CN203878041U - Organic sludge high-temperature micro-aerobic-anaerobic digestion device - Google Patents
Organic sludge high-temperature micro-aerobic-anaerobic digestion device Download PDFInfo
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- CN203878041U CN203878041U CN201420084349.3U CN201420084349U CN203878041U CN 203878041 U CN203878041 U CN 203878041U CN 201420084349 U CN201420084349 U CN 201420084349U CN 203878041 U CN203878041 U CN 203878041U
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- 239000010802 sludge Substances 0.000 title claims abstract description 67
- 238000000855 fermentation Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims description 26
- 238000005273 aeration Methods 0.000 claims description 22
- 238000010992 reflux Methods 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000005070 sampling Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 15
- 239000001301 oxygen Substances 0.000 abstract description 15
- 229910052760 oxygen Inorganic materials 0.000 abstract description 15
- 238000010438 heat treatment Methods 0.000 abstract 2
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- 238000000034 method Methods 0.000 description 38
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- 239000007787 solid Substances 0.000 description 10
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- 238000009413 insulation Methods 0.000 description 5
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 5
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
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- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
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- 229910052698 phosphorus Inorganic materials 0.000 description 1
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Classifications
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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
- Y02W10/20—Sludge processing
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Abstract
The utility model discloses an organic sludge high-temperature micro aerobic-anaerobic digestion device, which comprises a high-temperature aerobic reactor, an anaerobic fermentation reactor and a pH value adjusting tank; the pH value adjusting tank is arranged between the high-temperature micro-aerobic reactor and the anaerobic fermentation reactor, a discharge port of the self-heating high-temperature micro-aerobic reactor is communicated with the pH value adjusting tank through a pipeline, and the pH value adjusting tank is communicated with a feed port of the anaerobic fermentation reactor through a pipeline and a pump. The sludge after the self-heating type high-temperature microaerobic digestion can be used for adjusting the pH value in a pH value adjusting tank and releasing dissolved oxygen, and the pH value adjusting tank also plays a role of a blending tank, so that the sludge can be conveniently taken out from the pH value adjusting tank by a pump and pumped into an anaerobic fermentation reactor.
Description
Technical field
The utility model relates to the process field of solid waste, is specifically related to a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device.
Background technology
Along with the development of Chinese society economy and urbanization, the quantity of municipal effluent is in continuous growth.It is predicted, within 2010, China's urban wastewater discharge will reach 44,000,000,000 m
3/ d; The year two thousand twenty will reach 53,600,000,000 m
3/ d.Although at present wastewater treatment in China amount and processing rate are not high, municipal sewage plant discharges about 300,000 tons of dewatered sludge every year, but also with annual 10% speed increment
[2]., there is the light mud phenomenon of heavy water in existing sewage work of China, has mud greatly there is no stabilization treatment and harmless treatment, sludge treatment facility is not effectively operation also, mud is not properly disposed, and causes environmental pollution, has suppressed the long-term sustainable development of municipal wastewater treatment plant.At present, how effectively processing municipal sludge is the most important and complicated problem facing in dirty (giving up) water treatment field in international coverage.
Sludge digestion technology is degraded and is reached the stabilization of mud and innoxious organism by microorganism.Existing sludge digestion technique mainly contains traditional aerobic sigestion technique, conventional mesophilic anaerobic digestion technique, two-stage anaerobic digestion technique, anoxic/aerobic sigestion technique, autothermal thermophilic aerobic digestion technique, two sections of high-temperature aerobic/mesophilic anaerobic digestion techniques.
Two sections of high-temperature aerobic/mesophilic anaerobic digestion techniques wherein combine autothermal thermophilic aerobic digestion technique with mesophilic anaerobic digestion technique, first with one section of high loading autothermal thermophilic aerobic digestion process system, mud is carried out entering anaeration in normal temperature reactor after pre-treatment again.This technique can significantly improve the stability of clearance to pathogenic bacteria and the operation of follow-up mesophilic anaerobic digestion, but this technique is still in the experimental phase.
For example Chinese patent literature CN 100486722C(application number 200610087577.6) a kind of two stages semi-solid state organic waste digestion composting gas-made technology disclosed, semi-solid state organic waste are digested under the high-temperature micro-aerobic of connecting and anaeration in normal temperature condition, hot stage is killed pathogenic bacterium, predecomposition refuse, the main decomposition refuse of middle thermophase, generation biogas, final product is rich in humic acid, nitrogen, phosphorus, potassium; Concrete steps are that first semi-solid state organic waste enter high-temperature micro-aerobic digestion unit, in high-temperature micro-aerobic digestion unit, pass into air, maintain the dissolved oxygen concentration of semi-solid state refuse in high-temperature micro-aerobic digestion unit at 0.1～0.8mg/L, semi-solid state organic waste start to decompose, consume oxygen release reaction heat under microbial process again, Digestive system temperature can reach more than 55 DEG C, maintains 55 DEG C～70 DEG C of Digestive system temperature and keeps 1～3 day; The mesophilic anaerobic digestion unit that enters subordinate phase the quiet interchanger cooling of high temperature fluid of discharging from high-temperature micro-aerobic digestion unit, the used heat that interchanger reclaims is incubated mesophilic anaerobic digestion unit taking recirculated water as carrier; Mesophilic anaerobic digestion cell temperature maintains 35 DEG C～40 DEG C, pH value maintains 6.5～8, and the easy degradation material in Digestive system is constantly converted into biogas, and subordinate phase is after 15～20 days, digestion final product from mesophilic anaerobic digestion unit discharge, enter precipitation reservoir for subsequent use or sell.
There is the problem of oxygenation difficulty in this preparation technology's the high-temperature micro-aerobic stage, in actual job, under the hot conditions of 55 DEG C～70 DEG C, dissolved oxygen concentration is very low, and semisolid material oxygen transfer efficiency is low, oxygenation is very limited, therefore the method is difficult to reach oxygen condition according to the disclosed content of text, and cannot reach aerobic condition, first stage cannot discharge enough heats, the easy anaerobic acidification of organic solid, and the sludge pH value flowing out from the first stage is lower, cause subordinate phase anaerobic digestion process cannot produce biogas, and the anaerobic digestion residence time is long; In addition according to the current disclosed content of the method, the more difficult target temperature that controls to of mesophilic anaerobic digestion temperature, this is because the waste heat low (temperature difference heat of 55 DEG C～70 DEG C to 35 DEG C～40 DEG C is little) that interchanger reclaims is difficult to reach insulation effect; Anaerobic pond is because the residence time is long, bulky, reaches insulation effect effect in the winter time just lower by interchanger.
Utility model content
Technical problem to be solved in the utility model is to provide a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device.
The technical scheme that realizes the utility model object is a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device, comprises high-temperature aerobic reactor and anaerobic fermentation reactor, also comprises pH value equalizing tank; Described high-temperature aerobic reactor is autothermal high-temperature micro-aerobic reactor; PH value equalizing tank is arranged between high-temperature micro-aerobic reactor and anaerobic fermentation reactor, the discharge port of autothermal high-temperature micro-aerobic reactor communicates with pH value equalizing tank by pipeline, and pH value equalizing tank is connected with the opening for feed of anaerobic fermentation reactor with pump by pipeline.
Autothermal high-temperature micro-aerobic reactor comprises retort, sludge reflux system, aerating system, temperature sensor and gas absorption treating device; Described sludge reflux system is arranged on retort outside, comprises hypomere pipeline, sludge reflux pump and epimere pipeline; Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form a loop communicating; Aerating system includes aeration tube, aeration head, tensimeter, and aeration tube is arranged in the bottom of retort; Temperature sensor respectively arranges one in top, middle part, the bottom of retort; Gas absorption treatment unit is arranged on the top of retort, communicates with the inside of retort by pipeline.
Described anaerobic fermentation reactor comprises retort, agitator, collection and confinement of gases strainer, temperature sensor, gas sampling tube and circulating water line.Agitator comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of retort, bar axle penetrates retort inside from the top down, agitating vane arranges two-layer on bar axle, wherein the agitating vane of lower floor is arranged on the bottom of retort, and the agitating vane on upper strata is arranged on the middle part of available depth in retort.
Circulating water line is arranged on retort bottom, is connected with boiler by pipeline, and the gas-cooker of boiler is connected with the air outlet of collection and confinement of gases strainer by pipeline.
The utlity model has positive effect: (1) organic sludge autothermal of the present utility model high-temperature micro-aerobic-anaerobic digestion device is in series by autothermal high-temperature micro-aerobic reactor and anaerobic fermentation reactor.Leading portion autothermal high-temperature micro-aerobic reactor passes through Insulation, the heat discharging in volatile organic matter aerobic sigestion process is incubated, add mechanical heat production, thereby reactor is reached from being warming up to 45 DEG C～65 DEG C, the digestion of guarantee high-temperature micro-aerobic is carried out smoothly.
Selectablely in back segment anaerobic fermentation reactor carry out mesophilic digestion or thermophilic digestion, wherein mesophilic anaerobic digestion has utilized the heat that mud that autothermal high-temperature micro-aerobic reactor flows out carries, and does not need external heat source, saves cost; And the heat that the mud that a thermal source part for thermophilic digestion flows out from the autothermal high-temperature micro-aerobic of leading portion carries, the source of another part thermal source is that the methane that combustion high temperature anaerobic digestion produces obtains, and does not need equally external heat source, saves cost.Anaerobic fermentation reactor can produce the methane gas with energy substance, has carried out recycling; And mud has retained nitrogen phosphorus nutrition composition after digestion, can be agricultural after dehydration, solve the final outlet of mud.
(2) slaking apparatus of the present utility model comprises pH value equalizing tank, the postdigestive mud of autothermal high-temperature micro-aerobic can regulate pH value and discharge dissolved oxygen in pH value equalizing tank, because autothermal high-temperature micro-aerobic digestible energy produces a large amount of VFA, produce methane for anaerobic digestion process, but VFA can cause pH value to decline, so, before entering anaerobic pond, can in pH value equalizing tank, add alkali lye, the pH value in anaerobic digester is transferred between 6.8～7.2, not exceed 7.5.In addition, pH value equalizing tank can stay for some time for the mud after thermophilic digestion, and the mud flowing out from autothermal high-temperature micro-aerobic digester, is with some dissolved oxygen, need to discharge, and can not be brought into anaerobic pond, otherwise can kill anerobe.PH value equalizing tank also plays preparing pool effect, is convenient to pump mud is taken out from pH value equalizing tank, is pumped in anaerobic fermentation reactor.
(3) slaking apparatus compact construction of the present utility model, simple to operate, can be built on the ground, also can be buried or half buried, save the area, and beautify the environment.
Brief description of the drawings
Fig. 1 is the structural representation of slaking apparatus of the present utility model;
Mark in above-mentioned accompanying drawing is as follows:
High-temperature micro-aerobic reactor 1, retort 11, opening for feed 11-1, discharge port 11-2, drain 11-3, sludge reflux system 12, aerating system 13, temperature sensor 14, gas absorption treatment unit 15;
Anaerobic fermentation reactor 2, retort 21, opening for feed 21-1, discharge port 21-2, drain 21-3, agitator 22, collection and confinement of gases strainer 23, temperature sensor 24, gas sampling tube 25, circulating water line 26; PH value equalizing tank 3.
Embodiment
(embodiment 1)
See Fig. 1, the organic sludge high-temperature micro-aerobic-anaerobic digestion device of the present embodiment comprises autothermal high-temperature micro-aerobic reactor 1, anaerobic fermentation reactor 2 and pH value equalizing tank 3.PH value equalizing tank 3 is arranged between high-temperature micro-aerobic reactor 1 and anaerobic fermentation reactor 2, the discharge port of autothermal high-temperature micro-aerobic reactor 1 communicates with pH value equalizing tank 3 by pipeline, and pH value equalizing tank 3 is connected with the opening for feed of anaerobic fermentation reactor 2 with pump by pipeline.
Autothermal high-temperature micro-aerobic reactor 1 comprises retort 11, sludge reflux system 12, aerating system 13, temperature sensor 14 and gas absorption treating device 15.
The periphery of described retort 11 is provided with thermal insulation layer, and retort 11 is provided with opening for feed 11-1, discharge port 11-2 and drain 11-3.Opening for feed 11-1 is arranged on the upper end of retort 11, and discharge port 11-2 and drain 11-3 are arranged on the bottom of retort 11.Retort 11 inside are provided with intake zone, reaction zone and discharge zone, described intake zone on top, reaction zone at middle part, discharge zone is in bottom.
Sludge reflux system 12, in retort 11 outsides, comprises hypomere pipeline, sludge reflux pump and epimere pipeline, and hypomere pipeline is provided with vacuum breaker.The hypomere pipeline of sludge reflux system 12 is connected with the bottom of retort 11, and the discharge end of epimere pipeline is connected with the top of retort 11.Sludge reflux pump is arranged between hypomere pipeline and epimere pipeline, and mud is extracted out from the bottom of retort 11, then reenters retort 11 inside from the top of retort 11.
Described aerating system 13 includes aeration tube, aeration head, tensimeter; Aeration tube is arranged in the bottom of retort 11; Aeration head is evenly distributed on aeration tube and with aeration tube and communicates.Aeration head can provide micro-bubble, and to increase contact area and the duration of contact of liquid phase, aeration head quantity is relevant with its service area; Whether tensimeter can monitor aeration head and stop up, so that dredging in time.When practical device of the present utility model, in initial reaction stage, organic sludge needs oxygen amount many, and aeration rate needs to strengthen; In the reaction later stage, organic sludge oxygen requirement is few, and aeration rate demand is few.In the aerating system of this reactor, also can set up under meter, be used for regulating the flow of aeration tube.
Temperature sensor 14 respectively arranges one in top, middle part, the bottom of retort 11, with the temperature of detection reaction tank 11 interior mud.
Gas absorption treatment unit 15 is arranged on the top of retort 11, communicates with the inside of retort 11 by pipeline.Described gas absorption treatment unit 15 is microbial film absorbing and filtering device, can process H
2s, SO
2deng sour gas.
Anaerobic fermentation reactor 2 comprises retort 21, agitator 22, collection and confinement of gases strainer 23, temperature sensor 24, gas sampling tube 25 and circulating water line 26.
Retort 21 is provided with opening for feed 21-1, discharge port 21-2 and drain 21-3, and opening for feed is arranged on the top of retort 21, and discharge port 21-2 is arranged on the middle part of retort 21, and drain 21-3 is arranged on the bottom of retort 21.
In retort 21, establish three regions, be divided into successively intake zone, reaction zone and discharge zone, intake zone is located at top, and reaction zone is located at bottom, and discharge zone is located at middle part.
Agitator 22 comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of retort 21, bar axle penetrates retort 21 inside from the top down, agitating vane arranges two-layer on bar axle, wherein the agitating vane of lower floor is apart from the bottom 30cm of retort 21, the agitating vane on upper strata is arranged on the middle part of retort 21 interior available depths, and the two-layer blade of driven by motor rotates the abundant mix and blend of mud in tank.Agitator 22 is not 24 hours direct-opens, but just opens in the time that retort 21 is carried out to heat supply, also stops stirring after heat supply finishes.
Collection and confinement of gases strainer 23 is arranged on the top of retort 21, communicates with the inside of retort 21 by pipeline.Collection and confinement of gases strainer 23 is collected the methane gas of retort 21 interior generations, and after being collected, storage or burning are to retort 21 heat supplies.
Temperature sensor 24 respectively arranges one in top, middle part, the bottom of retort 21, with the temperature of the mud in detection reaction tank 11 interior each regions.
Gas sampling tube 25 respectively arranges one in top, middle part, the bottom of retort 21, with the gaseous constituent in detection reaction tank 11 interior each regions.
Circulating water line 26 is arranged on retort 21 bottoms, is connected with boiler by pipeline, and the gas-cooker of boiler is connected with the air outlet of collection and confinement of gases strainer 23 by pipeline.
Using above-mentioned slaking apparatus to carry out high-temperature micro-aerobic-anaerobic digestion process to organic sludge comprises the following steps:
1. the domestication of bacterial classification.
Getting solid content and be 5%～7% municipal sludge packs in high-temperature micro-aerobic reactor 1, open sludge reflux system 12 and aerating system 13, aerobic sigestion for some time, treat temperature rise, and reach (being that the interior mud temperature of retort 11 no longer rises) after balance, 1/2 mud in discharge retort 11, then supplement the fresh sludge that solid content is 5%～7%, continue operation, repeat above-mentioned steps until the interior temperature of retort 11 reaches 50 DEG C～55 DEG C.More than treating temperature rise to 50 DEG C, stop aeration and sludge reflux, domestication finishes, and discharges a part of mud, and interior reserved 1/3 mud of retort 11 is as kind of a mud.
2. the high-temperature micro-aerobic digestive process of organic sludge.
Open sludge delivery pump, to the organic sludge of sending into 2/3 effective volume of retort 11 in the retort 11 of autothermal high-temperature micro-aerobic reactor 1, after organic sludge and reserved domestication, mud is filled reactor, reaches effective volume, and reactor has 0.5m superelevation; Organic sludge solid content is 4%～7%, and volatility organic solid concentration accounts for 60%～80%; Open sludge reflux system 12 and aerating system 13, the aeration rate of aerating system 13 is 10～14m
3/ h, organic sludge starts high-temperature micro-aerobic digestive process.Mud stops and within 2～3 days, carries out high-temperature micro-aerobic digestive process in autothermal high-temperature micro-aerobic reactor.In high-temperature micro-aerobic digestive process, redox potential ORP is 0～-100mv.
In digestive process, sludge aerobic digestive process is from heat release, sludge reflux is supplied with the mechanical energy that is no more than 30%, while is because the periphery of the reactor body of autothermal high-temperature micro-aerobic reactor 1 is provided with thermal insulation layer, make to digest temperature without external heat source, maintain between 45 DEG C～65 DEG C, under this high temperature, organic sludge is carried out to sterilizing, realize the rear sewage sludge harmlessness of digestion.If temperature of reactor rises to more than 65 DEG C, strengthen aeration rate, close sludge reflux, heat radiation is increased, to realize cooling.
Because the sludge concentration in input reactor is high, viscosity is large, oxygen requirement is many, and that mass transfer enters the oxygen amount of reactor is limited, in autothermal high-temperature micro-aerobic reactor, be therefore not exclusively aerobic, by the acting in conjunction of aerobic bacteria, amphimicrobe, anerobe, volatile organic matter is degraded, be easy to produce voltaile fatty acid (VFA), and VFA is under anaerobic, be easy to produce methane, therefore the high-temperature micro-aerobic digestive process of organic sludge is beneficial to the anaerobic digestion process of back segment organic sludge.
After high-temperature micro-aerobic digestion finishes, postdigestive mud enters pH value equalizing tank 3 from discharge port by pipeline, in pH value equalizing tank 3, drops into sodium hydroxide solution, and the pH value of the material in pH value equalizing tank 3 is transferred between 6.8～7.2.Mud after pH value regulates stops 3h～5h to discharge the dissolved oxygen in mud in pond.
3. the mesophilic anaerobic digestion of organic sludge.
Open sludge pump, 2. step discharges the mud through high-temperature micro-aerobic digestion of dissolved oxygen by being pumped in anaerobic fermentation reactor 2.Mud stops and completes anaerobic digestion process in 10～20 days in anaerobic fermentation reactor 2, and without external heat source, anaeration in normal temperature temperature is 33 DEG C～35 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
If the mud excess Temperature flowing out after the digestion of autothermal high-temperature micro-aerobic exceedes 60 DEG C, by the many stops heat radiation in several hours in pH value equalizing tank 3 of postdigestive high-temperature micro-aerobic mud.If anaerobic pond temperature does not reach mesophilic range, the mud temperature of autothermal high-temperature micro-aerobic digestion can be improved as far as possible, by reducing aeration rate, strengthening sludge reflux to mechanical heat, make high-temperature micro-aerobic digestion temperature reach 50 DEG C～60 DEG C, ensure the middle temperature of anaerobic pond.
Slaking apparatus of the present utility model belongs to two-stage series connection reactor, autothermal high-temperature micro-aerobic reactor is uniformly mixed by sludge reflux, mix without dead angle, reach sludge suspension effect, promote microbial biochemical reaction, microorganism autoxidation is reacted completely, in autothermal high-temperature micro-aerobic reactor, discharge enough heats through micro-aerobic sigestion, guarantee the condition of high temperature of micro-aerobic reactor and the middle temperature state of the interior mud of anaerobic fermentation reactor.
When actual motion, adopt semi continuous charging marker method.In the present embodiment, the autothermal high-temperature micro-aerobic digested sludge residence time is 2 days, and anaerobically digested sludge stops 12 days.
If autothermal high-temperature micro-aerobic digestion reactor effective volume is V, it is V/2 that first day enters mud amount, stops two days, within the 3rd day, enters mud V/2, spoil disposal V/2.Enter every other day mud and spoil disposal.From autothermal high-temperature micro-aerobic digestion reactor, discharge mud V every day, enter anaerobic digester, anaerobic digester volume is 12V, so sludge retention time is 12 days.Anaerobic digester sludge volume every day V.Entering like this mud and spoil disposal equates.
For the digestion of autothermal high-temperature micro-aerobic, owing to being autothermal, temperature rise is not easy, so the reactor volume in the present embodiment is 10m
3.The autothermal high-temperature micro-aerobic digestion phase temperature of the present embodiment can reach between 45 DEG C～65 DEG C, though winter can be on the low side, because the greatly low energy of reactor volume maintains 50 DEG C.
The utilization of organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present utility model the advantage of the own heat production of autothermal high-temperature micro-aerobic digestible energy, do not need external heat source, save cost.
The anaerobically fermenting of slaking apparatus of the present utility model is mesophilic digestion, has utilized the heat that in autothermal high-temperature micro-aerobic, mud carries, and does not need external heat source, saves cost.Anaerobic fermentation reactor can produce the methane gas with energy substance, has carried out recycling; And mud has retained nitrogen phosphorus nutrition composition after digestion, can be agricultural after dehydration, solve the final outlet of mud.
(embodiment 2)
All the other are identical with embodiment 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present embodiment, and difference is:
Step 3. organic sludge is carried out thermophilic digestion.
Open the valve of connecting tube, 2. step discharges the mud through high-temperature micro-aerobic digestion of dissolved oxygen by being pumped in anaerobic fermentation reactor 2.Mud stops and within 6～10 days, completes anaerobic digestion process in anaerobic fermentation reactor 2, and the temperature of thermophilic digestion is 50 DEG C～55 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
Thermophilic digestion can make speed of response accelerate.The heat that the mud that a thermal source part for thermophilic digestion flows out from the autothermal high-temperature micro-aerobic of leading portion carries, the source of another part thermal source be methane collection after-burning that thermophilic digestion is produced heat up water the steam that obtains or hot water by the circulating water line 26 in anaerobic fermentation reactor 2 to the mud heat supply in retort 21 to maintain the high temperature of 50 DEG C～55 DEG C.
In the time that the temperature of anaerobic fermentation reactor 2 declines,, when circulating water line 26 heat supply, to open agitator 22 and make spread heat even with the mud heat supply in retort 21 to the interior delivering vapor of circulating water line 26 or hot water, heat supply finishes to stop to stir.
(embodiment 3)
All the other are identical with embodiment 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present embodiment, and difference is:
Autothermal high-temperature micro-aerobic reactor 1 also comprises defoaming system, and described defoaming system comprises air froth breaking pipe, jet orifice; Described air froth breaking pipe is arranged in the top of retort 11, evenly has aperture on tube wall; Described jet orifice is arranged on the top of reactor body.When the work of this defoaming system, the gas blowing out by the aperture on air froth breaking tube wall is smashed foam; Jet orifice can spray defoamer, and defoamer is ejected in reactor, is distributed on whole liquid level by stirring of agitator, plays froth breaking effect.
The step of digestion method is 2. in the high-temperature micro-aerobic digestive process of organic sludge, and defoaming system is broken to sending into air in retort the bubble producing in retort, and digestive process is carried out smoothly.
Claims (2)
1. organic sludge high-temperature micro-aerobic-anaerobic digestion device, comprises high-temperature aerobic reactor and anaerobic fermentation reactor (2), it is characterized in that: also comprise pH value equalizing tank (3); Described high-temperature aerobic reactor is autothermal high-temperature micro-aerobic reactor (1); PH value equalizing tank (3) is arranged between high-temperature micro-aerobic reactor (1) and anaerobic fermentation reactor (2), the discharge port of autothermal high-temperature micro-aerobic reactor (1) communicates with pH value equalizing tank (3) by pipeline, and pH value equalizing tank (3) is connected with the opening for feed of anaerobic fermentation reactor (2) with pump by pipeline;
Autothermal high-temperature micro-aerobic reactor (1) comprises retort (11), sludge reflux system (12), aerating system (13), temperature sensor (14) and gas absorption treating device (15); Described sludge reflux system (12) is arranged on retort (11) outside, comprises hypomere pipeline, sludge reflux pump and epimere pipeline; Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form a loop communicating; Aerating system (13) includes aeration tube, aeration head, tensimeter, and aeration tube is arranged in the bottom of retort (11); Temperature sensor (14) respectively arranges one in top, middle part, the bottom of retort (11); Gas absorption treatment unit (15) is arranged on the top of retort (11), communicates with the inside of retort (11) by pipeline.
2. organic sludge high-temperature micro-aerobic-anaerobic digestion device according to claim 1, is characterized in that: anaerobic fermentation reactor (2) comprises retort (21), agitator (22), collection and confinement of gases strainer (23), temperature sensor (24), gas sampling tube (25) and circulating water line (26);
Agitator (22) comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of retort (21), bar axle penetrates retort (21) inside from the top down, agitating vane arranges two-layer on bar axle, wherein the agitating vane of lower floor is arranged on the bottom of retort (21), and the agitating vane on upper strata is arranged on the middle part of the interior available depth of retort (21);
Circulating water line (26) is arranged on retort (21) bottom, is connected with boiler by pipeline, and the gas-cooker of boiler is connected with the air outlet of collection and confinement of gases strainer (23) by pipeline.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803770A (en) * | 2014-02-26 | 2014-05-21 | 江苏理工学院 | High-temperature microaerobic-anaerobic digestion device and method for organic sludge |
| CN106007278A (en) * | 2016-06-21 | 2016-10-12 | 昆明理工大学 | Sludge treatment method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803770A (en) * | 2014-02-26 | 2014-05-21 | 江苏理工学院 | High-temperature microaerobic-anaerobic digestion device and method for organic sludge |
| CN103803770B (en) * | 2014-02-26 | 2015-10-07 | 江苏理工学院 | High-temperature microaerobic-anaerobic digestion device and method for organic sludge |
| CN106007278A (en) * | 2016-06-21 | 2016-10-12 | 昆明理工大学 | Sludge treatment method |
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