CN103347824B - anaerobic treatment method and device - Google Patents

anaerobic treatment method and device Download PDF

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Publication number
CN103347824B
CN103347824B CN201180059643.8A CN201180059643A CN103347824B CN 103347824 B CN103347824 B CN 103347824B CN 201180059643 A CN201180059643 A CN 201180059643A CN 103347824 B CN103347824 B CN 103347824B
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sludge
flocculation
anaerobic digestion
mud
treatment
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CN103347824A (en
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片冈直明
萩野隆生
西胁正人
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Swing Corp
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Swing Corp
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Priority to JP2010-276156 priority
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Priority to PCT/JP2011/078531 priority patent/WO2012077778A1/en
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00Treatment of sludge; Devices therefor
    • C02F11/02Biological treatment
    • C02F11/04Anaerobic treatment; Production of methane by such processes
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00Treatment of sludge; Devices therefor
    • C02F11/12Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/14Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/30Fuel from waste, e.g. synthetic alcohol or diesel

Abstract

The invention provides a kind of anaerobic treatment method and the device that realize cost degradation, it makes anaerobic digestion equipment miniaturization, and the generation of the precipitate such as phosphorus, siloxanes is minimized, by the sludge stabilization that produces in sewage treatment equipment etc. and effectively anaerobic digestion, and effectively can reclaim biogas (especially methane gas), and can effectively digested sludge be dewatered.Specifically, the present invention relates to a kind of anaerobic treatment method and the device for implementing above-mentioned treatment process, described method comprises: the flocculation sludge solid-liquid separation prepared adding flocculation agent in mud is the sludge condensation thing of sludge concentration 4 ~ 12% and the pretreatment process of parting liquid; This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion operation of biogas; By the anaerobic digestion mud prepared in this anaerobic digestion operation and flocculation agent and be selected from described parting liquid and water at least any one mix, prepare the operation of digested sludge throw out; And to the operation that the digested sludge enriched material this digested sludge throw out solid-liquid separation obtained dewaters.

Description

Anaerobic treatment method and device
Technical field
The present invention relates to anaerobic treatment method and the device of mud.
Background technology
Compared with aerobism process, the mud generation of the anaerobic digestion process of mud is few, pathogenic micro-organism, parasitic ovum can promptly be killed and stabilization, do not need the supply of oxygen, power consumption is few, can obtain with methane gas is the biogas of principal constituent, is therefore since ancient times just as the technology of energy-conservation treatment process application.On the other hand, anaerobic digestion groove equipment must be Large Copacity, and in the process of digested sludge, chemical is costly, and mud is difficult dehydration property, and dewatered sludge water ratio is not easy to reduce, and is therefore also the technology of more problems.
Therefore, as existing method for sludge treatment, not that sludge anaerobic is digested, but or the rear landfill of dehydration, or after dehydration, the example of burning disposal is also a lot.Such as, as the anaerobism process of existing mud, the process shown in the feel flow draw of block shown in Fig. 6 can be listed.This flow process is below described.
Mud 1 is transported in storage facility 2, then, mud 1 is transported in equipment for separating liquid from solid 6, solid-liquid separation is sludge condensation thing 7 and parting liquid 8, sludge condensation thing 7 is transported in anaerobic digestion device 9, by the anaerobic digestion of mud, generate biogas 10 and anaerobic digestion mud 11, biogas 10 is transported in biological gas tank 101, then, biogas 10 is transported to gas and utilizes equipment 102(such as, gas turbine, biogas boiler, gaslight, drying machine thermal source etc.) or residual gas combustion unit 103 in.Anaerobic digestion mud 11 is transported in digested sludge throw out preparation facilities 12, while isolating parting liquid 14, preparation digested sludge throw out 15, digested sludge throw out 15 is transported in dewatering unit 16, prepares dewatered cake 18 while isolating parting liquid 17.Parting liquid 8, parting liquid 14 and parting liquid 17 are transported in sewage treatment equipment 104 etc.In digested sludge throw out preparation facilities 12, mostly add flocculation agent.
On the other hand, the treatment process of a kind of fecaluria, food waste, mud is proposed in patent documentation 1, by this treatment process, by the mud such as the mud of organic wastewater treatment facility, purification tank mud, fecaluria, food waste energy-efficient treatment containing plant and animal residue, simultaneously, by the non-hygiene screening reject wholesomeness composting in fecaluria, purification tank mud or Solid fuel, the treating method comprises following operation: (a) will mix the pretreatment process of the fecaluria solid-liquid separation of mud; B the solid substance be separated in treatment process does not dewater and the anaerobic digestion operation of direct anaerobic digestion by (); C () is by the anaerobic digestion operation of the food waste anaerobic digestion containing plant and animal residue and solid substance; D the dehydration of anaerobic digestion operation effluent liquid is separated into the dehydration procedure of solid substance and Separation of Water by (); E () is by the Separation of Water of pretreatment process, from the Separation of Water biological oxidative of dehydration procedure, the biologic treatment process of denitrogenation.
A kind of method for sludge treatment and system thereof is proposed in patent documentation 2, by this treatment process, by the primary sludge that produced by wastewater treatment and excess sludge two kinds of mud concentration in a system, concentrated by follow-up dehydration procedure simultaneously, be maintained until the suitableeest sludge concentration, thus play the concentrated of these wastewater sludges to greatest extent, the total efficiency of dewatering process, the treating method comprises: the excess sludge that the primary sludge produce the initial settling tank by sewage treatment equipment and final tank produce mixes, storage, flocculation agent is added in this mixing sludge, carry out a flocculation treatment, then, the mixing sludge concentration of a flocculation treatment will be completed, its sludge concentration is made to reach 6 ~ 8%, then, flocculation agent is added in mixing sludge after concentration, carry out secondary flocculation treatment, further processed is implemented to the mixing sludge having carried out secondary flocculation treatment.
In addition, in patent documentation 3, propose a kind of transport capacity improving equipment for separating liquid from solid, and increase the slit type thickner of extruding squeezing effect.
Prior art document
Patent documentation
Patent documentation 1: Japanese Unexamined Patent Publication 10-216785 publication
Patent documentation 2: Japanese Unexamined Patent Publication 2007-264758 publication
Patent documentation 3: Japanese Unexamined Patent Publication 2003-211293 publication
Summary of the invention
the problem that invention will solve
In the anaerobic digestion process of the mud produced in sewage treatment equipment etc., usually due to HRT(hydraulic detention time: Hydraulicretentiontime) be 20 ~ 30 days, therefore, need jumbo anaerobic digestion groove to be maximum problem.Such as, at mud TS(TotalSolids) concentration 3wt%, treatment capacity 100m 3in the sludge treatment in/sky, need to design usual 2000 ~ 3000m 3large-scale anaerobic digestion groove.In addition, in digested sludge process, the chemical expense had needed for sludge flocculation, processed increases, and mud becomes difficult dehydration property, and moisture percentage in sewage sludge is also not easy the problem reduced.This is because in the anaerobic digestion of mud, because protein is decomposed, generate ammonia-state nitrogen, M basicity (reaching the acid consumption of pH4.8) is also increased to about 3,000mgCaCO 3/ more than L, deviate from the slightly acidic region of the optimal pH condition being considered to sludge flocculation.In addition, Problems existing is, due to sludge digestion, the thick seston (fibre composition) in mud is decomposed together, and therefore, the thick seston content of dehydration when going far towards sludge dewatering declines, and dewatered cake water ratio increases.In addition, also there is the problem that the precipitate such as phosphorus, calcium occurs in anaerobic digestion groove, pipe arrangement etc.In addition, the silicon contained in draining is normally derived from the form of the siloxanes of the silicon compounds such as the silicone oil contained in shampoo, hair conditioner, makeup etc.Siloxanes refers to that main framing is the organic compound with silicon-oxygen key Si-O-, side chain having alkyl.As siloxanes, include, for example out Siliciumatom is 2 ~ 6, alkyl is methyl etc. wire or annular siloxane.Because the solubleness of siloxanes in water is low, during by sewage sludge anaerobic digestion, distributing moves in biogas, therefore, when gas-to electricity biogas, in the generating sets such as gas engine, peripherals, form dirt and separate out, there will be a known manyly cause decrease of power generation, maintenance of the equipment produces dysgenic example, its Prevent countermeasures becomes important.
The present invention makes in view of the above problems, its objective is and a kind of anaerobic treatment method and the device that realize cost degradation are provided, it makes anaerobic digestion equipment miniaturization, and the generation of the precipitate comprising phosphorus, calcium, siloxanes (having the silicon compound of siloxane bond) etc. is reduced, by the sludge stabilization that produces in sewage treatment equipment etc. and effectively anaerobic digestion, and effectively can reclaim biogas (especially methane gas), and can effectively digested sludge be dewatered.
for the scheme of dealing with problems
According to the present invention, provide following anaerobic treatment method and anaerobism treatment unit.
1) anaerobic treatment method, it comprises: the flocculation sludge solid-liquid separation prepared adding flocculation agent in mud is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the pretreatment process of parting liquid; This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion operation of biogas; By the anaerobic digestion mud prepared in this anaerobic digestion operation and flocculation agent and be selected from described parting liquid and water at least any one mix, prepare the operation of digested sludge throw out; And to the operation that the digested sludge enriched material this digested sludge throw out solid-liquid separation obtained dewaters.
2) an anaerobism treatment unit, it comprises: in mud, add flocculation agent and prepare the flocculation tank of flocculation sludge; Be sludge condensation thing and the parting liquid of sludge concentration 4 ~ 12wt% by this flocculation sludge solid-liquid separation, prepare the pretreating sludge concentrating unit of sludge condensation thing; This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion device of biogas; By the anaerobic digestion mud prepared in this anaerobic digestion device and flocculation agent and be selected from described parting liquid and water at least any one mixes and prepares the digested sludge flocculation plant of digested sludge throw out; And to the dewatering unit that the digested sludge enriched material this digested sludge throw out solid-liquid separation obtained dewaters.
In treatment process of the present invention, solid-liquid separation in pretreatment process and the sludge condensation thing prepared contain 4 ~ 12wt%, be the mud of the high densitys of existing methodical more than 1.5 ~ 2 times.In order to by this sludge condensation thing anaerobic digestion process, anaerobic digestion mud of the present invention has the M basicity higher than now methodical anaerobic digestion mud and ammonia density.Therefore, when wanting directly add flocculation agent and obtain throw out (floc) that can dewater in anaerobic digestion mud, a large amount of flocculation agents is needed.Therefore, in the present invention, in order to obtain the digested sludge throw out that can dewater, by the parting liquid obtained in pretreatment process or water at least any one mixes with anaerobic digestion mud, anaerobic digestion mud is diluted, react by the sludge flocculation of the flocculation agent of anaerobic digestion mud and interpolation and generate digested sludge throw out reposefully, thus realizing the reduction of flocculent agent injection rate.In addition, in pretreatment process of the present invention, in order to add flocculation agent, the flocculation sludge prepared is separated into sludge condensation thing and parting liquid, and the water-soluble or hydrophilic useful resources such as phosphorus contains in parting liquid, effectively can reclaim useful resources.In addition, because the pretreatment process that can reclaim useful resources carried out before anaerobic digestion operation, be transported to the reductions such as the phosphorus in the sludge condensation thing of anaerobic digestion operation, siloxanes, and due to sludge concentration be high density, therefore can reduce the generation of precipitate containing phosphorus, siloxanes etc. in anaerobic digestion groove.
In the present invention, unless otherwise prescribed, " % " refers to " quality % ".Anaerobism treatment unit of the present invention can have the unit for carrying mud between above-mentioned each intrinsic device aptly, such as pipe arrangement, pump, valve etc.
the effect of invention
According to the present invention, by the anaerobic digestion of the mud in waste water processing station etc., by organic substance decomposing, and effectively can reclaim biogas (especially methane gas), thus, energy recovery efficiency can be improved significantly.Especially, for in existing treatment process must Large Copacity anaerobic digestion equipment, for the chemical of digested sludge process, costly and mud is difficult dehydration property, dewatered sludge water ratio is difficult to the technical task that reduces, in the present invention, in the concentrating unit of low operating cost, mud height can be concentrated, and can significantly cut down anaerobic digestion capacity, in addition, the dehydration operation that can also carry out the anaerobic digestion mud of difficult dehydration property improves, thus can realize can effectively by the anaerobic digestion system of the low cost of digested sludge processed.In addition, the introduction volume of the phosphorus in anaerobic digestion groove, calcium, siloxanes etc. can be reduced to roughly half in the past by the present invention, and then the generation of the precipitate containing phosphorus, calcium, siloxanes etc. in anaerobic digestion groove can be reduced, contribute to the maintenance of anaerobic digestion groove and pipe arrangement etc., the reduction of overhead charges, effectively can reclaim the useful resources such as phosphorus simultaneously.
Accompanying drawing explanation
Figure 1 shows that the explanatory view of the formation of the treatment unit of embodiments of the present invention.
Figure 2 shows that the explanatory view of the formation of the treatment unit of embodiments of the present invention.
Figure 3 shows that the explanatory view of the formation of the treatment unit of embodiments of the present invention.
Figure 4 shows that the explanatory view of the formation of the treatment unit of embodiments of the present invention.
Figure 5 shows that the explanatory view of the formation of the treatment unit of embodiments of the present invention.
Figure 6 shows that the explanatory view of the formation of existing treatment unit.
Embodiment
Suitably be described in more detail the present invention with reference to accompanying drawing below.
Anaerobic treatment method of the present invention comprises: the flocculation sludge solid-liquid separation prepared adding flocculation agent in mud is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the pretreatment process of parting liquid; This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion operation of biogas; By the anaerobic digestion mud prepared in this anaerobic digestion operation and flocculation agent and be selected from described parting liquid and water at least any one mix, prepare the operation of digested sludge throw out; And to the operation that the digested sludge enriched material this digested sludge throw out solid-liquid separation obtained dewaters.
In the present invention, " mud " mud of referring to disposing of sewage, discharging in the operation of the organic system material such as fecaluria, food waste.
As the mud processed in the present invention, be preferably selected from least one in the primary sludge produced by the initial settling tank of sewage treatment equipment and the excess sludge produced by final tank, be more preferably the mixing sludge from both.This mud is preferably stored in storagetank, carries out gravity concentration.
Flocculation agent is added, preparation flocculation sludge in the mud of being discharged by storagetank.The addition of flocculation agent relative to the SS(SuspendedSolids of mud, suspended particle) be preferably 0.2 ~ 1.0wt%, be more preferably 0.3 ~ 0.6wt%.
As flocculation agent, conventional flocculation agent can be used without particular limitation.Such as, bodied ferric sulfate or the inorganic based flocculating agent such as PAC, Tai-Ace S 150 and organic polymer coargulator (hereinafter also referred to polymeric flocculant) etc. can be listed, can be used alone or in combination separately, preferably at least containing polymeric flocculant.As polymeric flocculant, positively charged ion system, negatively charged ion system, both sexes system etc. can be listed, such as, amidine based flocculating agent, acrylamide based flocculating agent, acrylic acid series flocculation agent etc. can be listed.
According to operation, anaerobic treatment method of the present invention is described below.
< pretreatment process >
This pretreatment process is the flocculation sludge solid-liquid separation prepared adding flocculation agent in mud is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the sludge condensation operation of parting liquid.In existing treatment process, by sludge condensation, therefore, be concentrated into 3 ~ 4wt% owing to adding polymeric flocculant, the sludge concentration of about 4 ~ 5wt% is the limit at the most.In the present invention, the high concentration reaching sludge concentration 4 ~ 12wt% is possible.On the other hand, phosphorus, calcium, siloxanes etc. are contained in parting liquid.
< anaerobic digestion operation >
Then, above-mentioned sludge condensation thing is transported in anaerobic digestion operation, the biogas produced while being recovered in anaerobic digestion.Preferably, the digestion of sludge condensation thing, at 30 ~ 60 DEG C, is preferably carried out in the mesophilic digestion region of 30 ~ 40 DEG C or the thermophilic digestion region of 50 ~ 60 DEG C.Applicable pH during anaerobic digestion is pH6 ~ 8.5, most preferably is pH6.5 ~ 8.0.
During by the following organic waste liquid containing many lubricant components or waste mixture slaking, during temperature height, the dispersiveness of neutral fat, higher fatty acid increases, the therefore thermophilic digestion method of prioritizing selection 50 ~ 60 DEG C.On the other hand, the ammonia generated in the anaerobic digestion of mud easily dissociates in high pH and high-temperature zone, therefore, should be noted that this point being easily subject to ammonia and hindering in thermophilic digestion.As NH in Digestive system 4 +-N concentration is 3, more than 500mg/L in mesophilic digestion, and when being 2, more than 000mg/L in thermophilic digestion, methane generation reaction is hindered.Water yield variation when these operational conditions consider sludge concentration, sludge character, the anaerobic digestion of thickened sludge, target processing water quality are determined.
Anaerobic digestion operation more preferably comprises: at treatment temp 30 ~ 60 DEG C, HRT(hydraulic detention time: Hydraulicretentiontime) leading portion digestion operation that is solubilized and acid-fermentation process is carried out to described sludge condensation thing under the condition of 1 ~ 3 day, and methane fermentation process is carried out in the digested sludge processed in this leading portion digestion operation, prepare the methane fermentation operation of anaerobic digestion mud.
This leading portion digestion operation has the function of anaerobism process of the methane fermentation operation promoting back segment, for reducing methane fermentation operation HRT, make the recovery effectuation of biogas and stabilization, stably maintain high thick seston containing ratio, reduce fermentation broth viscosity.In addition, can digest at leading portion the adjustment carrying out SS concentration in operation.
Methane fermentation operation preferably to be carried out under the condition of HRT12 ~ 20 day treatment temp 30 ~ 60 DEG C, preferably prepares anaerobic digestion mud in the mode that to make relative to the thick seston containing ratio of SS be 3 ~ 20%.The thick seston of above-mentioned thick seston containing ratio refers to fibrous material, the particulate matters etc. such as Mierocrystalline cellulose.This HRT is more preferably 12 ~ 15 days, and thick seston containing ratio is more preferably 5 ~ 18%.By thick seston containing ratio is set as above-mentioned scope, can improve the dehydration property of digested sludge enriched material, the water ratio realizing dewatered cake reduces.
In addition, in anaerobic digestion operation of the present invention, can by from outside, the organic waste liquid that its exterior of the waste water processing station of namely implementing in the present invention is transported or waste process together with mud.From the organic waste liquid of outside or waste at least containing the organic compound of discharging from the equipment of factory, sewage work etc., mud, draft class etc. can be contained.Can be input to from the organic waste liquid of outside or waste in any one of pretreatment process, leading portion digestion operation and methane fermentation operation.From the organic waste liquid of outside or waste together with mud during anaerobic digestion, preferably by the slurry TS(TotalSolids of this organic waste liquid or waste) concentration is adjusted to 1 ~ 15%(more preferably 3 ~ 10%), add under the mixing condition reaching relative to the TS of sludge condensation thing the slurry TS ratio being less than 120% (more preferably 5 ~ 100%).Wherein, slurry TS concentration refers to the TS concentration in slurry, and slurry TS is than the TS ratio referring to the input material contained in slurry.Slurry TS concentration considers that the kind, concentration, state, incoming frequency etc. of organic waste liquid or waste are determined.In addition, when being incorporated into anaerobic digestion operation after carrying out physical property, chemical, biological disaggregating treatment as required from the organic waste liquid of outside input or waste, digestion reaction stabilization can be made, because of but preferably.As an example of processing mode, wet type fragmentation, dry type pulverizing, thermal treatment, high temperature high pressure process, acid or alkaline purification, biosoluble or acid-fermentation process etc. can be listed aptly.
< digested sludge throw out preparation section >
Then, by the anaerobic digestion mud prepared in anaerobic digestion operation and flocculation agent and be selected from the parting liquid of pretreatment process and water at least any one mix, prepare digested sludge throw out.
As the flocculation agent added in anaerobic digestion mud, polymeric flocculant etc. are preferred.In addition, the inorganic system flocculant aid such as bodied ferric sulfate or PAC and polymeric flocculant combinationally use the clarity that sometimes also can be effective to improve parting liquid.As polymeric flocculant, less expensive cationic polymers based flocculating agent such as acrylic ester, methacrylate ester, both sexes based flocculating agent etc. that cationic degree is higher than anion degree can be used, but also can use the amidine based flocculating agent of high price.As acrylic ester, molecular weight 300 ~ 6,000,000 is owing to obtaining the high digested sludge throw out of settlement separate property but preferred.
The addition of flocculation agent changes according to the proterties of anaerobic digestion mud, and in order to improve the settlement separate property of digested sludge throw out, preferably the east floes of throw out reaches the addition of several millimeter.Specifically, to be the scope of 1.0 ~ 2.5% relative to the SS in anaerobic digestion mud, preferably the scope of 1.5 ~ 2.0% adds flocculation agent, makes the east floes of throw out be the scope of 5 ~ 20mm, is preferably the scope of 10 ~ 20mm.
The parting liquid used in digested sludge throw out preparation section or water (also referred to as " dilution water ") have the function of dilution anaerobic digestion mud.By utilizing the dilution of the thickened sludge of parting liquid or water, the specific conductivity of mud is adjusted to below 1200mS/m, preferred below 750mS/m, the M basicity of mud is adjusted to below 4000mg/l, preferred below 2500mg/l, is adjusted to more than 35 DEG C by the temperature of mud, preferably 50 ~ 75 DEG C.The temperature of the mud of dilution can be adjusted by the parting liquid or water adding said temperature scope, or can at interpolation post-heating.As long as meet, dilution water, except the parting liquid obtained in pretreatment process, common tap water etc., is dissolved into that the concentration of grading is less to be waited condition of water quality (electric conductivity is below 500mS/m, M basicity be below 1500mg/L, SS is below 1500mg/L, COD crfor below 15000mg/L) water, any process water in processing plant can be used.In addition, the biological treatment of water such as active sludge treatment water, biological deodorizing device waste liquid can also be used.
Gained digested sludge throw out is carried out solid-liquid separation, preparation digested sludge enriched material and parting liquid.The concentration rate of digested sludge enriched material is preferably about 2.5 ~ 8 times.Herein, concentration rate refers to the value obtained divided by the volume of digested sludge enriched material by the volume of digested sludge throw out.
In the digested sludge enriched material that solid-liquid separation is crossed, again add flocculation agent and dilution water as required, prepare reconcentration flocculation sludge.The flocculation agent now used and dilution water can be the flocculation agent and dilution water that use in digested sludge throw out preparation section.When reconcentration flocculation sludge has a sufficient dehydration property (the TS concentration of concentrated flocculation sludge is the scope of 4 ~ 15wt%, is preferably 6 ~ 10wt%), be transported in dehydration procedure as final digested sludge throw out.But, when this reconcentration flocculation sludge does not have a sufficient dehydration property, or originally design is considered as if desired (when the TS concentration of concentrated flocculation sludge is lower than 4wt%) etc., such as, can repeats above-mentioned flocculation agent and reinject with follow-up solid-liquid separation or only repeat solid-liquid separation.The flocculation agent identical with the flocculation agent used in digested sludge throw out preparation section can be used for the reflooded flocculation agent of flocculation agent, also can use different flocculation agents.
Final digested sludge throw out even if preferably there is the shearing force stood in the dehydration procedure of back segment after the throw out of intensity of the also residual a little degree of its granular throw out shape.Flocculation agent for obtaining this digested sludge throw out is not particularly limited, preferably polymeric flocculant.As polymeric flocculant, the polymeric flocculant for above-mentioned flocculation sludge preparation section can be listed, can be identical with the flocculation agent of pretreatment process, also can be different.
< dehydration procedure >
Then, dewatered by digested sludge throw out, solid-liquid separation is dewatered cake and parting liquid.In the present invention, the concentration rate of dewatered cake is preferably about 4 ~ 10 times.Herein, concentration rate refers to the value obtained divided by the volume of dewatered cake by the volume of digested sludge throw out.The parting liquid be separated in dewatered cake preparation section, owing to having little SS concentration, M basicity and specific conductivity, is therefore suitable as the dilution water used in the operation of preparation digested sludge throw out.Dewatered cake, therefore can renewable resources owing to being hyposaline and low-water-content, is also suitable for the secondary processing etc. such as composting, carbonization, turning sludge into fuel.
< phosphorus and siloxanes reclaim >
Containing phosphorus, calcium, siloxanes etc. in the parting liquid obtained in pretreatment process.In the present invention, can be transported to containing all or part of of their parting liquid and to reclaim or except in the operation of dephosphorization, calcium, siloxanes etc.The recovery of phosphorus can apply the contact dephosphorization method using hydroxyapatite, the MAP method etc. using ammonium magnesium phosphate.
In MAP method, can following methods be listed: the crystal seed being pre-charged with MAP in reactive tank such as upward flow groove, in addition, as required, in parting liquid, add the medicament being used for supplementing not enough MAP composition, such as MgCl 2, Mg (OH) 2deng, further, as required, the pH of parting liquid is adjusted to 7.8 ~ 8.5, is passed in reactive tank by parting liquid according to upward flow, the particle diameter of MAP is increased, this being had the MAP increasing particle diameter suitably discharges from reactive tank, is separated, reclaims.The fine MAP generated in reactive tank reclaims from groove top, turns back in reactive tank.
Parting liquid can carry out as gas and even spray form absorption or the method for directly adsorbing in a liquid state by utilizing the sorbent materials such as gac, silica gel, zeolite, polymkeric substance (such as styrene diethylene benzene copoly mer etc.) by the recovery of siloxanes.In addition, as required, nitrogen is suitably heated, pass through in the sorbent material being adsorbed with siloxanes, thus siloxanes can be departed from, reclaim.For following biogas, sorbent material similar to the above can be used to process siloxanes, use the same method siloxanes disengaging, reclaim.
The present invention is as mentioned above owing to having the operation that solid-liquid separation is parting liquid and sludge condensation thing, therefore compared with the pastly the import volume in anaerobic digestion device such as phosphorus, siloxanes is reduced, and then the generation comprising the precipitate of phosphorus, siloxanes etc. reduced in the apparatus, have and contribute to reducing the maintenance of this device or pipe arrangement etc., the effect of overhead charges.
< anaerobism treatment unit >
Anaerobism treatment unit of the present invention comprises: in mud, add flocculation agent and prepare the flocculation tank of flocculation sludge; Solid-liquid separation is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the pretreating sludge concentrating unit of parting liquid; This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion device of biogas; By the anaerobic digestion mud prepared in this anaerobic digestion device and flocculation agent and be selected from described parting liquid and water at least any one mixes and prepares the digested sludge flocculation plant of digested sludge throw out; And to the device that the digested sludge enriched material this digested sludge throw out solid-liquid separation obtained dewaters.
Flocculation tank can be normally used flocculation tank.
Pretreating sludge concentrating unit can be the solid-liquid separation tank of sludge condensation thing and parting liquid by flocculation sludge solid-liquid separation.Solid-liquid separation tank is not particularly limited, the simple groove of application of weight method of enrichment, the separating centrifuge of application centrifugal concentrating method, the separating machine of application flotation method of enrichment, the separating machine, slit type thickner etc. of use screen cloth can be listed.Wherein, slit type thickner is preferred, such as, the physical construction as recorded in above-mentioned Japanese Unexamined Patent Publication 2003-211293 publication (patent documentation 3) can be listed: caught by handled thing slit plate (slitplate), on the slit plate being formed with multiple slit, the outstanding multiple plectanes of side face are made to utilize axial rotary handled thing discharge direction eccentric rotary, handled thing is transferred to discharge side on slit plate, in this process, liquid component from slit and gap between plectane fall and be filtered, the separated trapping of solids component in handled thing, to arrange on above-mentioned slit plate further with the upper surface of slit plate close to and rotate to the discharge direction at handled thing, trapping thing on slit plate is squeezed, the belt conveyor of de-liquid.During application slit type thickner, can stablize by cheap running cost and reliably realize the high concentration of 4 ~ 12wt%.
Anaerobic digestion device at least comprises anaerobic digestion groove.Anaerobic digestion groove is not particularly limited, the complete mixed type digestive shelf of advantageous applications.Anaerobic digestion groove is in order to realize the homogenization of the homogenizing of liquid in groove, temperature distribution, prevent the generation of scum silica frost simultaneously, stirring is required, in the present invention, mechanical stirring mode is the most effective, but according to facility environment, treatment condition, attached pump alr mode, gas stirring mode are also effective.In addition, as long as possess the watertight of these important documents and the digestive shelf of airtight construction, can be any one of skeleton construction or steel plate, also can transform according to treatment condition and upgrade existing anaerobic digestion groove and apply.In addition, anaerobic digestion device preferably includes: the solubilized and acid-fermentation treatment trough carry out solubilized and acid-fermentation process to sludge condensation thing and the methane fermentation groove of digested sludge methane fermentation process that will process in the cell.Anaerobic digestion device preferably includes: the external biogas storage facility storing organic waste liquid from outside or waste; And the biogas of discharging from this external biogas storage facility imported to be selected from by the mechanism at least any one device in described storage facility, the device carrying out solubilized and acid-fermentation process and methane fermentation device and pipe arrangement.
Digested sludge flocculation plant comprises the extraction unit etc. of digested sludge flocculation tank, the unit introducing the mud of suitably dilution, flocculation agent adding device, agitating unit, heating unit, flocculation sludge.In addition, mixing device in the pipe arrangement for diluting can be had.
Anaerobism treatment unit of the present invention preferably has the device being prepared digested sludge enriched material by digested sludge throw out.
The device of preparation digested sludge enriched material preferably have by flocculation agent prepare flocculation sludge sludge flocculation treatment unit, prepared by this flocculation sludge solid-liquid separation concentrated flocculation sludge flocculation sludge separation concentration device, in this concentrated flocculation sludge, add flocculation agent and prepare the device of reconcentration mud.
Flocculation sludge separation concentration device is the device of concentrated flocculation sludge and parting liquid by flocculation sludge solid-liquid separation.Flocculation sludge separation concentration device is not particularly limited, the simple groove, the separating centrifuge of application centrifugal concentrating method, the separating machine of application flotation method of enrichment, the separating machine etc. of use screen cloth that use application of weight method of enrichment can be listed.Wherein, preferably there is the equipment for separating liquid from solid of screen cloth, such as, can list by the multiple screen cloth according to arrangement parallel at certain interval and multiple disks of rotating between this adjacent screen cloth, the flocculation sludge physical property in the gap between this adjacent screen cloth is got rid of, simultaneously the separable equipment for separating liquid from solid for concentrating flocculation sludge and Separation of Water.Wherein, the wavelength width of a slit principle of screen cloth is less than the east floes of digested sludge throw out, is preferably 0.1 ~ 2.5mm.
Reconcentration flocculation sludge preparation facilities is suitable for having the extraction unit etc. that concentrated flocculation sludge imports unit, flocculation agent adding device, agitating unit, reconcentration flocculation sludge.
The device dewatered by digested sludge enriched material is not particularly limited, usually the device identical with in flocculation sludge separation concentration device principle can be used, but compared with flocculation sludge separation concentration device, general higher for separating of the stress on the digested sludge throw out of dewatered cake, known unit can be adopted.Dewatered cake preparation facilities is preferably by giving the means of stress and form through the filters of parting liquid, maintenance digested sludge throw out in reconcentration flocculation sludge.As the means of giving stress on digested sludge throw out, pressure, centrifugal etc. can be listed.As filters, the screen cloth etc. that opening diameter is 0.1 ~ 2.5mm can be listed.
Then an example of the present invention is further illustrated with reference to accompanying drawing.
Figure 1 shows that the feel flow draw of block of the first embodiment of the present invention, is the explanatory view of the formation representing anaerobism treatment unit.
Mud 1 is transported in storage facility 2.Then, mud 1 is discharged from storage facility 2, via pipe arrangement, is transported in flocculation tank 3.In flocculation tank 3, flocculation agent 4 is added in mud 1, preparation flocculation sludge 5.Flocculation sludge 5 is transported in pretreating sludge thickener 6, and solid-liquid separation is sludge condensation thing 7 and the parting liquid 8 of sludge concentration 4 ~ 12%.Sludge condensation thing 7 is transported in anaerobic digestion device 9, by the anaerobic digestion of mud, generates biogas 10 and anaerobic digestion mud 11.Biogas 10 is transported in biological gas tank 101, and then, biogas 10 is transported to gas and utilizes equipment 102(such as gas turbine, biogas boiler, gaslight, drying machine thermal source etc.) or residual gas combustion unit 103 in.Anaerobic digestion mud 11 is transported in digested sludge flocculation plant 12.A part for the parting liquid 8 formed in pretreating sludge thickener 6 is incorporated in digested sludge flocculation plant 12.In digested sludge flocculation plant 12, parting liquid 8 and flocculation agent 13 are added in anaerobic digestion mud 11, form digested sludge throw out 15 and parting liquid 14.Digested sludge throw out 15 from digested sludge flocculation plant 12 is transported in dewatering unit 16, while isolating parting liquid 17, and preparation dewatered cake 18.The part of parting liquid 8, parting liquid 14 and parting liquid 17 are transported in sewage treatment equipments such as phosphorus recovery 104 etc.Wherein, before biological gas tank, siloxanes removing or retrieving arrangement can be set.
Then, Figure 2 shows that the feel flow draw of block of the second embodiment of the present invention, is the explanatory view of the formation representing anaerobism treatment unit.Solubilized and acid-fermentation process is carried out in the leading portion of anaerobic digestion.
In a flow diagram in figure 1, the sludge condensation thing 7 be separated in pretreating sludge thickener 6 was transported in solubilized and acid-fermentation treatment unit 9a before being transported in anaerobic digestion device 8, generated and implemented solubilized and digested sludge 7a that is acid-fermentation process.Digested sludge 7a is transported in anaerobic digestion device 9, processes according to the flow process of Fig. 1 later.
Then, Figure 3 shows that the feel flow draw of block of the 3rd embodiment of the present invention, is the explanatory view of the formation representing anaerobism treatment unit, and anaerobic digestion mud utilizes the sludge flocculation process of flocculation agent to carry out at twice.
In this flow process, a part for anaerobic digestion mud 11 and parting liquid 8 in Fig. 2 flow process be transported in digested sludge flocculation tank 12, the operation passing through to prepare while parting liquid 14 isolated by added flocculation agent 13 digested sludge throw out 15 changes as follows.
A part for anaerobic digestion mud 11 and parting liquid 8 is transported in sludge flocculation treatment unit 12a, passes through added flocculation agent 13a, preparation flocculation sludge 12c.Flocculation sludge 12c is incorporated in flocculation sludge separation concentration device 14A, and solid-liquid separation is parting liquid 14 and concentrated flocculation sludge 12d.Then, concentrated flocculation sludge 12d is transported in reconcentration flocculation sludge preparation facilities 12b, passes through added flocculation agent 13b and prepares reconcentration flocculation sludge, using this as final digested sludge throw out 15.
Then, Figure 4 shows that the feel flow draw of block of the 4th embodiment of the present invention, is the explanatory view of the formation representing anaerobism treatment unit, biological treatment of water 19 is added in sludge flocculation treatment unit 12a in the flow chart of figure 3, diluted by mud, other process is identical with Fig. 3.
As this biological treatment of water, active sludge treatment water, biological deodorizing process water, nitrated denitrogenation processing water etc. can be listed.Have influence on the kind of flocculation agent or addition and then expense due to biological treatment of water containing the kind of composition and concentration thereof, therefore, suitably determine according to processing intent.
Then, Figure 5 shows that the feel flow draw of block of the 5th embodiment of the present invention, be the explanatory view of the formation representing anaerobism treatment unit, be that the organic waste liquid transported from outside in the flow process of Fig. 4 or waste also carry out anaerobism consumption process, other process is identical with Fig. 4.
In this flow process, organic waste liquid or waste 20 are stored in biogas storage tank 21 as slurry, be incorporated at least in any one of storagetank 2, solubilized and acid-fermentation treatment unit 9a and anaerobic digestion device 9 after adjusting TS concentration as required from the slurry 22 of biogas storage tank 21, and implement process.
The anaerobism treatment unit of above-mentioned Fig. 1 ~ 5 can control automatically, also can batch process, also can be its combination.In addition, the temperature of various mud controls can be automatization.
Embodiment
Below embodiments of the invention are described.For the sewage sludge produced from A sewage work, carry out anaerobism process of the present invention test.It should be noted that, the present invention is not by any restriction of this embodiment.
In test, add in mud, mix the ratio of 0.4%(relative to SS) cationic polymeric flocculant (molecular-weight average 3,000,000), carries out flocculation treatment, then, in the mechanical thickener with back pressure plate, solid-liquid separation is sludge condensation thing and parting liquid.The proterties of mud, sludge condensation thing, parting liquid has been shown in table 1.
The anaerobic digestion test conditions of anaerobic digestion device has been shown in table 2.In anaerobism process test, use the complete mixed type digestion trial device (cubic capacity 30L, useful volume 25L, chuck Warm water circulation formula) of heat-resisting vinylchlorid.In addition, solubilized with in acid-fermentation device, use the complete mixed type of Tokyo physics and chemistry apparatus (strain) fermentor tank processed MDL(cubic capacity 10L, operate under the 4L depth of water).In test, anaerobic digestion device (digestive shelf) operates at 37 DEG C, operates in solubilized and acid-fermentation device (solubilized groove) at 45 DEG C.Wherein, in comparative example 2, carry out the high temperature anaerobic process test of 55 DEG C.Raw material comes into operation tube pump RP-60 type (Tokyo Physico-chemical Apparatus Co., Ltd.'s system), and every natural gift drop into for 4 ~ 8 times under timing register controls.
[embodiment 1]
According to the flow implementation of Fig. 1.
[embodiment 2]
According to the flow implementation of Fig. 2.Wherein, about the processed of anaerobic digestion mud, the treatment process combination shown in Fig. 3 and Fig. 4 is carried out.
[comparative example]
According to the flow implementation of Fig. 6.Wherein, digested sludge throw out 15 is by utilizing the sludge flocculation of polymeric flocculant to prepare.
[table 1]
The proterties of table 1 sewage sludge sample
Mud Sludge condensation thing Parting liquid
pH - 5.2 5.3 5.2
M basicity (mg/L presses CaCO 3Meter) 600 950 530
TS (g/L) 29.5 72.7 -
VTS (%) 86 87 -
SS (g/L) 24.0 71.8 307※
VSS (%) 88 88 -
Thick seston (%, SS ratio) 37 35 -
Kj-N (mg/L) 1,730 4,280 431
T-P (mg/L) 615 1,360 156
※ unit: mg/L
[table 2]
Table 2 anaerobism process test conditions
Wherein, analytical procedure is carried out according to following method.
TS(TotalSolids, total evaporation residue): 105 DEG C of evaporation residue weight (JISK0102)
VTS(Volatiletotalsolids, burning decrement): 600 DEG C of burning decrements (JISK0102)
SS(Suspendedsolids, suspended particle): utilize centrifugal separation in the weight of precipitate (JISK0102) of rotating speed under 3,000rpm, 10 minutes
VSS(Volatilesuspendedsolids, volatility suspended particle): 600 DEG C of burning decrements (JISK0102) of suspended particle
COD cr(chemical oxygen consumption): potassium dichromate process (JISK0102)
BOD(biological chemistry zmount of oxygen consumption): Winkler (Winkler) sodiumazide revised law (JISK0102)
Protein: (kelvin (Kjeldahl) nitrogen-ammonium-nitrogen) × 6.25
VFA (VFA): high performance liquid chromatography (ERMAOPTICALERC-8710, detector RI, post ShodexRSpakKC-811, column temperature 60 DEG C, moving phase 0.1% phosphoric acid)
Methane gas, carbonic anhydride: gas chromatograph (GLScienceGC-323, detector TCD, TCD current value 120A, separator column ActiveCarbon30/60, column temperature 95 DEG C, carrier gas He)
Siloxanes in digestive gas: digestive gas is passed in hexane solution with the circulation speed of 0.6L/ minute, after trapping siloxanes, concentrated, by gas chromatograph-mass spectrometer GC/MS quantitative analysis.Herein, decamethylcyclopentasiloxane (D5) concentration being considered to the annular siloxane that content is maximum in sewage sludge digestive gas is evaluated by quantitative analysis.
Solvability fraction: GF/B(1 μm) filtrate
M basicity: be titrated to pH4.8(sewage test method with the supernatant liquor that the hydrochloric acid soln of 0.1mol/L will utilize separating centrifuge to obtain under 3,000rpm, 3 minutes at rotating speed)
Thick seston: analyze (sewage test method) with the thick seston of specified size 74 μm of sieves
[table 3]
Table 3 anaerobism result
1) calculated by the input mud of each composition and the difference of Digestive system
2) D: digestibility
D = ( 1 - VS 2 &CenterDot; A 1 VS 1 &CenterDot; A 2 ) &times; 100 VS 1: the organic composition (%) dropping into mud
VS 2: the organic composition (%) of digested sludge
A 1: the inorganic components (%) dropping into mud
A 2: the inorganic components (%) of digested sludge
As shown in the anaerobism process test-results of table 3, in the anaerobism process of embodiment 1 and 2, obtain the performance of the TS rate of decomposition equal with prior art, VTS rate of decomposition, methane gas incidence.
In addition, when comparing the siloxanes D5 concentration in digestive gas, in embodiment 1 and 2, its containing ratio reduces, and it is believed that because silicone compounds is adsorbed in in the digested sludge SS composition of high density maintenance, thus the siloxane concentrations step-down in digestive gas.
In addition, during thicker seston, can find out, in embodiment 1 and 2, its containing ratio increases, and compared with existing digested sludge, defines the mud condition more favourable to sludge dewatering.
Wherein, in any digestive shelf of comparative example, embodiment, do not find the residual of VFA, therefore think that anaerobism processing reaction is carried out no problemly.
Use the anaerobic digestion mud obtained in above-mentioned comparative example 1 and 2, embodiment 1 and 2, research sludge dewatering treatment performance.Sludge dewatering uses cationic polymeric flocculant (molecular-weight average 3,000,000).In addition, water extracter uses press belt type water extracter, and processed condition was carried out under filter cloth tension force 4.9kN/m, filter cloth speed 1.0m/ minute.
First, carry out processed, result to the anaerobic digestion mud of comparative example 1 and 2, polymeric flocculant input rate and dewatered cake water ratio are the result of table 4.
[table 4]
The processed result (1) of table 4 anaerobic digestion mud
Then, the result of the processed result of anaerobic digestion mud obtained in embodiment 1 and 2, polymeric flocculant input rate and dewatered cake water ratio is the result of table 5.In any dewatering, be high performance relative to existing method, wherein, can find out, the processing mode that the flocculation agent shown in Fig. 4 injects, combinationally uses biological treatment of water is at twice the most effective.Wherein, the anaerobic digestion mud obtained in embodiment 1 dilutes without Separation of Water, and directly inject polymeric flocculant, during by sludge flocculation, processed, polymeric flocculant input rate is that 3.8%(is relative to SS), dewatered cake water ratio is 83%.
[table 5]
The processed result (2) of table 5 anaerobic digestion mud
In all tests of ※, anaerobic digestion mud: the liquid measure ratio of parting liquid is 1:0.5, by parting liquid dilution mixture in first time flocculation agent injection process, M basicity during dilution mixture is 2500 ~ 3600mg/L
[embodiment 3]
Then, according to Fig. 5, the embodiment of carrying out sewage sludge and food mfg waste (waste saccharide liquid and dessert system waste prods) and rivers and creeks and taking up an area the anaerobism process of mowing is described.
< treatment condition >
Sewage sludge amount (mixing sludge of primary sludge and excess sludge) 30m 3/ sky (TS concentration 3.1%)
The food mfg waste amount of being transported into 1.35t/ days (TS concentration 9.9%)
Rivers and creeks takes up an area the mowing amount of being transported into 0.15t/ days (water ratio 70.0%)
Biogas storage tank 3m 2× 2 grooves
< pre-treatment equipment for separating liquid from solid (sewage mixing sludge >
Slit type thickner (screen cloth wavelength width of a slit 1.0mm, with back pressure plate)
Cationic polymeric flocculant (molecular-weight average 3,000,000) input rate 0.4%(is relative to the ratio of SS)
Sludge condensation thing amount 12t/ days (TS concentration 7.9%)
Be separated liquid measure 19.5m 3/ sky (SS concentration 395mg/L)
The SS rate of recovery 97%
Mowing shredding unit
< anaerobic digestion: solubilized and acid-fermentation device (vertical mechanical formula stirrer >
Food mfg waste, rivers and creeks take up an area mow, the mixture of the sludge condensation thing input amount 3m in solubilized and acid-fermentation device 3/ sky (slurry TS concentration: 10%)
Food mfg waste and rivers and creeks take up an area the ratio 19% of TS relative to the TS of sludge condensation thing of mowing
HRT2 days
Useful volume 6m 3
Water temperature 45 DEG C
< anaerobic digestion: anaerobic digestion device (vertical mechanical formula stirrer) >
Input amount 13.5m in anaerobic digestion device 3/ sky
HRT14.8 days
Useful volume 200m 3
Water temperature: 37 DEG C
The flocculation treatment operation > of < anaerobic digestion mud
Slit type thickner (screen cloth wavelength width of a slit 1.0mm)
The combined amount 10.5m of mud parting liquid 3/ sky (M basicity 690mgCaCO 3/ L)
The combined amount 3.5m of biological deodorizing device waste liquid 3/ sky (M basicity 1250mg/L)
Cationic polymeric flocculant (molecular-weight average 3,000,000) input rate 1.7%(is relative to the ratio of SS)
(input rate is detailed: the input rate 1.3% of leading portion flocculation tank, the input rate 0.4% of reflocculation groove)
< water extracter >
Helical pressure type water extracter
< generator >
Micro gas turbine generator
< result >
Anaerobic digestion sludge character (TS concentration 3.9%, VTS68%, SS concentration 3.0%, M basicity 8900mgCaCO 3/ L, thick seston containing ratio 16.7%(is relative to the ratio of SS))
Biogas generation 570m 3/ sky (NTP)
Methane gas generation 365m 3/ sky (NTP)
Concentration of methane gas 64%
Methane gas production rate 0.37m 3/ drop into kgVTS(NTP)
Siloxanes D5 concentration 2.3mg/m in biogas 3
Generated energy 686kwh/ days
Dewatered cake generation 2.1t/ days (water ratio 77%)
Wastewater flow rate 37.6m 3/ sky
As mentioned above, can find out, according to the present invention, by the anaerobic digestion device of remarkable miniaturization compared with the past, by mud, the process of organic waste anaerobism, stably can produce the biogas of high-quality, can biogas generating be carried out.In the processing mode of existing methodical HRT20 ~ 30 day, need to arrange anaerobic digestion groove 630 ~ 945m 3, on the other hand, in the present invention, owing to being 206m 3anaerobic digestion device, therefore, can be contracted in the system of existing 1/3 ~ 1/4 at anaerobism recess gauge mould and carry out anaerobism process.In addition, the anaerobic digestion mud produced flocculates and dehydration with low cost by easy operation, gained dewatered cake water ratio 77% is low-water-content (with reference to table 4) compared with existing about 82%, outward appearance and currently available products do not change, there is no undesirable smell, and be health.
[embodiment 4]
Similarly to Example 3, according to Fig. 5, in sewage farm, carry out the anaerobism process of sewage sludge and food mfg waste (fruit juice citrus waste matter).Sewage sludge is the first heavy thickened sludge of gravity concentration and the mixing sludge of excess sludge, implements sludge condensation.Anaerobic digestion is implemented under the mixture ratio of basic equivalent in each solid substance amount of sewage sludge and citrus waste matter.
< treatment condition >
Sewage sludge amount (mixing sludge of primary sludge and excess sludge) 35m 3/ sky
(primary sludge: TS concentration 3.88%, excess sludge: TS concentration 0.93%, mixing sludge: TS concentration 1.39%)
The food mfg waste amount of being transported into 4.0t/ days (TS concentration 12.5%)
Biogas storage tank 3m 2× 2 grooves
< pre-treatment equipment for separating liquid from solid (sewage mixing sludge >
Slit type thickner (screen cloth wavelength width of a slit 1.0mm, with back pressure plate)
Cationic polymeric flocculant (molecular-weight average 3,000,000, strength of solution 2.0g/L) injection rate 0.95m 3/ sky
Polymeric flocculant input rate 0.44%(is relative to the ratio of SS)
Sludge condensation thing amount 6.2t/ days (TS concentration 7.5%)
Be separated liquid measure 29.8m 3/ sky (SS concentration 230mg/L)
The SS rate of recovery 98%
Solubilized and the acid-fermentation device > of < food mfg waste
6.0m 3× 1 groove, vertical mechanical stirrer, 37 DEG C of heating
The TS of food mfg waste is relative to the ratio 102% of the TS of sludge condensation thing
< anaerobic digestion device (vertical mechanical formula stirrer >
Input amount 10.2m in anaerobic digestion device 3/ sky
HRT19.6 days
Useful volume 200m 3
Water temperature 37 DEG C
The flocculation treatment operation > of < anaerobic digestion mud
Slit type thickner (screen cloth wavelength width of a slit 1.0mm)
The combined amount 2.0m of mud parting liquid 3/ sky (M basicity 320mgCaCO 3/ L)
Cationic polymeric flocculant (molecular-weight average 3,000,000) input rate 1.6%(is relative to the ratio of SS)
Flocculation agent injection process 1 time
< water extracter >
Helical pressure type water extracter
< generator >
Micro gas turbine generator
< result >
Anaerobic digestion sludge character (TS concentration 3.8%, VTS70%, SS concentration 3.2%, M basicity 4490mgCaCO 3/ L, thick seston containing ratio 12.1%(is relative to the ratio of SS))
Biogas generation 591m 3/ sky (NTP)
Methane gas generation 349m 3/ sky (NTP)
Concentration of methane gas 59%
Methane gas production rate 0.38m 3/ drop into kgVTS(NTP)
Siloxanes D5 concentration 1.2mg/m in biogas 3
Generated energy 656kwh/ days
Dewatered cake generation 1.6t/ days (water ratio 78%)
Wastewater flow rate 41.5m 3/ sky
As mentioned above, can find out, in utilizing sewage sludge of the present invention concentrated, for there is no mechanical thickening and the only first heavy thickened sludge of gravity concentration and the mixing sludge (TS concentration 1.39%) of excess sludge, can effectively concentration to TS concentration 7.5%(sludge condensation multiplying power about 5.4 times), the various mechanical thickening equipment of at present mostly application can be omitted.And in the present invention, in the anaerobic digestion device of remarkable miniaturization, even if each solid substance amount of thickened sludge and citrus waste matter carries out anaerobic digestion process with the mixture ratio of basic equivalent, also Absorbable organic halogens ground produces the biogas of high-quality.In addition, the anaerobic digestion mud produced flocculates and dehydration with low cost by easy operation similarly to Example 3, and gained dewatered cake water ratio 78% is compared with the past is low-water-content.
[embodiment 5]
The waste liquid produced in research performation example 3 and 4 and effective utilization of dewatered cake.The phosphorus that the parting liquid produce the solid-liquid separation by the sewage sludge being equivalent to pretreatment process of the present invention and the dehydration parting liquid of dehydration procedure reclaim, the dewatered cake produced by the dehydration procedure of anaerobic digestion sludge condensation thing carry out composting.
< treatment condition >
(1) phosphorus of the solid-liquid separation waste liquid of mud reclaims (MAP method)
PH8.3 during reaction, Mg concentration is more than 30mg/l
Single-channel type reactor (reacting part: diameter 35cm × height 2.2m, precipitation portion: diameter 80cm × height 1.8m, is pre-charged with the crystal seed of particle diameter about 0.4 ~ 1.0mm)
Phosphorus volumetric loading 20kg-P/m 3my god
(2) composting of dewatered cake
Composting testing apparatus 15m 3(high rate composting vertical type fermentation groove)
The moisture of dewatered sludge adjusts mud mechanical drying, water ratio 45 ~ 55%
Do not add subsidiary material
Draft speed 0.15m during composting 3/ t minute
< result >
[table 6]
Table 6 phosphorus reclaims
[table 7]
Table 7 product compost proterties
As can be seen from the above, in the present invention, the devil liquor recovery phosphorus produced from embodiment 3 and 4, dewatered cake can composting, and quality there is no change with currently available products (as comparative example, listing the compost proterties of food waste system mesophilic methane fermentation mud).The organic matter decomposition rate of composting is 24% in the mud of embodiment 3, is 28% in example 4.Wherein, the gross calorific value (HigherHeatingValue) of dewatered cake is 17MJ/kg-dry in the mud of embodiment 3, be 17.3MJ/kg-dry in the mud of embodiment 4, therefore, by this dewatered sludge mechanical drying, there is the quality [quality standard of fuel compound (granulating and drying compound) is more than thermal value 4000kal/kg (more than 16.7MJ/kg)] that can be used as sludge fuel and effectively utilize.
description of reference numerals
1 ... mud, 2 ... storagetank, 3 ... flocculation tank, 4 ... flocculation agent, 5 ... flocculation sludge, 6 ... pretreating sludge thickener, 7 ... sludge condensation thing, 7a ... digested sludge, 8 ... parting liquid, 9 ... anaerobic digestion groove, 9a ... solubilized and acid-fermentation treatment trough, 10 ... biogas, 11 ... anaerobic digestion mud, 12 ... digested sludge flocculation plant, 12a ... sludge flocculation treatment trough, 12b ... reconcentration flocculation sludge preparation facilities, 12c ... flocculation sludge, 12d ... concentrated flocculation sludge, 14A ... flocculation sludge separation concentration device, 15 ... digested sludge throw out, 13, 13a, 13b ... flocculation agent, 14 ... parting liquid, 15 ... digested sludge throw out, 16 ... dewatering unit, 17 ... parting liquid, 18 ... dewatered cake, 19 ... biological treatment of water, 20 ... organic waste liquid or waste, 21 ... biogas storage tank, 101 ... biological gas tank, 102 ... gas utilizes equipment, 103 ... residual gas combustion equipment, 104 ... sewage treatment equipment.

Claims (13)

1. an anaerobic treatment method, it comprises:
The flocculation sludge solid-liquid separation prepared adding flocculation agent in mud is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the pretreatment process of parting liquid, and described mud is selected from least one in the excess sludge of primary sludge and the final tank generation produced by the initial settling tank of sewage treatment equipment;
This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion operation of biogas, and described anaerobic digestion operation comprises: under the condition for the treatment of temp 30 ~ 60 DEG C, HRT1 ~ 3 day, carry out leading portion digestion operation that is solubilized and acid-fermentation process; And with treatment temp 30 ~ 60 DEG C, HRT12 ~ 15 day and carry out methane fermentation process relative to the mode that the thick seston containing ratio of the SS (suspended particle) of mud is 3 ~ 20wt%, prepare the methane fermentation operation of anaerobic digestion mud;
The anaerobic digestion mud prepared in this anaerobic digestion operation is mixed with flocculation agent and described parting liquid, the digested sludge flocculation operation of preparation digested sludge throw out;
The digested sludge enrichment process of digested sludge enriched material and parting liquid prepared by this digested sludge throw out solid-liquid separation; And
The operation that the digested sludge enriched material obtained solid-liquid separation dewaters.
2. anaerobic treatment method according to claim 1, wherein, described flocculation sludge is prepared relative to the flocculation agent that the SS (suspended particle) of mud is 0.2 ~ 1.0wt% by use.
3. anaerobic treatment method according to claim 1, wherein, the organic waste liquid transported from outside or waste are adjusted to slurry TS concentration 1 ~ 15wt%, be transported in described anaerobic digestion operation, under the mixing condition reaching relative to the TS of described sludge condensation thing the slurry TS ratio being below 120wt%, carry out anaerobic digestion.
4. anaerobic treatment method according to claim 1, wherein, described anaerobic digestion operation comprises: under the condition for the treatment of temp 30 ~ 60 DEG C, HRT1 ~ 3 day, carry out leading portion digestion operation that is solubilized and acid-fermentation process to described sludge condensation thing; And methane fermentation process is carried out in the digested sludge processed in this leading portion digestion operation, prepare the methane fermentation operation of described anaerobic digestion mud,
The organic waste liquid transported from outside or waste are adjusted to slurry TS concentration 1 ~ 15wt%, be transported in described anaerobic digestion operation, under the mixing condition reaching relative to the TS of described sludge condensation thing the slurry TS ratio being below 120wt%, carry out anaerobic digestion.
5. anaerobic treatment method according to claim 1, wherein, described digested sludge enriched material is prepared by least carrying out 2 flocculation agent injection process at the in-process be made up of flocculation agent injection process and follow-up solid-liquid separation process.
6. anaerobic treatment method according to claim 1, wherein, described anaerobic digestion operation comprises: under the condition for the treatment of temp 30 ~ 60 DEG C, HRT1 ~ 3 day, carry out leading portion digestion operation that is solubilized and acid-fermentation process to described sludge condensation thing; And methane fermentation process is carried out in the digested sludge processed in this leading portion digestion operation, prepare the methane fermentation operation of described anaerobic digestion mud,
The organic waste liquid transported from outside or waste are adjusted to slurry TS concentration 1 ~ 15wt%, be transported in described anaerobic digestion operation, anaerobic digestion is carried out under the mixing condition reaching relative to the TS of described sludge condensation thing the slurry TS ratio being below 120wt%
Described digested sludge enriched material is prepared by least carrying out 2 flocculation agent injection process at the in-process be made up of flocculation agent injection process and follow-up solid-liquid separation process.
7. an anaerobism treatment unit, it comprises:
The mud storage facility of storage mud, described mud is selected from least one in the excess sludge of primary sludge and the final tank generation produced by the initial settling tank of sewage treatment equipment;
In the mud from mud storage facility, add flocculation agent and prepare the flocculation tank of flocculation sludge;
Solid-liquid separation is the sludge condensation thing of sludge concentration 4 ~ 12wt% and the pretreating sludge concentrating unit of parting liquid;
This sludge condensation thing anaerobic digestion is reclaimed the anaerobic digestion device of biogas, and described anaerobic digestion device possesses: under the condition for the treatment of temp 30 ~ 60 DEG C, HRT1 ~ 3 day, carry out solubilized and acid-fermentation treatment unit that is solubilized and acid-fermentation process; And with treatment temp 30 ~ 60 DEG C, HRT12 ~ 15 day and carry out methane fermentation process relative to the mode that the thick seston containing ratio of the SS (suspended particle) of mud is 3 ~ 20wt%, prepare the methane fermentation device of anaerobic digestion mud;
The anaerobic digestion mud prepared in this anaerobic digestion device is mixed with flocculation agent and described parting liquid and prepares the digested sludge flocculation plant of digested sludge throw out;
Parting liquid from this pretreating sludge concentrating unit is delivered to the pipe arrangement of this digested sludge flocculation plant;
This digested sludge throw out solid-liquid separation is obtained by this flocculation sludge concentrating unit of digested sludge enriched material and parting liquid; And
To the device that the digested sludge enriched material obtained dewaters.
8. anaerobism treatment unit according to claim 7, it pipe arrangement possessing the mechanism the mud being supplied to by flocculation agent and discharging from described mud storage facility and be used for carrying mud.
9. the anaerobism treatment unit according to claim 7 or 8, wherein, described solubilized and acid-fermentation treatment unit and described methane fermentation device treatment temp is 30 ~ 60 DEG C.
10. the anaerobism treatment unit according to claim 7 or 8, it possesses the device of preparation digested sludge enriched material further, and the device of described preparation digested sludge enriched material possesses: by described flocculation agent prepare flocculation sludge sludge flocculation treatment unit, by this flocculation sludge solid-liquid separation being prepared the device of concentrated flocculation sludge, being prepared the device of reconcentration flocculation sludge by flocculation agent by this concentrated flocculation sludge.
11. anaerobism treatment unit according to claim 7 or 8, wherein, described anaerobic digestion device comprises: carry out the solubilized and acid-fermentation treatment unit of solubilized and acid-fermentation process to described sludge condensation thing and the digested sludge processed in and acid-fermentation treatment unit solubilized at this carried out to the methane fermentation device of methane fermentation process
Described anaerobism treatment unit possesses the device of preparation digested sludge enriched material further, and the device of described preparation digested sludge enriched material possesses: by described flocculation agent prepare flocculation sludge sludge flocculation treatment unit, by this flocculation sludge solid-liquid separation being prepared the device of concentrated flocculation sludge, being prepared the device of reconcentration flocculation sludge by flocculation agent by this concentrated flocculation sludge.
12. anaerobism treatment unit according to claim 7, it possesses:
Solubilized and the acid-fermentation treatment unit of solubilized and acid-fermentation process is carried out to described sludge condensation thing and the digested sludge processed in and acid-fermentation treatment unit solubilized at this is carried out to the methane fermentation device of methane fermentation process;
Store the external biogas storage facility of organic waste liquid or the waste transported from outside; And mechanism at least any one device biogas of discharging from this external biogas storage facility being imported in the group that is selected from and is made up of described mud storage facility, described solubilized and acid-fermentation treatment unit and described methane fermentation device and pipe arrangement.
13. anaerobism treatment unit according to claim 7, it possesses:
Solubilized and the acid-fermentation treatment unit of solubilized and acid-fermentation process is carried out to described sludge condensation thing and the digested sludge processed in and acid-fermentation treatment unit solubilized at this is carried out to the methane fermentation device of methane fermentation process;
The device of preparation digested sludge enriched material, the device of described preparation digested sludge enriched material possesses: by described flocculation agent prepare flocculation sludge sludge flocculation treatment unit, by this flocculation sludge solid-liquid separation being prepared the device of concentrated flocculation sludge, being prepared the device of reconcentration flocculation sludge by flocculation agent by this concentrated flocculation sludge;
Store the external biogas storage facility of organic waste liquid or the waste transported from outside; And mechanism at least any one device biogas of discharging from this external biogas storage facility being imported in the group that is selected from and is made up of described mud storage facility, described solubilized and acid-fermentation treatment unit and described methane fermentation device and pipe arrangement.
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