CN104768880A - A method for the in-situ thermal-alkaline treatment of organic waste to enhance anaerobic solids degradation and biogas generation - Google Patents

A method for the in-situ thermal-alkaline treatment of organic waste to enhance anaerobic solids degradation and biogas generation Download PDF

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CN104768880A
CN104768880A CN201380054798.1A CN201380054798A CN104768880A CN 104768880 A CN104768880 A CN 104768880A CN 201380054798 A CN201380054798 A CN 201380054798A CN 104768880 A CN104768880 A CN 104768880A
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organic waste
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CN104768880B (en
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周琰
郭成洪
伍文桢
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Nanyang Technological University
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Abstract

There is disclosed a process for the treatment of organic waste comprising the steps of: introducing a feed stream comprising organic waste into a first reactor; generating an effluent from the first reactor; and providing the effluent from the first reactor to a second reactor, wherein the first reactor is maintained at a pH of from about 6.5 to about 10.0. There is also disclosed a plant adapted for running and/or using said process.

Description

A kind of for in-situ heat alkaline purification organic waste with improve Solid anaerobic degraded and biogas generation method
Technical field
The present invention relates to a kind of method of process organic waste of improvement and improve biosolids degraded and biogas generation in bio anaerobic Digestive tract.Such as, the method for sludge treatment that the present invention relates to a kind of improvement generates to improve biosolids degraded and biogas in bio anaerobic Digestive tract.
Background technology
This specification sheets is enumerated or is discussed to be counted as admit that described file is a part or the common practise of prior art front disclosed file.
The sludge treatment of sewage work (WWTP) can consume about 50% of total operating cost.The application anaerobic digestion of many sewage works is removed the organism in degraded mud and generates biogas so that recovered energy.Organic sludge steam is hydrolyzed, and carries out acid production and methanogenesis afterwards.Acid production generates voltaile fatty acid (VFA), carbonic acid gas (CO 2) and a small amount of hydrogen (H 2), methanogenesis generates carbonic acid gas and methane (CH simultaneously 4).In traditional single-stage (single stage) system, the pH of hydrolysis is about 7, and traditional two-phase (2-phase) system, pH value is less than 6 usually.
Although anaerobic digestion is stage by stage in essence, the anaeroic digestor used in traditional sludge digestion process is typical single stage type.But, although anaerobic process completely are stage by stage actually and are difficult to realize, if success, probably can realize the conversion of high per-cent and the organism stabilization of two-forty and gas and generate.Usual hypothesis acid production is optimize under the pH being less than 6.5, and methanogenesis is mainly about pH7.Therefore, in single-phase (singlephase) system, the CO comprised from acid production is generated 2with the CO from methanogenesis 2and CH 4biological air-flow.In such a system, system pH must Cautious control because methanogenesis to low ph value and high ph-values all responsive, mean that pH needs to maintain in the scope of 6.5 to 7.5.
Two-phase anaerobic digestion system and/or method have been used to hydrolysis/acid-producing and product acetic acid/methane phase reacts and separate, allow each react respectively lower pH and lower than the neutral pH of 8.0 under carry out.This method allows the operational condition optimizing acid production and methanogenesis individually, thus optimal conditions is to maintain specified microorganisms involved in material to the different transformation stages of biogas.This two stages occur simultaneously and provide the condition of optimization for acid-producing bacteria and methanogen in two different reactors, thus improve the performance of whole system, comprise organic degraded, more specifically, comprise methane generation and carbon dioxide fixation.But, it is noted that also the unrealized stage is completely separated (namely producing being separated completely of acid phase and methane phase stage) in laboratory with entity apparatus.This means that the gas of self-produced acid phase is by containing a small amount of CH 4(< 20%).
In product acid phase, major objective is that biodegradable organism is converted into voltaile fatty acid (VFA).The acid-producing bacteria being responsible for VFA conversion is mainly present in the mud producing acid, and described acid-producing bacteria comprises:
(1) fermenting bacteria, described fermenting bacteria is responsible for generating VFA;
(2) hydrogen-producing acetogenic bacteria, propionic acid, other VFA and alcohol metabolism are acetate and H by described hydrogen-producing acetogenic bacteria 2; With
(3) homoacetogenic bacteria, described homoacetogenic bacteria utilizes H 2and CO 2produce acetate.
In the methane phase stage, the VFA generated in consumption product acid phase is to generate methane and carbon dioxide.
The anaerobic digestion of mud is subject to the obstruction of large-sized organic particle and microorganism wall (if especially comprising the rubbish from cooking of secondary sludge) usually.Therefore, the hydrolysis of mud granule can become the overall rate-limiting step of whole process in the above-mentioned single-stage mentioned or two-phase reactor.In order to improve hydrolysis dynamics, have studied various pretreatment process to decompose mud and microorganism wall.These methods comprise ultrasonication, ozone oxidation, alkaline purification, Fenton process (Fenton process) and enzymolysis processing.
Compared with additive method, alkaline purification has some advantages, such as, use simple device, easy handling and efficiency is high.In pre-treatment, use the alkaloid substance of larger dose can produce pH higher in the mud of higher solid abatement and process.But although the content of VFA can significantly increase after alkaline purification, the high pH of the mud of process can suppress follow-up methane phase step.After alkaline purification, the high density of consequential total dissolved solidss (TDS) also can suppress microorganism.Usual way is removed neutralization bases material with acid and reduced pH before the mud of process is dropped into anaerobic system.Which increase the cost of sludge treatment.
Therefore, in order to provide the better performance of expection, typical antibiotic wastewater needs strict pH to control (producing above-mentioned neutral pH process by low pH process) acid process and methane phase process to be separated.Then, before methanogenesis, needs acid neutralizes to be lowered by pH by oxygenation pretreatment.
Sludge hot process has been illustrated and has been effective as pre-treatment.The all temps within the scope of 60 to 270 DEG C has been reported in document.Under such process, the protein of mud and carbohydrate will be released before reaching 60 DEG C, and during more than 60 DEG C, further release will be restricted.
There is the method for the alkaline Pretreatment for waste sludge at present.These methods are chemical process and apply under very high pH value (10-12) and temperature, to improve the efficiency of sludge degradation.Then, before pretreated mud is fed into anaeroic digestor, in needing extra chemical reagent to go and pH, raw material and the cost of energy of increase is created.
In view of foregoing, be still necessary the method for sewage disposal that improvement is provided.
Summary of the invention
Unexpectedly, it is unnecessary that the strict pH used in traditional antibiotic wastewater controls for process organic waste, the organic waste such as processing oily sludge, oily(waste)water, rubbish from cooking, industrial sludge, sewage sludge and especially produce in sewage (namely from the mud of sewage disposal).Compared with main reactor typical in biphasic system, the main reactor running two-stage (2-stage) system in the basic conditions produces better solid relief performance, more stable CH 4generate and increase VFA and generate.
Described two-stage system only needs very little pH adjustment after pretreating sludge, because this reducing the cost relevant with using extra chemical reagent.In two-stage approach of the present invention, lower pH value and temperature is used to be possible, because chemical reaction combines with Enzymic reaction to realize being hydrolyzed and follow-up acid production by described method.Discharge/the effluent of the conditions permit first step of these gentlenesses is when less or be fed into the second main methane-producing reactor when not having pH correct and do not have temperature correction.The mild operating conditions had in first reactor can make methanogen floras survive in this reactor and utilize metabolite (the such as H producing and generate in sour step 2, CO 2and VFA) generate CH 4.This methanogen floras existed in first reactor can pass through H 2, CO 2control to propose the generation of metabolite in high acid step under certain level with the concentration of VFA, and this level can not suppress the generation of described metabolite further, and the existence of this methanogen can also be passed through H 2and CO 2be converted into CH 4improve the methane generation of the first step.
Therefore, in first aspect present invention, provide the method for the treatment of organic waste, comprise the steps: the incoming flow including organic waste to introduce the first reactor; Effluent is generated by the first reactor; Be provided to the second reactor with by the described effluent in the first reactor, wherein, described first reactor maintains pH about 6.5 to about 10.0 times.
In an embodiment of the present invention, the first reactor is provided in the upstream of the second reactor.
In one more embodiment of the present invention, under the first reactor maintains the pH of about 7.0 to about 9.0.Such as, under the first reactor can maintain the pH of about 7.5 to about 8.5, such as about 8.0.
In another embodiment of the invention, the first reactor is mainly hydrolyzed/acidogenic reactor.In another embodiment of the present invention, the second reactor is methane-producing reactor or single-stage anaerobic reactor mainly.
In another embodiment of the present invention, more specifically, the second reactor or the first reactor run at the temperature of about 35 DEG C to about 60 DEG C.Such as, more specifically, the second reactor or the first reactor can run at the temperature of about 50 DEG C to about 60 DEG C.Optional or selective, more specifically, the first reactor or the second reactor can run at about 35 temperature to about 49 DEG C.
In another embodiment of the present invention, the first reactor can run under the hydraulic detention time of about 2 hours to about 5 days.Such as, the first reactor runs under the hydraulic detention time of about 3 days to about 5 days.In another embodiment, solid/sludge retention time can be about 2 days to about 5 days.
In certain embodiments of the present invention, the second reactor can run under the hydraulic detention time more than 10 days.
In another embodiment, the second reactor runs under about 6.5 pH to about 7.9.Such as, the second reactor can run under about 6.8 pH to about 7.4, and such as about 7.1.
In embodiments of the present invention, charging is the organic waste comprising biodegradable solid.Such as, organic waste can be mud, such as waste sludge or secondary sludge.Alternatively, organic waste can be the organic waste of other type any, the oily sludge that such as organic content is high, industrial sludge, sewage sludge, rubbish from cooking, oily waste, solid waste, or their arbitrary combination.
In another embodiment, the first and second reactors comprise pH, redox-potential (ORP) and temperature regulator further.Such as, in the embodiment of described method, once method is stablized, ORP value can maintain the value being less than-100mV.
Estimate the method for above-mentioned general introduction by be applied to in conserve energy and recovered energy process the interested place of waste water and the restricted place of sludge treatment.Method and apparatus used herein can be used in sludge treatment factory and sewage work, and can use in new factory or add in existing installation as improvement and use.In improved plan, interpolation can also be used for for the device running disclosed method the processing power expanding existing installation, and therefore to avoid along with increase in demand the demand that existing installation is built again.
Similarly, in a second aspect of the present invention, provide and use the method for first aspect present invention and the waste reduction and disposal equipment of the disclosed embodiments.In embodiments of the present invention, waste reduction and disposal equipment can be sewage treatment equipment, such as sewage disposal device or industrial wastewater treatment device.
In a third aspect of the present invention, provide the reactor assembly for the treatment of organic waste, described reactor assembly comprises the first reactor and the second reactor, described second reactor is positioned at the downstream of described first reactor, and be connected with described first reactor fluid, wherein, described first and second reactors are applicable to method described in first aspect present invention and the disclosed embodiments.
In a third aspect of the present invention, the first reactor is mainly hydrolysis/acidogenic reactor.In another embodiment of the present invention, the second reactor is mainly methane-producing reactor or single-stage anaerobic reactor.In another embodiment of the present invention, the first and second reactors comprise pH, redox-potential (ORP) and temperature regulator further.
Accompanying drawing
In further detail the present invention is described by under the help of the following drawings below.
Resolvable chemical oxygen demand (SCOD) concentration in the reactor that Fig. 1 embodiment 1 is selected
Total VFA concentration in the reactor that Fig. 2 embodiment 1 is selected
Volatile suspended solid abatement in Fig. 3 embodiment 1 in two-stage system and simple system
Volatile solid abatement in Fig. 4 embodiment 1 in single-stage, two-phase and two-stage system
Volatile suspended solid abatement in Fig. 5 embodiment 3 in two-stage & simple system
Methane generation speed in Fig. 6 embodiment 3 in two-stage & simple system
In Fig. 7 embodiment 5 from the 76th day, the pH of 2 stage reactors is maintained the volatile solid abatement in the two-stage & simple system under 7.1
Methane generation speed in Fig. 8 embodiment 5 in two-stage and simple system
Fig. 9 embodiment 3 addicted to warm charging, addicted to warm single-stage reactor, addicted to temperature the 1st stage reactor and the absolute quantitation addicted to the bacterium obtained by RT-PCR in temperature the 2nd stage reactor and Archimycetes; And the thermophilic charging of embodiment 5, addicted to warm single-stage reactor, thermophilic 1st stage reactor and the absolute quantitation addicted to the bacterium obtained by RT-PCR in temperature the 2nd stage reactor and Archimycetes.
Describe
As shown here, it might not be in such a system for the treatment of the method for organic waste that the strict pH used in traditional antibiotic wastewater controls, described organic waste as mud (such as oily sludge, oily(waste)water, rubbish from cooking, industrial sludge, sewage sludge and especially from the mud of sewage disposal).Compared with main reactor typical in biphasic system, show at this main reactor running biphasic system in the basic conditions and obtain better solid relief performance, more stable CH 4the VFA generated and increase generates.
The system proposed has the hydrolysis/acidogenic reactor being different from acidogenic reactor traditional in antibiotic wastewater.Separate this is because the method target that described system uses does not lie in be generated by VFA completely with power consumption process.On the contrary, target is to increase solid abatement and VFA generation by original position alkaline purification, and is therefore increased in the methane generation in subsequent reactor.Relatively high pH (such as > 6.5 is applied in the first reactor, such as about 6.5 to about 10.0, such as about 7.0 to about 9.0, or about 7.5 to about 8.5, such as 8.0), this pH is higher than the pH used in biphasic system before.The pH of this increase means that the effluent of first step reactor can not suppress the reaction of the 2nd stage reactor.Therefore, in following described system, reactor two-stage layout instead of two-phase layout.Therefore first step reactor, running under those similar operating parameters desired in the acidogenic reactor of two-phase layout, except higher pH, and uses alkali to obtain this higher pH.The temperature of described 1st stage reactor is controlled in about 35 DEG C to about 60 DEG C, and preferred temperature range is about 50 DEG C to about 60 DEG C.But described 1st stage reactor can run at the temperature of 35 to 49 DEG C.The pH of the first reactor and temperature range facilitate chemical degradation and the biological degradation of suspended solids in introduced mud.
Two-stage reactor needs very little or does not need pH to adjust after pre-treatment biodegradable solid (such as mud).Therefore, relate to little additional chemical cost.Application relatively lower pH value and temperature is possible, because chemical reaction and Enzymic reaction combine to realize being hydrolyzed and follow-up acid production by the method proposed.The pretreatment condition of these gentlenesses allow the discharge/effluent of the 1st grade when less or do not have pH correct and there is no temperature correction put into the second main methane-producing reactor.Without being bound by theory, in first reactor, the operational conditions of these gentlenesses also allows methanogen to survive in this reactor and contributes to removing some metabolite generated (i.e. VFA), and described metabolite may suppress it to generate further.Given this, prove as following embodiment, the methanogen floras in the first reactor can utilize generated H 2, CO 2with VFA to generate CH 4.
Described method for the treatment of organic waste comprises the steps:
The incoming flow including organic waste is introduced in the first reactor;
Effluent is generated by the first reactor; With
Effluent in first reactor is provided to the second reactor,
Wherein, under the first reactor maintains the pH of about 6.5 to about 10.0.
Be understandable that, the first reactor is provided in the upstream of the second reactor.Namely, the second reactor is provided in the downstream of the first reactor, so that the second reactor receives the effluent (charging namely processed or mud) of the first reactor discharge and use this effluent in its reaction process.
When used herein, " downstream " means that particular reactor is set to receive at least some material generated by reactor before (mud such as processed or effluent), or directly or indirectly (such as one or more reactor can be arranged between downstream reactor and initial reactor).
When used herein, " upstream " mean particular reactor be set to provide at least some material generated by it (mud such as processed or effluent) to another reactor, or directly or indirectly (such as one or more reactor can be arranged between upstream reactor and another reactor).
The charging used in method can be the organic waste comprising biodegradable solid.Such as, biodegradable solid can be organic particle and/or microorganism wall.Organic waste can be mud (such as oily sludge, industrial sludge and sewage sludge) or other organic waste.Such as, charging can be the waste sludge from waste water treatment plant, secondary sludge, rubbish from cooking, oily waste or the solid waste that organic content is high.
As mentioned above, the pH of the first reactor can be about 6.5 to about 10.0.Such as, the first reactor can maintain about 7.0 under the pH of about 9.0 (such as about 7.5 to about 8.5), and such as about 8.0.Being understandable that, even if having selected the specific pH for maintaining, just naturally having fluctuation once add more effluent and/or add alkaline matter to increase or to reduce pH, pH.Such fluctuation may cause pH value to rise or the nearly unit that declines, the brief fluctuations of such as half unit.
PH value in described method can be monitored with pH meter and controller, like this when pH value is reduced to lower than predetermined level, adds a certain amount of alkaline matter so that pH value is returned to predetermined level in the first reactor.This monitoring and adjustment can automatically or by artificial interpolation be undertaken.Be understandable that, by alkaline matter being joined the first reactor control ph.These alkaline matters can be any alkaline matters that the pH of the mixture of generation will be caused to increase.Sodium hydroxide that is that the example of alkaline matter comprises particle form or aqueous solution form.It is also the potassium hydroxide, calcium hydroxide etc. of solid form or aqueous solution form (such as the 1N-5N aqueous solution) that further example comprises.
First reactor is mainly hydrolyzed/acidogenic reactor.Similarly, the first reactor can be hydrolyzed organic particle, such as microorganism wall by being combined with Enzymic reaction by chemical reaction, and can also maintain acid-producing bacteria group carries out acid production in the reactor simultaneously.This is by using the condition extremely similar to traditional acidogenic reactor (such as, the temperature run is about 35 to about 60 DEG C, such as about 50 to about 60 DEG C) be achieved, but pH scope be chosen as about 6.5 to about 9.0 (such as about 7.0 to about 8.5, or about 7.5 to about 8.25, such as about 8.0).This pH scope is higher than the pH scope used in traditional acidogenic reactor, and traditional acidogenic reactor runs under the pH value lower than 6.5 (such as 5.5).Although the first reactor is mainly used in carrying out the hydrolysis of particle and carries out acid production, the pH environment in reactor can also make methanogen floras survive in the first reactor, and methanogen floras can by least some hydrogen generated by acid-producing bacteria, CO 2methane is converted into VFA.That methanogen floras prevents in the first reactor and produces acid product (such as H with the advantage that there is methanogen floras relevant in the first reactor 2) the increase gradually of inhibition concentration, thus can make described product acid product be created on higher efficiency under proceed.
Be understandable that, the hydraulic detention time of any appropriate can be used to run the first reactor.Suitable hydraulic detention time comprises about 2 hours to about 5 days, such as about 3 days to about 5 days.In addition, the first reaction can be the solid/sludge retention time of about 2 days to about 5 days.
Second reactor is positioned at the downstream of the first reactor, can be methane-producing reactor or single-stage anaerobic reactor.Because the effluent of the first reactor or the mud of process have higher pH, it can when very little or directly put into the second reactor, because this reducing the cost relevant with whole technological process and energy requirement when not having pH correct and do not have temperature correction.Be understandable that, a more than reactor can in series or be concurrently set in the downstream of the first reactor.
When the second reactor is methane-producing reactor (or multiple reactor), the second reactor mainly methane-producing reactor.Namely, reactor can also containing a small amount of acid-producing bacteria group, and it is used for a large amount of methanogens that any unreacted acid-producing agent material from the first reactor is enough converted into product acid product by acid-producing bacteria group energy.
When the second reactor is single-stage anaerobic reactor, the second reactor can comprise the product acid phase mainly comprising acid formers and the methane phase stage mainly comprising methane-producing bacteria.In other words, when the second reactor is single-stage anaerobic reactor, it can be the traditional single-stage anaerobic reactor being positioned at the first reactor downstream.
In the second reactor as above, can control or not control pH.In either case, the pH of the second reactor may be about 6.5 to about 7.9, such as about 6.8 to about 7.4, such as about 7.1.If control the pH of the second reactor, pH can control about 6.8 to about 7.4, such as about 7.1.
In use, the second reactor may have the hydraulic detention time of more than 10 days.
Be understandable that, in order to ensure the technological process that optimal control is different, the first and second reactors may further include pH, redox-potential (ORP) and temperature regulator.The reading of reactor and adjustment by the mode artificially for the treatment of unit or method or automatically can be carried out.
First and second reactors for being furnished with the continuous stirred tank reactor (CSTR) of pH and temperature-control device, and can have very little forward gaseous tension inside described reactor.In general, the first reactor can be less than the second reactor, but can be also formed objects with the second reactor.Typically, when there being more than second reactor, the first reactor will be formed objects with the second reactor.The specific setting of reactor described above and treatment condition improves hydrolysis and acid production simultaneously, and this permission reactor assembly achieves and acid combined with classification behavior.
By way of example, described method can be run according to following principle and arrange.
A. the acid production inserting improvement before typical single-stage anaerobic reactor or methane-producing reactor dominates level.By in conjunction with initial setting and operational conditions, the acidogenic reactor of improvement allows cultivation and the gathering of microorganism species, and it has greater efficiency for the organic particle abatement under higher pH condition and VFA generation.
B. this two-stage anaerobic Operation system setting has pH, ORP and temperature regulator.The pH of first step reactor is 6.5-8.5 and temperature is 35-60 DEG C.The first step of this successive type sludge digestion system can run under the hydraulic detention time of some hours to 5 days.
C., after adaptation for some time, the microflora of the 1st stage reactor can expect and comprises the bacterium of about 99% and the Archimycetes of 1%.The acetic acid nutritional type methanogen (aceticlastic methanogens) comprising methane trichobacteria and sarcina methanica and the hydrogen nutritional type methanobacteria comprising methagen and methane germ will account for leading in first step reactor.
Be understandable that, method described before this can be used for any waste treatment plant needing to process organic waste, the waste sludge from waste water treatment plant that described organic waste such as organic content is high, secondary sludge, oily sludge, industrial sludge, sewage sludge, rubbish from cooking, oily waste or solid waste.Such as, method described here may be used for the waste water treatment plant of sludge treatment, such as sludge treatment factory or processing wastewater treatment plant.
Be understandable that, method described here by be especially applied to in conserve energy and recovered energy process the interested place of waste water and the restricted place of sludge treatment.Consider that the understanding of the energy-environmental concerns improves constantly, energy recovery is more and more important.The method of wastewater treatment of prior art has significant carbon vestige, and above-mentioned disclosed method is towards energy neutrality (energy neutral) and be finally the equipment development of energy positive treatment.Method and apparatus used herein can be used in sludge treatment factory and industrial effluent treatment plant, and can be used in new factory or join existing installation as improvement.In improvement project, the processing power that can also expand existing installation for the device running disclosed method of interpolation, and therefore avoid and build demand again along with increase in demand to existing treatment facility.
Embodiment
embodiment 1
Two-stage reactor is set.1st stage reactor runs in the basic conditions, and controls 8.0 by the artificial 1-5N NaOH that adds by pH, and then the 2nd stage reactor runs under the pH of 6.8-7.4.The hydraulic detention time (HRT) of two reactors maintains 5 days and 10 days separately.
In order to contrast the performance of two-stage system and traditional biphasic system and traditional simple system, also establish biphasic system and simple system.Biphasic system is run under be the 5.5 ± 0.3 and the 2nd phase pH being 6.8-7.4 at the 1st phase pH, and the hydraulic detention time of the 1st phase and the 2nd phase is 5 days and 25 days separately.Simple system is 6.8-7.4 and HRT 15 runs all over the world at pH.All said system are all run at 35 DEG C.
About the performance of mud solubilising, the VFA of simple system generates and consumes as simultaneous process, and the intermediate product of described process and resolvable chemical oxygen demand (SCOD) and VFA, as depicted in figs. 1 and 2, the two is relatively low level.Consider this point, contrast is mainly concentrated on the performance of two-stage system and biphasic system.
In two-stage system, the SCOD of significant quantity generates and assembles in the 1st stage reactor.The highest SCOD concentration reached is 12544mg/L, and the feed sludge wherein dissolved is 27.28%.By comparison, in biphasic system, the highest SCOD concentration reached in the 1st phase only has 6173mg/L, and the feed sludge being equivalent to dissolve is 14.14%.
The concentration of the VFA generated in the 1st stage reactor of two-stage system is listed in Fig. 2, wherein with acetic acid and propionic acid for main compound (be respectively 60% and 20%-30%).The maximum total VFA concentration generated in the 1st phase reactor of biphasic system is less than the half of the summation generated in the 1st stage reactor of two-stage system.According to these results, by original position alkali treatment method drastically increase hydrolysis and acid process be obvious.
It should be noted, after the adaptive phase, the methanogenesis in the 1st stage reactor of two-stage system is also active.The VFA generated in the 1st stage reactor by existing methanogen consumption to generate biogas.The pH of the mud be hydrolyzed in the 1st stage reactor is 6.8-7.5, and the mud of this hydrolysis can directly put into the 2nd stage reactor when not having further pH to adjust.2nd stage reactor is found the VFA that can respond actively the obvious high loading generated in the 1st stage reactor.This result shows that methanogen in the 2nd stage reactor rapid adjustment can decompose most SCOD and VFA (Fig. 2) to load impact.
Due to the hydrolysis that strengthens in the 1st stage reactor and acid process, compare with simple system with biphasic system, two-stage system achieves higher volatile suspended solid (VSS) abatement.It is 43.8% that the average VSS of two-stage system cuts down efficiency, and the average VSS abatement efficiency of biphasic system and simple system is respectively 32.3% and 33.2% (Fig. 3).The average volatile solid (VS) of each system is cut down efficiency and is: two-stage system is 60.7%, biphasic system be 30.2% and simple system be 31.6%.According to these results, it is obvious that two-stage system has significantly higher solid abatement ability than biphasic system and simple system.Further, the biogas generated in the 1st stage reactor of two-stage system has higher methane content (75.7%, 48.2% of contrast biphasic system the 1st phase, 65.1% of contrast simple system) compared to other two kinds of systems.
After the adaptive phase, the microflora in the 1st stage reactor can expect and comprises the bacterium of 99% and the Archimycetes of 1%.Most cells is all active.The acetic acid nutritional type methanobacteria comprising methane trichobacteria and sarcina methanica and the hydrogen nutritional type methanobacteria comprising methagen and methane germ will account for leading in the 1st stage reactor, without being bound by theory, this can explain that the VFA (mainly acetic acid) in the 1st stage reactor consumes and methane generation.
embodiment 2
In order to verify the ability of two-stage system under different HRT, the 1st stage reactor of two-stage system is also utilized to test this system with the HRT of 3 days.The result of this test shows that the 1st stage reactor also achieves the solubilising of feed sludge more than 21% under the HRT that this is shorter.
embodiment 3
1st grade addicted to warm & the 2nd grade addicted to warm CSTR system
Two-stage system is run with 2.5L/ days sewage sludge feed in laboratory continuous stirred tank reactor (CSTR) (CSTR) system.PH to be 8-8.5 (pH is generally near 8.0), HRT/SRT be 3 days and temperature be 35 DEG C at run the 1st stage reactor.HRT/SRT be 17 days, temperature be 35 DEG C at run the 2nd stage reactor.There is no the pH of control the 2nd stage reactor.In the single-stage CSTR system compared, HRT/SRT be 20 days, temperature is 35 DEG C, and runs reactor under the condition of not control pH.
Result shows, compared with simple system, two-stage system achieves significantly higher volatile solid (VS) abatement (Fig. 4), and to cut down efficiency with the average VS realized in simple system be compared with in the of 29.32 ± 3.55%, and two-stage system is 57.60 ± 3.68%.In simple system, not control pH, but pH is set in self the maintenance level between 6.8-6.95.The pH of the 2nd stage reactor of two-stage system does not also control, but pH value is initially increase, and then keeps stable at 7.82 places.
Because the VS abatement increased in two-stage system, the methane generation of two-stage system is higher than the methane generation (Fig. 5) realized in simple system.Compared with simple system, in whole experimental period, in two-stage system, generate the methane (amount (volume)) more than 31.54 ± 6.46%.
embodiment 4
The two-stage system described in embodiment 3 also runs with charging in 18L/ days under pilot scale.Similar to embodiment 3, the 1st stage reactor maintains that pH scope is 8.0-8.5 (being generally 8.0), temperature is 35 DEG C and HRT/SRT is 3 days.2nd stage reactor HRT/SRT be 17 days, temperature is 35 DEG C and pH runs under maintaining the scope of 6.8-7.2 with very little ACTIVE CONTROL.Result shows the VS abatement achieving 69.09 ± 5.21% in pilot test system.
embodiment 5
1st grade thermophilic & the 2nd grade is addicted to warm CSTR laboratory system
Above-mentioned two-stage system runs with 2.5L/d sewage sludge feed in the CSTR system of laboratory.1st stage reactor is that 8-8.5 (being generally pH 8.0), HRT/SRT are 3 days and temperature is run at being 55 DEG C at pH, and the 2nd stage reactor runs at HRT/SRT is 17 days and temperature is 35 DEG C.The pH of the 2nd stage reactor did not control during first 75 days of experiment, but starting to control built in pH 6.8-7.1 (being generally 7.1) for the 76th day then from experiment.For the object of contrast, be also provided with single-stage CSTR system.In simple system, reactor HRT/SRT be 20 days, temperature is 35 DEG C and do not run under control pH.
Result shows that in two-stage system, achieve significant VS cuts down (Fig. 6).When not having pH to control in the 2nd level system, the average VS abatement of two-stage system and simple system is respectively 66.79 ± 3.01% and 30.04 ± 3.65%.During first 75 days of experiment, the pH in the 2nd stage reactor is increased to about 7.85 and then keeps stable when not having pH to control.Within identical period, the pH self―sustaining in simple system is at 6.8-6.95.
From experiment the 76th day, the pH in the 2nd stage reactor maintain 7.1 and in the 2nd stage reactor VS abatement be further improved.Terminating to experiment for the 76th day from experiment, the average VS abatement of the 2nd stage reactor and single-stage reactor is respectively 78.56 ± 1.88% and 33.39 ± 4.17%.At whole experimental session, the average VS abatement in two-stage system and simple system is respectively 72.65 ± 6.53% and 31.65 ± 4.26%.
About methane generation, generate in two-stage system more methane (amount) (Fig. 7).Compared with simple system, experiment 0-75 days during, when the 2nd stage reactor not control pH time, generate the methane of more than 32.80 ± 6.75% (amount) in two-stage system; And from the 76th day, when the pH in the 2nd stage reactor controls 7.1 time, to generate the methane of more than 40.05 ± 4.81% (amount) in two-stage system.At whole 0-141 days experimental session, compared with simple system, in two-stage system, generate the methane of more than 36.73 ± 6.78% (amount).
embodiment 6
The microorganism related in single-stage and two-stage laboratory CSTR system
Collection is taken from charging, single-stage reactor, addicted to temperature the 1st stage reactor with addicted to the sample of temperature the 2nd stage reactor (embodiment 4) and from thermophilic charging, single-stage reactor, thermophilic 1st stage reactor and the sample addicted to temperature the 2nd stage reactor (embodiment 5), and is undertaken analyzing to study the microflora related in single-stage and two-stage system by reverse transcription polymerase chain reaction (RT-PCR).Fig. 8 shows the dominance (dominance) of bacterium and Archimycetes in sample.Found out that, in charging and each bio-reactor, all find the methane bacterial classification of methane germ, methagen, methane trichobacteria and sarcina methanica, pH has been controlled the cultivation of the methanogen addicted to gentleness in thermophilic 1st stage reactor not in suppression the 1st stage reactor 8.0.

Claims (24)

1., for the treatment of a method for organic waste, described method comprises the steps:
The incoming flow including organic waste is introduced in the first reactor;
Effluent is generated by described first reactor; With
Described effluent in described first reactor is provided to described second reactor,
Wherein, under described first reactor maintains the pH of about 6.5 to about 10.0.
2. method according to claim 1, wherein, under described first reactor maintains the pH of about 7.0 to about 9.0.
3. method according to claim 2, wherein, under described first reactor maintains the pH of about 7.5 to about 8.5.
4. method according to claim 3, wherein, described first reactor maintains pH about 8.0.
5. the method according to aforementioned arbitrary claim, wherein, described first reactor is mainly hydrolysis/acidogenic reactor.
6. the method according to aforementioned arbitrary claim, wherein, described second reactor is mainly methane-producing reactor or is single-stage anaerobic reactor.
7. the method according to aforementioned arbitrary claim, wherein, described first reactor and/or the second reactor run at about 35 temperature to about 60 DEG C.
8. method according to claim 7, wherein, described first reactor runs at about 50 temperature to about 60 DEG C.
9. the method according to claim 7 or 8, wherein, described second reactor runs at about 35 temperature to about 49 DEG C.
10. the method according to aforementioned arbitrary claim, wherein, described first reactor runs under the hydraulic detention time of about 2 hours to about 5 days.
11. methods according to claim 10, wherein, described first reactor runs under the hydraulic detention time of about 3 days to about 5 days.
12. methods according to aforementioned arbitrary claim, wherein, described second reactor runs under about 6.5 pH to about 7.9.
13. methods according to claim 12, wherein, described second reactor runs under about 6.8 pH to about 7.4.
14. methods according to claim 13, wherein, described second reactor runs under the pH of about 7.1.
15. methods according to aforementioned arbitrary claim, wherein, described organic waste comprise biodegradable solid.
16. methods according to claim 15, wherein, described organic waste are mud, rubbish from cooking, oily waste, solid waste and their arbitrary combination that organic content is high.
17. methods according to claim 16, wherein, described mud is waste sludge, secondary sludge, oily sludge, industrial sludge or sewage sludge or their arbitrary combination.
18. methods according to aforementioned arbitrary claim, wherein, described first and second reactors comprise pH, redox-potential (ORP) and temperature regulator further.
19. 1 kinds of waste reduction and disposal equipments, described waste reduction and disposal equipment uses the method according to claim 1-18.
20. waste reduction and disposal equipments according to claim 19, wherein, described waste reduction and disposal equipment is sewage treatment equipment.
21. 1 kinds of reactor assemblies for the treatment of biodegradable waste material, described reactor assembly comprises the first reactor and the second reactor, described second reactor is positioned at the downstream of described first reactor, and be connected with described first reactor fluid, wherein, described first and second reactor adapted use the method according to claim 1-18.
22. reactor assemblies according to claim 21, wherein, described first reactor is mainly hydrolysis/acidogenic reactor.
23. reactor assemblies according to claim 21 or 22, wherein, described second reactor is mainly methane-producing reactor or is single-stage anaerobic reactor.
24. according to the arbitrary described reactor assembly of claim 21-23, and wherein, described first and second reactors comprise pH, redox-potential (ORP) and temperature regulator further.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107245448A (en) * 2017-08-03 2017-10-13 盐城工学院 A kind of methane production equipment and its system

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11453608B2 (en) 2017-05-11 2022-09-27 Bl Technologies, Inc. Method for pre-conditioning sludge
BE1027989B1 (en) * 2020-01-15 2021-08-16 Organic Waste Systems Verkort O W S Process for the production of bioproducts from streams of organic material
CN114535246B (en) * 2022-02-21 2023-03-24 大连理工大学 Device and process for enhancing two-phase anaerobic digestion by using Fenton iron mud and iron-containing biochar
CN114906999B (en) * 2022-04-26 2023-04-21 北京化工大学 Method for improving sequencing batch anaerobic digestion performance of cow dung by gradient heating method

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020102673A1 (en) * 1998-08-07 2002-08-01 The Regents Of The University Of California Biogasification of solid waste with an anaerobic-phased solids-digester system
CN2719837Y (en) * 2004-09-03 2005-08-24 戴文祥 Anaerobic bioreactor
CN1761624A (en) * 2003-03-19 2006-04-19 卡罗洛工程师公司 Two phase anaerobic organic matter treatment and system
CN102115344A (en) * 2010-12-03 2011-07-06 清华大学 Two-phase integral anaerobic digestion process and equipment for treating biomass solid wastes
CN102241464A (en) * 2011-06-01 2011-11-16 北京中持绿色能源环境技术有限公司 Urban sludge treating method and equipment
CN102482686A (en) * 2009-08-03 2012-05-30 Dge京特博士工程有限公司 Method for producing biogas or biogas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020102673A1 (en) * 1998-08-07 2002-08-01 The Regents Of The University Of California Biogasification of solid waste with an anaerobic-phased solids-digester system
CN1761624A (en) * 2003-03-19 2006-04-19 卡罗洛工程师公司 Two phase anaerobic organic matter treatment and system
CN2719837Y (en) * 2004-09-03 2005-08-24 戴文祥 Anaerobic bioreactor
CN102482686A (en) * 2009-08-03 2012-05-30 Dge京特博士工程有限公司 Method for producing biogas or biogas
CN102115344A (en) * 2010-12-03 2011-07-06 清华大学 Two-phase integral anaerobic digestion process and equipment for treating biomass solid wastes
CN102241464A (en) * 2011-06-01 2011-11-16 北京中持绿色能源环境技术有限公司 Urban sludge treating method and equipment

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107245448A (en) * 2017-08-03 2017-10-13 盐城工学院 A kind of methane production equipment and its system

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