CN202107700U - Separate two-phase anaerobic fermentation device - Google Patents

Separate two-phase anaerobic fermentation device Download PDF

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Publication number
CN202107700U
CN202107700U CN2011201691812U CN201120169181U CN202107700U CN 202107700 U CN202107700 U CN 202107700U CN 2011201691812 U CN2011201691812 U CN 2011201691812U CN 201120169181 U CN201120169181 U CN 201120169181U CN 202107700 U CN202107700 U CN 202107700U
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liquid
natural pond
oxidation
pond
acidication
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毛正荣
常志州
叶小梅
罗永成
杜静
王志荣
徐霄
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QUZHOU DOHI AND COUNTRYSIDE ENERGY TECHNOLOGY PROMOTION STATION
Jiangsu Academy of Agricultural Sciences
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QUZHOU DOHI AND COUNTRYSIDE ENERGY TECHNOLOGY PROMOTION STATION
Jiangsu Academy of Agricultural Sciences
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    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12MAPPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12MAPPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M27/00Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/02Stirrer or mobile mixing elements
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    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12MAPPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00Means for pre-treatment of biological substances
    • C12M45/04Phase separators; Separation of non fermentable material; Fractionation
    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12MAPPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00Means for pre-treatment of biological substances
    • C12M45/06Means for pre-treatment of biological substances by chemical means or hydrolysis
    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12MAPPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18Gas cleaning, e.g. scrubbers; Separation of different gases
    • 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 utility model relates to a separate two-phase anaerobic fermentation device, which comprises a hydrolytic acidification reaction device, an anaerobic fermentation device, a biogas treatment device and a biogas slurry oxidation device, wherein the hydrolytic acidification reaction device comprises at least two parallel-connected hydrolytic acidification reaction tanks of a hydrolytic acidification basic unit, and a hydrolyzate collection tank, and the anaerobic fermentation device is a sealed anaerobic digestion reactor; a feed port is arranged at the bottom of the anaerobic fermentation device, and a biogas outlet is arranged at the top of the anaerobic fermentation device; a biogas slurry overflowing port is arranged at a position which is 80% -90% of the total height of the anaerobic fermentation device, and the biogas slurry oxidation device is a biogas slurry oxidation tank; and baffles which are vertically staggered are arranged in the biogas slurry oxidation device, and the volume ratio of the hydrolytic acidification tank, the anaerobic digestion reactor, and the biogas slurry oxidation tank is 2-5:1:0.2-0.5.

Description

Separate type diphasic anaerobic fermentation fermentation unit
Technical field
The utility model relates to a kind of separate type diphasic anaerobic fermentation fermentation unit, belongs to the rural ecological environment protection and the rural area renewable and clean energy resource utilizes the field.
Background technology
In recent years, along with China's rapid economic development, urbanization process are accelerated, environmental problem more and more receives people's attention.Certificate was firmly built the investigation of portion to national part rural area in 2005; The annual sewage that produces in China rural area reaches more than 80 hundred million tons, 96% rural area does not have WWT and gathering system; Sewage arbitrarily discharges, serious harm tap water, ecological environment security and resident healthy.In addition, a large amount of agricultural crop straws are not utilized, and arbitrarily abandon or burn, and cause accidents such as serious environmental pollution and fire.
Rice straw, sewage are carried out hybrid anaerobic fermentation as the biogas raw material, can solve the rural environmental pollution problem on the one hand, also can produce clean energy biogas on the other hand, satisfied the dual needs of environment protection and Sustainable development.
Publication number is the patent of CN1769220; Proposed to use kitchen excess, stalk, feces of livestock and poultry and the active sludge biogas production technology as raw material, this patent characteristic is to adopt two parallel high solid substance marsh gas reactors, with city domestic sewage treatment plant anaerobically digested sludge as kind of a mud; In reactor drum, raw material kitchen excess, stalk, feces of livestock and poultry, active sludge and kind mud are mixed; The quality proportioning of kitchen excess, stalk, feces of livestock and poultry and active sludge is 1: 1: 1: 1, and planting the mud consumption is 25% of material quantity, warm 33-37 ℃ anaerobically fermenting during northern area is taked; Southern area is taked middle high temperature 33-55 ℃ anaerobically fermenting; The pH value maintains 7.0, and humidity is controlled at 90%-100%, and the residence time of material in reactor drum is 40-45 days; Per 2 days input and output materials once.
Publication number is the patent of CN101020912; A kind of method of the stalk mixing fermentation of methane bacterium refluxing and pulverizing being produced biogas is proposed; It is characterized in that; It is to adopt the raw material agricultural crop straw with fermentation methane to be ground into stalk powder, stalk particle, stalk silk, reenters marsh-gas fermentation tank, and marsh-gas fermentation tank bottom discharge pipe is discharged contains the methanobacteria slag charge; According to the contained methanobacteria quantity of practical measurement, be to be input to the marsh-gas fermentation tank production biogas that continuously ferments after 0.5~8.0: 1.0 the mixed by containing methanobacteria slag charge and the new volume ratio that drops into stalk.
Publication number is the patent of CN10159167; A kind of pure straw stackretting-free feeding methane fermentation method has been proposed; This method is: start by conventional zymotechnique, with the preferred natural pond of bacterial classification slag stalk is inoculated, fed intake, add water at 9: 1 by ratio of water to material; Water material to be added accounts for and stops pan feeding when methane-generating pit always ferments volume 10%, waits for aerogenesis; Behind the normal gas producing, stalk broken hand hay cutter or blue or green storage feeds intake by the multiple feed mode, and only fed intake by an opening for feed every day, changed next opening for feed in second day to feed intake, with this by day feeding intake by a mouthful circulation; The methane-generating pit inner top is equipped with a plurality of shower nozzles, and scum pump is set at the bottom of the pond, by scum pump the natural pond liquid of methane-generating pit bottom is transported to shower nozzle through liquid-transport pipe-line, sprays getting into the fermentation raw material that floats over liquid top, natural pond in the methane-generating pit, makes raw material acidifying neutralization; Discharge a certain amount of useless natural pond slag that has fermented and finished by the inlet amount on the same day by the methane-generating pit bottom every day.
More than the technology that proposes of these patents be single-phase anaerobic ferment process, i.e. acidication and produce methane and in same reactor drum, carry out.Many to rural area organic waste kind, the source is complicated and based on the biological procedures of anaerobically fermenting, the anaerobic biological treatment novel process that early 1970s U.S.'s dagger-axe assorted (Ghosh) and portland (Pohland) are developed.This fermentation system carries out two step of reaction of acidication and product methane respectively at two reactive systems; 2 different biologies and nutrient environment condition have been created; Like temperature and pH value etc.; Each self-forming acidogenic fermentation mikrobe and the best ecological condition that produces the methane fermentation mikrobe are to reach the purpose of optimizing each stage process parameter.Ghosh (1995) is a substrate with the solid waste organic matter in city; Discovery is in two cancellation ratio processes; The transformation efficiency of its biogas yield and volatile solid all increased than single plane method, and Zhang etc. have carried out the experimental study of diphasic anaerobic fermentative processing straw in 1999, and this technology is reasonably cut apart solid state fermentation and liquid state fermentation and connect; Make the stability of reaction and the capacity utilization of reactor drum improve, also improved the efficient of anaerobic biodegradation simultaneously.Lehtom ki (2008) adopts two to ferment mutually and single-phase zymotechnique processing ensiling grass, and the product acid phase that single-phase fermentation and two is fermented is mutually accomplished in dripping the filter bed reactor drum, produces methane phase and in the UASB reactor drum, accomplishes.Test-results shows that methane production reaches 66% of theoretical methane production when adopting two phase zymotechniques, and single-phase fermentation has only 20%.Liu Guangqing (2006,2007) etc. with the kitchen surplus with weeds waste mixture be that fermentation substrate has carried out single-phase and diphasic anaerobic fermentation test, the result shows, with batch formula digestion relatively; This biphasic system pollution load is high; Aerogenesis is stable, and the cycle is short, is the effective ways of handling the type organic waste.Zhang Xingqing (2009) etc. have adopted two phase process technical study cities and towns organic waste hydrolysis experiments; Show and adopt natural pond liquid reflux type can obtain higher organic carbon solubility rate; It is that substrate discovers that in the waterpower residence time be 10 days that De LaRubia (2010) presses the slag residue with sunflower seed, and organic loading is 6gVSL -1D -1Under the condition; Its percent hydrolysis can reach 86%; The molecular biological method of Seung Gu Shin (2010) utilization has been studied superior microorganism flora in the two-phase reactor, finds can change to some extent with organic loading at hydrolysis phase superior microorganism, but is producing the methane phase; Then the dominant population Stability Analysis of Structures has proved that further two phase process can play the effect of optimizing two types of functional microorganism ecological conditions.Two ferment mutually both can independently carry out in the reactor drum at 2 respectively; Also can accomplish in 2 reaction zones in a reactor drum; Planning institute of the Ministry of Agriculture develops integrated two-phase anaerobic digestion techniques (publication number CN201581074U); Promptly in same digestive organ, realize two subregions mutually of " the solid phase filter tank is produced acid and mixed product methane entirely with liquid phase ", guaranteed acid-producing bacteria and the methanogen suitable growth environment in reaction zone separately.Compare with single-phase zymotechnique, the TPAD technology can reach following two purposes at least, and the one, can improve the activity of producing methanogen in the methane phase reactor; The 2nd, can improve the stability and the treatment effect of entire treatment system.
Yet; Achievement in research mentioned above and patented technology are when relating to stalk as raw material, and all proposition need be piled pre-treatment such as corruption or pulverizing, and the input and output material difficulty; Operational requirement is high; And the crushed stalk cost is high, the work work condition environment is abominable, and labor cost is high in addition, thereby causes existing technology to be difficult to promote the use of in the rural area; In addition; People such as Zhu Jin (2011) discover stalk two and single-phase fermentation comparison test, if it is not good to be separated in the two phase technologies, it is because the middle mutually methanogen of product methane constantly gets in the hydrolysis acidification pool; The ratio that causes final acidication to produce biogas mutually accounts for 79.52% of gross output biogas amount; And often acidication all is an open type mutually, will certainly cause a large amount of methane, carbonic acid gas isothermal chamber gas purging, and low-carbon (LC) and the circulating technology theory with biogas engineering runs in the opposite direction like this; Once more, all can produce a large amount of natural pond liquid in the existing biogas engineering,, will certainly cause secondary pollution or increase the weight of the burden of follow-up purifying treatment if can not get properly using and discharging arbitrarily, and present technology that has and patent these practical problemss of solution all not yet in effect.
The utility model content
The purpose of the utility model is: existing rural area organic waste producing methane through anaerobic fermentation technology, all require material is pulverized or pre-treatment such as broken or heap corruption, and complicated operation, technical requirements are high; Secondly; Be the two phase zymotechniques that adopt acidication batch charging, produce the mutually semicontinuous charging of methane, can not need substrate be done special pre-treatment, but require to carry out airtight reactor for hydrolysis and acidification; To collect part biogas; Thereby increased construction, input and output material operation easier, and also increased a series of problems such as cost of investment, proposed a kind of separate type diphasic anaerobic fermentation unit.
The purpose of the utility model is achieved in that a kind of separate type diphasic anaerobic fermentation fermentation unit, it is characterized in that: comprise acidication reaction unit, anaerobic ferment devices, biogas treatment unit and natural pond liquid oxidation device, wherein:
A) described acidication reaction unit comprises the acidication reaction tank and the hydrolyzed solution collecting tank of the acidication elementary cell of at least two parallel connections; Each elementary cell is open solid accumulation pond; The solid accumulation pond is provided with that the reuse of natural pond liquid enters the mouth after acidication liquid outlet and the oxidation; Described acidication liquid outlet is positioned at the bottom in solid accumulation pond, and links up with the hydrolyzed solution collecting tank, and the reuse inlet of natural pond liquid is equipped with independently valve after described acidication liquid outlet and the oxidation; The top of each elementary cell all is furnished with independently fence cover plate, and each elementary cell all is furnished with independently rain-proof shelter; The reuse of natural pond liquid inlet is greater than or equal to the installation site of fence cover plate after the described oxidation;
B) described anaerobic ferment devices is that airtight anaerobic digestion reaction vessel, anaerobic digestion reaction vessel bottom is provided with opening for feed, is provided with the biogas delivery port at the anaerobic digestion reaction vessel top; Height at anaerobic digestion reaction vessel 0.8~0.9 is provided with natural pond hydrorrhea head piece, and natural pond hydrorrhea head piece is furnished with filtration unit; The hydrolyzed solution collecting tank is linked up through the opening for feed of fresh feed pump and anaerobic digestion reaction vessel;
C) described natural pond liquid oxidation device is liquid oxidation pond, natural pond; One end in liquid oxidation pond, natural pond is a natural pond liquid opening for feed, and the other end is an oxidized natural pond liquid discharge port, by the natural pond liquid opening for feed in liquid oxidation pond, natural pond to being provided with the baffling shutter of dislocation up and down the liquid discharge port of oxidized natural pond; Baffling shutter to liquid oxidation pond, major general natural pond is divided into three oxidation zones; Liquid oxidation pond, natural pond is furnished with oxygen-increasing device, and the air outlet of oxygen-increasing device is a micro porous aeration head, and described micro porous aeration head is distributed in the bottom of each oxidation zone; The natural pond hydrorrhea head piece of described natural pond liquid opening for feed and anaerobic digestion reaction vessel is linked up, and the reuse of natural pond liquid enters the mouth and docks after the oxidation of oxidized natural pond liquid discharge port and acidication liquid;
D) volume ratio in described hydrolysis acidification pool, anaerobic digestion reaction vessel, liquid oxidation pond, natural pond is 2~5: 1: 0.2~0.5.
In the utility model, the opening for feed of anaerobic digestion reaction vessel is provided with blade agitators apart from reactor bottom 50cm in the anaerobic digestion reaction vessel.
In the utility model, described natural pond liquid oxidation tank depth is no more than 1000mm; The oxidation zone that in natural pond liquid oxidation device, is positioned at natural pond liquid opening for feed one end is first oxidation zone, and at least one micro porous aeration head is positioned at the bottom of first oxidation zone.
In the utility model, described acidication reaction tank is made up of the acidication elementary cell of 2~6 parallel connections.
In the utility model; The outlet of the acidication liquid of described acidication reaction tank is higher than the design liquid level of the maximum hold-up of collecting tank of hydrolyzed solution collecting tank, and the oxidized natural pond liquid discharge port in liquid oxidation pond, natural pond is higher than the reuse inlet of natural pond liquid after the oxidation of hydrolysis acidification pool.
In the utility model, described hydrolyzed solution collecting tank places underground.
In the utility model, described acidication liquid places underground.
In the utility model, described acidication reaction tank and liquid oxidation pond, natural pond all are located at underground or on the ground, all are furnished with pressure pump between the reuse of the natural pond liquid inlet after the oxidized natural pond liquid discharge port in liquid oxidation pond, natural pond and the oxidation of acidication liquid and communicate with each other.
In the utility model; Described separate type diphasic anaerobic fermentation fermentation unit also comprises the biogas treatment unit; Described biogas treatment unit is made up of biogas gas holder, dehydration tower, thionizer, biogas supercharger; The biogas gas holder is connected with the biogas delivery port of anaerobic digestion reaction vessel, after biogas gas holder, dehydration tower, thionizer are connected in series successively, is connected with the biogas user by the biogas supercharger.
The advantage of the utility model is: adopt separate type diphasic anaerobic fermentation unit; Two processes of substrate hydrolysis acidifying and producing methane through anaerobic fermentation are separated; Wherein the acidication process is accomplished in uncovered pond, is convenient to input and output material at any time like this, and can adapt to the processing needs of different physical behavior substrates; After hydrolyzed solution gets into anaerobic digestion reaction vessel, can consume the oxygen in the reactor drum fast owing to self bring a certain amount of aerobic bacteria into, thereby not influence its anaerobic environment; After filtering processing, get rid of a large amount of impurity through the natural pond liquid after the Anaerobic Digestion, to prevent the obstruction in follow-up pipeline and liquid oxidation pond, natural pond; Natural pond liquid makes methanogen be killed basically because of contact oxygen after getting into behind the oxidation pond and handling through aeration aerating, is back to the risk that hydrolysis acidification pool causes methane to leak thereby reduced because of natural pond liquid.
The technological indicators of overall performance of the utility model is with similar technology advantage relatively: hydrolysis acidification pool is uncovered shape; Input and output material is simple to operate; And at any time can charging; Adapted to the uncertainty that countryside wastes produces kind and quantity preferably, and hydrolysis acidification pool do not do sealing treatment, reduced construction costs; The second, after filtering processing, get rid of a large amount of impurity through the natural pond liquid after the anaerobic digestion, prevented obstruction to follow-up pipeline and liquid oxidation pond, natural pond; The 3rd, natural pond liquid makes methanogen be killed basically because of contact oxygen after getting into behind the oxidation pond and handling through aeration aerating, is back to the risk that hydrolysis acidification pool causes methane to leak thereby reduced because of natural pond liquid; The 4th, convenient for maintenance management.
Description of drawings
Fig. 1 is the synoptic diagram of the embodiment of the utility model;
Fig. 2 is the structural representation in liquid oxidation pond, natural pond.
Among the figure: 1, acidication reaction tank; 2, standing bolt; 3, fence cover plate; 4, acidication liquid outlet; 5, hydrolyzed solution collecting tank; 6, fresh feed pump; 7, anaerobic digestion reaction vessel; 8, opening for feed; 9, natural pond hydrorrhea head piece; 10, phonomoter; 11, blade agitators; 12, biogas delivery port; 13, strainer; 14, natural pond liquid oxidation pond; 15, oxygen-increasing device; 16, micro porous aeration head; 17, baffling shutter; 18, oxidized natural pond liquid discharge port; 19, the reuse of natural pond liquid inlet; 20, biogas gas holder; 21, dehydration tower; 22, thionizer; 23, biogas supercharger.
Embodiment
Accompanying drawing discloses the concrete structure of the utility model embodiment without limitation, below in conjunction with accompanying drawing present embodiment is further described.
Visible by Fig. 1 and Fig. 2, separate type diphasic anaerobic fermentation fermentation unit comprises acidication reaction unit, anaerobic ferment devices and natural pond liquid oxidation device, wherein:
The acidication reaction unit comprises the acidication reaction tank 1 and hydrolyzed solution collecting tank 5 of the acidication elementary cell of 2~6 parallel connections; Each elementary cell is open solid accumulation pond; The solid accumulation pond is provided with the reuse inlet 19 of natural pond liquid after acidication liquid outlet 4 and the oxidation; Described acidication liquid outlet 4 is positioned at the bottom in solid accumulation pond, and links up with hydrolyzed solution collecting tank 5, and the reuse inlet 19 of natural pond liquid is equipped with independently valve after described acidication liquid outlet 4 and the oxidation; The top of each elementary cell all is furnished with independently fence cover plate 3, and fixing through standing bolt 2, and each elementary cell all is furnished with independently rain-proof shelter (not shown); The reuse of natural pond liquid inlet 19 is greater than or equal to the installation site of fence cover plate 3 after the described oxidation.
Anaerobic ferment devices is that airtight anaerobic digestion reaction vessel 7, anaerobic digestion reaction vessel 7 bottoms are provided with opening for feed 8, are provided with biogas delivery port 12 at the anaerobic digestion reaction vessel top; Height at anaerobic digestion reaction vessel 0.8~0.9 is provided with natural pond hydrorrhea head piece 9, and natural pond hydrorrhea head piece 9 is furnished with filtration unit 13; Hydrolyzed solution collecting tank 5 is linked up through the fresh feed pump 6 and the opening for feed 8 of anaerobic digestion reaction vessel 7.
Liquid oxidation device in natural pond is liquid oxidation pond, natural pond 14; One end in liquid oxidation pond, natural pond 14 is a natural pond liquid opening for feed, and the other end is an oxidized natural pond liquid discharge port, by the natural pond liquid opening for feed in liquid oxidation pond, natural pond to being provided with the baffling shutter 17 of dislocation up and down the oxidized natural pond liquid discharge port 18; Baffling shutter 17 to liquid oxidation pond, major general natural pond is divided into three oxidation zones; Liquid oxidation pond, natural pond is furnished with oxygen-increasing device 15, and the air outlet of oxygen-increasing device 15 is a micro porous aeration head 16, and described micro porous aeration head is positioned at the bottom of oxidation zone; The natural pond hydrorrhea head piece 9 of described natural pond liquid opening for feed and anaerobic digestion reaction vessel is linked up, and the reuse of natural pond liquid enters the mouth and 19 docks after the oxidation of oxidized natural pond liquid discharge port 18 and acidication liquid 1.
In the present embodiment, the opening for feed 8 of anaerobic digestion reaction vessel 7 is provided with blade agitators 11 apart from reactor bottom 50cm in the anaerobic digestion reaction vessel 7, and the drive-motor 10 of blade agitators 11 is positioned at anaerobic digestion reaction vessel 7 center of top.The oxidation zone that in liquid oxidation pond, natural pond 14, is positioned at natural pond liquid opening for feed one end is first oxidation zone, and at least one micro porous aeration head 16 is positioned at the bottom of first oxidation zone, also can according to practical situation in the bottom of each oxidation zone multiple spot arrange.
In the present embodiment, described acidication reaction tank 1 is made up of the acidication elementary cell of 3 parallel connections, and described baffling shutter 17 is divided into 4 oxidation zones with liquid oxidation pond, natural pond.
In the present embodiment; Described biogas treatment unit is made up of biogas gas holder 20, dehydration tower 21, thionizer 22, biogas supercharger 23; Biogas gas holder 20 is connected with the biogas delivery port 12 of anaerobic digestion reaction vessel 7; Biogas gas holder 20, dehydration tower 21, thionizer 22 are connected with the biogas user by biogas supercharger 23 after being connected in series successively.
During practical implementation, liquid oxidation pond, natural pond 14 degree of depth are no more than 1000mm, and the volume ratio in hydrolysis acidification pool 1, anaerobic digestion reaction vessel 7, liquid oxidation pond, natural pond 14 is 2~5: 1: 0.2~0.5.
During practical implementation; The acidication liquid outlet 4 of described acidication reaction tank 1 is higher than the design liquid level of the maximum hold-up of collecting tank of hydrolyzed solution collecting tank 5; The oxidized natural pond liquid discharge port 18 in liquid oxidation pond, natural pond 14 is higher than the reuse inlet 19 of natural pond liquid after the oxidation of acidication liquid pool 1, relies on waterhead to flow automatically into hydrolysis acidification reaction pond 1.Putting before this, hydrolyzed solution collecting tank 5 can place underground, or acidication liquid 1 all places underground with hydrolyzed solution collecting tank 5.
During practical implementation; Can also all be located at underground with liquid oxidation pond, natural pond 14 described acidication reaction tank 1 or the ground, communicate with each other through pressure pump between the reuse of the natural pond liquid inlet 19 after the oxidized natural pond liquid discharge port 18 in liquid oxidation pond, natural pond 14 and the oxidation of acidication liquid 1.
The operational process of the utility model is: at first be ready to the required anaerobic activated sludge in the required aerobic activated sludge of hydrolysis acidification pool 1 and anaerobically fermenting pond 7; Wherein aerobic activated sludge adopts sewage work's aerobic activated sludge to mix with fresh cow dung that (mass ratio is 5-10: 1); Aeration aerating is subsequent use after two weeks at interval; The biogas residue and biogas liquid that anaerobic activated sludge is then directly gathered the operational excellence biogas engineering gets final product, and add-on is to keep in the reactor drum 7 concentration with 5kgVSm -3About be advisable (being the volatile organic matter that contains in every cubic metre of mixed solution about 5 kilograms); Make this anaerobic activated sludge adapt to pending property of raw material through constantly repeatedly adding the stalk soak solution on a small quantity; Thereby make and form the good particulate state mud (being the good mikrobe cenobium of settling property) of digestic property in the mud; This process be commonly referred to anaerobic fermentation process the unloading phase or the sludge acclimatization stage, the general cycle is 15-45 days.Treat to begin after above-mentioned preparation work finishes in first lattice of hydrolysis acidification pool 1 layering successively and add countryside wastes and aerobic sludge; The amount that adds aerobic activated sludge is according to waste: mud (dry-matter than) is 1: 0.2-0.5 (can decide according to the treatment capacity of countryside wastes); Added material to the 2nd lattice according to identical method in alternate 1~2 day; The interval is 1~2 day again, and the 3rd lattice add material according to identical method ... continue successively in follow-up each lattice, to add materials, until last lattice.Add water logging then and do not soak at least after 1-2 days, open the valve of the acidication outlet 4 of first lattice in the hydrolysis acidification pool 1, hydrolyzed solution is imported in the collecting tank 5; Through lift pump 6 it is pumped into the anaerobic digestion reaction vessel 7 from hydrolyzed solution opening for feed 8 then; Natural pond liquid after digestion finishes simultaneously flows out through natural pond hydrorrhea head piece 9, closes hydrolyzed solution opening for feed 8 and natural pond hydrorrhea head piece 9 after input and output material finishes, and opens the blade stirrer 11 that phonomoter 10 drives; The rotating speed of blade is lower than 30 rev/mins; So that the material thorough mixing in the reactor drum 7, can open phonomoter 2-3 time every day, is no more than 10 minutes at every turn.Open the valve of the hydrolyzed solution water outlet 4 of second lattice in the hydrolysis acidification pool 1; Hydrolyzed solution is imported in the collecting tank 5, through lift pump 6 it is pumped into the anaerobic digestion reaction vessel 7 from hydrolyzed solution opening for feed 8 then, open the valve of natural pond hydrorrhea head piece 9 simultaneously; Natural pond liquid is after natural pond hydrorrhea head piece 9 flows out; By strainer 13 suspended substance removal is fallen the back and flow in the liquid oxidation pond, natural pond 14, after at first passing through oxygen-increasing device 15 (like aeration aerating machine) and micro porous aeration head 16 and carrying out oxygenation, make methanogen residual in the liquid of natural pond contact and be killed with oxygen; And through 17 effects of circuitous baffling shutter, stop reaching after circuitous purify after the purpose subsequent use.And material causes water level to descend owing to a large amount of hydrolyzed solutions are drawn out of in the hydrolysis acidification pool 1; Can open the rain shade at hydrolysis acidification pool 1 top; The waste material that hydrolysis finishes in hydrolysis acidification pool 1 first lattice can adopt manual work or mechanical cleaning to go out (handling through draining), adds a certain amount of countryside wastes, opens the valve between the reuse inlet 19 that purifies liquid outlet 18 of natural pond, back and natural pond liquid then; The natural pond liquid reuse that digestion is finished remedies the demand of water in previous hydrolysis acidification pool 1 first lattice; And therefore natural pond liquid get into and can not produce methane in hydrolysis acidification pool 1 first lattice basically through not having methanogen basically after the oxide treatment early stage here, thereby avoided the methane leakage.It is thus clear that; In entire work process; Have only lattice to be in cleaning in the hydrolysis acidification pool 1 and add materials, lattice are in provides acidication liquid, and other each lattice are in the alternation state of acidication reaction; The acidication liquid of each lattice at interval gets into anaerobic digestion reaction vessel 7 in regular turn in succession, and the natural pond liquid that contains anerobes is introduced the corresponding lattice that just added materials in the hydrolysis acidification pool 1 after handling through liquid oxidation pond, natural pond 14.
Material behind the acidication that each lattice takes out from hydrolysis acidification pool 1 can also continue to be used as fertilizer or matrix raw materials for production, and also can realize natural pond liquid zero release in the total system.
Only importing collecting tank 5 with hydrolysis acidification pool 1 and hydrolyzed solution from above-mentioned and embodiment that realize recycle is underground type; And anaerobic digestion reaction vessel 7 is ground type with liquid oxidation pond, natural pond 14; Mainly be to lean on the liquid gravity gravity flow in the working process; If anaerobic digestion reaction vessel 7, liquid oxidation pond 14, natural pond and hydrolysis acidification pool 1 and hydrolyzed solution import collecting tank 5 and receive environmental restraint, liquid can't be realized flow by gravity in the work, then need increase pressure pump force particular stream that liquid observes the utility model to.

Claims (9)

1. separate type diphasic anaerobic fermentation fermentation unit is characterized in that: comprise acidication reaction unit, anaerobic ferment devices and natural pond liquid oxidation device, wherein:
A) described acidication reaction unit comprises the acidication reaction tank and the hydrolyzed solution collecting tank of the acidication elementary cell of at least two parallel connections; Each elementary cell is open solid accumulation pond; The solid accumulation pond is provided with that the reuse of natural pond liquid enters the mouth after acidication liquid outlet and the oxidation; Described acidication liquid outlet is positioned at the bottom in solid accumulation pond, and links up with the hydrolyzed solution collecting tank, and the reuse inlet of natural pond liquid is equipped with independently valve after described acidication liquid outlet and the oxidation; The top of each elementary cell all is furnished with independently fence cover plate, and each elementary cell all is furnished with independently rain-proof shelter; The reuse of natural pond liquid inlet is greater than or equal to the installation site of fence cover plate after the described oxidation;
B) described anaerobic ferment devices is airtight anaerobic digestion reaction vessel; The anaerobic digestion reaction vessel bottom is provided with opening for feed, is provided with the biogas delivery port at the anaerobic digestion reaction vessel top; Be provided with natural pond hydrorrhea head piece at anaerobic digestion reaction vessel total height 80%-90% place, natural pond hydrorrhea head piece is furnished with filtration unit; The hydrolyzed solution collecting tank is linked up through the opening for feed of fresh feed pump and anaerobic digestion reaction vessel;
C) described natural pond liquid oxidation device is liquid oxidation pond, natural pond; One end in liquid oxidation pond, natural pond is a natural pond liquid opening for feed, and the other end is an oxidized natural pond liquid discharge port, by the natural pond liquid opening for feed in liquid oxidation pond, natural pond to being provided with the baffling shutter of dislocation up and down the liquid discharge port of oxidized natural pond; Baffling shutter to liquid oxidation pond, major general natural pond is divided into three oxidation zones; Liquid oxidation pond, natural pond is furnished with oxygen-increasing device, and the air outlet of oxygen-increasing device is a micro porous aeration head, and described micro porous aeration head is distributed in the bottom of each oxidation zone; The natural pond hydrorrhea head piece of described natural pond liquid opening for feed and anaerobic digestion reaction vessel is linked up, and the reuse of natural pond liquid enters the mouth and docks after the oxidation of oxidized natural pond liquid discharge port and acidication liquid;
D) volume ratio in described hydrolysis acidification pool, anaerobic digestion reaction vessel, liquid oxidation pond, natural pond is 2~5: 1: 0.2~0.5.
2. separate type diphasic anaerobic fermentation fermentation unit according to claim 1, it is characterized in that: the opening for feed of anaerobic digestion reaction vessel is provided with blade agitators apart from reactor bottom 50cm in the anaerobic digestion reaction vessel.
3. separate type diphasic anaerobic fermentation fermentation unit according to claim 1, it is characterized in that: described natural pond liquid oxidation tank depth is no more than 1000mm; The oxidation zone that in natural pond liquid oxidation device, is positioned at natural pond liquid opening for feed one end is first oxidation zone, and at least one micro porous aeration head is positioned at the bottom of first oxidation zone.
4. separate type diphasic anaerobic fermentation fermentation unit according to claim 1, it is characterized in that: described acidication reaction tank is made up of the acidication elementary cell of 2~6 parallel connections.
5. according to the described separate type diphasic anaerobic fermentation of one of claim 1~4 fermentation unit; It is characterized in that: the outlet of the acidication liquid of described acidication reaction tank is higher than the design liquid level of the maximum hold-up of collecting tank of hydrolyzed solution collecting tank, and the oxidized natural pond liquid discharge port in liquid oxidation pond, natural pond is higher than the reuse inlet of natural pond liquid after the oxidation of hydrolysis acidification pool.
6. separate type diphasic anaerobic fermentation fermentation unit according to claim 5, it is characterized in that: described hydrolyzed solution collecting tank places underground.
7. separate type diphasic anaerobic fermentation fermentation unit according to claim 5, it is characterized in that: described acidication liquid places underground.
8. according to the described separate type diphasic anaerobic fermentation of one of claim 1~4 fermentation unit; It is characterized in that: described acidication reaction tank and liquid oxidation pond, natural pond all are located at underground or on the ground, all are furnished with pressure pump between the reuse of the natural pond liquid inlet after the oxidized natural pond liquid discharge port in liquid oxidation pond, natural pond and the oxidation of acidication liquid and communicate with each other.
9. according to the described separate type diphasic anaerobic fermentation of one of claim 1~4 fermentation unit; It is characterized in that: described separate type diphasic anaerobic fermentation fermentation unit also comprises the biogas treatment unit; Described biogas treatment unit is made up of biogas gas holder, dehydration tower, thionizer, biogas supercharger; The biogas gas holder is connected with the biogas delivery port of anaerobic digestion reaction vessel, after biogas gas holder, dehydration tower, thionizer are connected in series successively, is connected with the biogas user by the biogas supercharger.
CN2011201691812U 2011-05-25 2011-05-25 Separate two-phase anaerobic fermentation device Expired - Fee Related CN202107700U (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102260019A (en) * 2011-05-25 2011-11-30 衢州市土肥与农村能源技术推广站 Separated two-phase anaerobic fermentation device
CN105062869A (en) * 2015-07-31 2015-11-18 符放中 Zero-residue biogas fermentation apparatus and application and biogas production method thereof
CN106517714A (en) * 2016-11-30 2017-03-22 四川宏基博业企业管理有限公司 Efficient livestock excrement biogas manure pool

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102260019A (en) * 2011-05-25 2011-11-30 衢州市土肥与农村能源技术推广站 Separated two-phase anaerobic fermentation device
CN105062869A (en) * 2015-07-31 2015-11-18 符放中 Zero-residue biogas fermentation apparatus and application and biogas production method thereof
CN106517714A (en) * 2016-11-30 2017-03-22 四川宏基博业企业管理有限公司 Efficient livestock excrement biogas manure pool
CN106517714B (en) * 2016-11-30 2019-06-18 衢州佳苑牧业有限公司 A kind of efficient feces of livestock and poultry biogas residue-biogas liquid pool

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