advanced the speed than rear 30
Faster, with the progress of digestion reaction, itrogenous organic substance is largely degraded it rate, and system discharges a large amount of ammonia nitrogens, meanwhile, it produces
Methane backeria increased activity is greater than yield to the degradation rate of acid, and ammonia nitrogen concentration is integrally in the trend of rising.4 sample tap dirts
Mud ammonia-nitrogen content is integrally presented otherness, and concentration of No. 4 mouth sludge ammonia nitrogen concentrations in change procedure is above other several groups, and 1
Number sludge ammonia-nitrogen content is minimum, this may be because the plug-flow effect of reactor stirring, which makes, different has different disappear along the sludge of journey
Change the time, No. 4 mouth sludge digestion time longests, No. 1 mouth sludge digestion time is most short, and ammonia nitrogen amount is tired in the longer sludge of digestion time
Product is more, so No. 4 sludge ammonia nitrogen values are higher than other several groups.
Implementation column 6: the situation of change of VS in reactor operational process
Fig. 7 is the situation of change of 4 sample tap sludge VS during reactor start-up.React 4 sample tap sludge early period
VS is increased to 10% or so by 5% almost without apparent variation, preceding 20 days VS conversion ratios, and by the 20th day, VS content was about
10.2%, the conversion rate of VS was obviously accelerated since the 30th day, and conversion ratio is increased to about 38.5% from 10%, to the 73rd day VS
Value is 7%, and VS/TS is about 35.7% at this time, comparison diagram 3 it is found that early period rate it is lower, and the higher reason of later period rate, this
It is not to be inoculated with anaerobic sludge, on the other hand because one side reactor feed uses excess sludge as digestion substrate completely
The digestion temperature in later period improves 10 DEG C or so than early period, and the temperature in later period is more advantageous to the anaerobic digestion of sludge.Compare 4 samplings
The conversion ratio of mouth sludge VS, No. 4 sample tap sludge VS degradation rate initial values are greater than No. 1 sludge, this is because near No. 4 sample taps
The residence time of sludge is greater than the sludge near No. 1 sample tap.It is bright that the VS conversion ratio of 4 taken sludge of sample tap is presented in this
Aobvious otherness.
Implementation column 7: the situation of change of protein content in reactor operational process
What Fig. 8 reflected is the variation tendency of protein in sludge, and with the increase of digestion time, protein contains in sludge
Amount is constantly reduced, and the 73rd day 269mg/kg is reduced to from initial 425mg/kg, degradation rate is about 36.7%.Wherein from the 20th
By the 60th day, the degradation rate of protein was most fast, and degradation rate is the 65% of total degradation amount, this is primarily due to suitable temperature and mentions
The high digestion effect of sludge.4 groups of sludge situations of change are compared, the sludge protein content of No. 4 mouths is bright during digestion
It is aobvious to be lower than other several groups, this is because the sludge near No. 4 experienced longer digestion delay, No. 4 sample taps compared with other several groups
The digestion time of sludge is greater than the sludge of No. 3 sample taps.The sludge digestion time of No. 3 sample taps is greater than No. 2 and No. 1 sample tap dirt
Mud, protein content are also lower compared with No. 2 and No. 1.
Implementation column 8: the situation of change of polyoses content in reactor operational process
What Fig. 9 reflected is the variation of polyoses content in each delay sludge in digestion process, compares Fig. 8 Fig. 9, the change that the two has
Change trend is more similar, illustrates that protein and polysaccharide are all the organic matters that can be degraded in anaerobic digestion, polysaccharide concentration is opened from one
The 315mg/kg of beginning is reduced to the 73rd day 220mg/kg, and degradation rate has reached 30.1%, the slightly below degradation rate of protein, this
It is because total protein is more in excess sludge, the utilization efficiency in digestion process is higher.
Claims (3)
1. a kind of method for handling excess sludge, is handled using excess sludge processing unit, which is characterized in that described surplus
Remaining sludge treatment equipment mainly includes feeding device, horizontal type anaerobic reaction unit, collecting methane and purification device, warming solar energy
Device and biogas residue dehydration device；The warming solar energy device is arranged in horizontal type anaerobic reaction unit outer layer；Feeding device and sleeping
The feed inlet of formula anaerobic reaction device connects, and biogas collection device is connected with horizontal type anaerobic reaction unit；Wherein, described horizontal to detest
The reactor of oxygen reaction unit generally Horizontal cylinder body, lateral diameters and length of tank ratio are 1:5；The warming solar energy
Device is the sunlight board with ultraviolet-absorbing film, and pulling flow type agitating device is had in the horizontal type anaerobic reaction unit, described
Feeding device is screw conveyor, and the dischargeable capacity of horizontal type anaerobic reaction unit is 40m3；The horizontal type anaerobic reaction unit opens
It is fed by the way of continuous feed when dynamic, it is complete in the 1st day into 10 tons of excess sludge, 1 ton, 1 month of charging daily later
It at charging, feeds 40 tons altogether, volume is 35 cubes, and methane phase strain is not added；It is periodically stirred, stirs daily after completing charging
Mixing revolving speed is 5r/min, and the anaerobic digestion time of start-up course is 73d.
2. the method according to claim 1, wherein the pH of the excess sludge be 7.2 ~ 8.0, TS 18 ~ 22%,
VS/TS 55 ~ 60%, 20 ~ 26mg/kg of ammonia nitrogen, 135 ~ 160g/kg of total carbon, 25 ~ 30g/kg of total nitrogen, carbon-nitrogen ratio 5.0 ~ 5.5.
3. the method according to claim 1, wherein the method is to use the excess sludge of solid content 20%
Horizontal reactor carries out Anaerobic Digestion.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1812936A (en) * | 2003-06-24 | 2006-08-02 | 埃尔加利亚公司 | Method for anaerobic sludge digestion and a digester |
| CN102531312A (en) * | 2012-01-12 | 2012-07-04 | 北京昊海天际科技有限公司 | Technology for treating sludge by using dry anaerobic fermentation and low-temperature carbonization |
| CN204265621U (en) * | 2014-12-03 | 2015-04-15 | 北京佳瑞环境保护有限公司 | Sludge anaerobic digestion system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1812936A (en) * | 2003-06-24 | 2006-08-02 | 埃尔加利亚公司 | Method for anaerobic sludge digestion and a digester |
| CN102531312A (en) * | 2012-01-12 | 2012-07-04 | 北京昊海天际科技有限公司 | Technology for treating sludge by using dry anaerobic fermentation and low-temperature carbonization |
| CN204265621U (en) * | 2014-12-03 | 2015-04-15 | 北京佳瑞环境保护有限公司 | Sludge anaerobic digestion system |
Non-Patent Citations (1)
| Title |
|---|
| 用于污泥厌氧消化的温室-太阳能热水器组合增温***;孟成林等;《农业工程学报》;20090930;第25卷(第9期);第210页引言至第211页2.1节、第213页第3节 * |
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