CN107417051A - A kind of high temeperature chemistry anaerobic system - Google Patents

A kind of high temeperature chemistry anaerobic system Download PDF

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Publication number
CN107417051A
CN107417051A CN201710828327.1A CN201710828327A CN107417051A CN 107417051 A CN107417051 A CN 107417051A CN 201710828327 A CN201710828327 A CN 201710828327A CN 107417051 A CN107417051 A CN 107417051A
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anaerobic
reactor
outlet
biogas slurry
depth
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何泳良
何梓锋
谭文泷
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Guangzhou Biogas Environmental Protection Science And Technology Co Ltd
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Guangzhou Biogas Environmental Protection Science And Technology Co Ltd
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Priority to CN201710828327.1A priority Critical patent/CN107417051A/en
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/025—Thermal hydrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2833—Anaerobic digestion processes using fluidized bed reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/286—Anaerobic digestion processes including two or more steps
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C02F3/2873—Particular arrangements for anaerobic reactors with internal draft tube circulation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Sludge (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

The invention discloses high temeperature chemistry anaerobic system, for organic waste treatment field, including pretreatment unit, anaerobic device and biogas slurry treatment device, the pretreatment unit includes hydrolysis fluidizing component, lead to the entrance of anaerobic device for the hydrolyzate outlet of hydrolysis fluidizing component, the biogas slurry treatment device includes depth anaerobic reactor, aerobic nitrification reactor and the anaerobic ammonia oxidation reactor being sequentially connected, and the concentrated solution outlet of anaerobic device leads to the entrance of depth anaerobic reactor.The present invention by set hydrolysis fluidizing component significantly reduce discarded object can suspension, and some insoluble COD under common process is converted into the soluble COD for being easy to biochemical, improve the biodegradability of organic matter, also make the more conventional height of factor of created gase of technique；In addition, by using depth anaerobic reactor, aerobic nitrification reactor and anaerobic ammonia oxidation reactor, solves the problems, such as ammonia nitrogen in biogas slurry at low cost using aerobic and anaerobic ammonia oxidation process combination.

Description

A kind of high temeperature chemistry anaerobic system
Technical field
The present invention relates to organic waste treatment field, more particularly to a kind of high temeperature chemistry anaerobic system.
Background technology
Castoff high in containing water includes medicine puree, cultivation excrement, human feces, kitchen garbage, municipal sludge, food industry Sludge etc..At present, the method handled it is generally anaerobic biological.Biogas slurry can be produced after anaerobic biological, and in biogas slurry NH3And influence of the material such as PO to environment is maximum, such as unprocessed discharge, these materials can cause the pollution of environment water. There is the technique handled using anaerobic ammonia oxidation process biogas slurry at present, but universal higher, the Anammoxs of COD in biogas slurry Have certain requirement in process system to the COD of water quality, and in system ANAMMOX (red bacterium) propagation it is also more quick to COD Sense；The less COD considered how in reduction biogas slurry of current anaerobic ammonia oxidation process.
The content of the invention
In order to solve the above problems, the present invention provides a kind of high temeperature chemistry anaerobic system, being capable of low-energy-efficiency, the place of low cost Manage organic waste.
The technical solution adopted in the present invention is：
A kind of high temeperature chemistry anaerobic system, including pretreatment unit, anaerobic device and biogas slurry treatment device, the pretreatment Device includes hydrolysis fluidizing component, and the entrance of anaerobic device, the biogas slurry treatment are led in the hydrolyzate outlet for hydrolyzing fluidizing component Device includes depth anaerobic reactor, aerobic nitrification reactor and the anaerobic ammonia oxidation reactor being sequentially connected, anaerobic device Concentrated solution outlet leads to the entrance of depth anaerobic reactor.
As a further improvement on the present invention, the pretreatment unit also includes homogenate part, the dirt of the homogenate part Hydrolysis fluidizing component is led in slurry outlet.
As a further improvement on the present invention, the homogenate part includes equal stock tank and homogenate tank, and the outlet of equal stock tank is set There is cutting pump, the outlet of cutting pump is provided with feed pump, and the outlet of feed pump connects homogenate tank by pipeline, and the outlet of homogenate tank leads to Piping connection hydrolysis fluidizing component.
As a further improvement on the present invention, the hydrolysis fluidizing component includes fluidized bed body, shell and steam distributor, The fluidized bed body top is provided with overfall, and bottom, which is provided with, lets out mud mouth, and pretreatment unit is provided with the dirty slurry led in fluidized bed body Entrance；Shell is placed on outside fluidized bed body, and spill cavity is formed between shell and fluidized bed body, and housing top end is communicated with spill cavity Ammonia outlet, outer casing bottom is additionally provided with the hydrolyzate outlet for leading to spill cavity, and steam distributor is arranged on fluidized bed body bottom And external water vapour input pipe.
As a further improvement on the present invention, the pretreatment unit also includes release of pressure tower and ammonia crystallizer, the fluidisation The ammonia outlet of bed body leads to ammonia crystallizer, the hydrolyzate outlet release of pressure tower of fluidized bed body, and the outlet of release of pressure tower is detested Oxygen device.
As a further improvement on the present invention, the depth anaerobic reactor have inlet, methane outlet, liquid outlet and Liquid return hole, aeration devices are set in the aerobic nitrification reactor, and the liquid outlet of depth anaerobic reactor leads to aerobic nitrification reaction The entrance of device, the inlet of the anaerobic ammonia oxidation reactor communicate with the liquid outlet of aerobic nitrification reactor, Anammox The liquid outlet of reactor leads to transfer container.
As a further improvement on the present invention, the aerobic nitrification reactor is provided with mud discharging mouth, aerobic nitrification reactor Mud discharging mouth passes to the sludge reflux mouth of depth anaerobic reactor by pipeline and the reflux pump being arranged on pipeline.
As a further improvement on the present invention, it is provided with back between the liquid return hole of the transfer container and depth anaerobic reactor Flow device.
As a further improvement on the present invention, biogas slurry treatment device also includes biogas slurry pond and solid-liquid separator, the solid-liquid Separator has biogas residue outlet, biogas slurry outlet and the suction inlet for leading to biogas slurry pond, and the concentrated solution outlet of anaerobic device passes through pipeline It is passed through in biogas slurry pond, the biogas slurry outlet of solid-liquid separator communicates with the inlet of depth anaerobic reactor.
As a further improvement on the present invention, the depth anaerobic reactor is provided with mud discharging mouth, depth anaerobic reactor The mud discharging mouth of mud discharging mouth and aerobic nitrification reactor is passed in biogas slurry pond after being connected in parallel by pipeline.
The beneficial effects of the invention are as follows：The present invention is by setting hydrolysis fluidizing component to significantly reduce suspending for discarded object Thing (SS), and some insoluble COD under common process is converted into the soluble COD for being easy to biochemical, improve organic matter Biodegradability, also make the more conventional height of factor of created gase of technique；In addition, reacted by using depth anaerobic reactor, aerobic nitrification Device and anaerobic ammonia oxidation reactor, solves ammonia nitrogen in biogas slurry at low cost using aerobic and anaerobic ammonia oxidation process combination Problem.
Brief description of the drawings
The present invention is further described with embodiment below in conjunction with the accompanying drawings.
Fig. 1 is the process principle figure of the present invention；
Fig. 2 is the schematic diagram of pretreatment unit；
Fig. 3 is the schematic diagram for hydrolyzing fluidizing component；
Fig. 4 is the schematic diagram of biogas slurry treatment device.
Embodiment
High temeperature chemistry anaerobic system as shown in Figure 1, including pretreatment unit, anaerobic device 2 and biogas slurry treatment device.In advance Processing unit includes hydrolysis fluidizing component 1, and lead to the entrance of anaerobic device 2 for the hydrolyzate outlet of hydrolysis fluidizing component 1.Hydrolysis stream The effect for changing part 1 is decomposed in the organic matter in acceleration organic waste is made, and is broken organic-matter chemical key, long chain Organic matter becomes the organic matter of short molecular chain, and the material for being partly difficult to decompose in traditional anaerobic reactor is by hydrolysis fluidizing component Become biochemical material after 1 so that the biodegradability of organic waste obtains very big raising, is thus discharged into anaerobic device 2 liquid (hydrolyzate) is relatively easy to handle.The specific configuration of pretreatment unit will be described below.
Above-mentioned biogas slurry treatment device includes depth anaerobic reactor 3, aerobic nitrification reactor 4 and the anaerobism being sequentially connected Ammonia oxidation reactor 5, the concentrated solution outlet of anaerobic device 2 lead to the entrance of depth anaerobic reactor 3, and concentrate (biogas slurry) is arranged Enter depth anaerobic reactor 3.The effect of biogas slurry treatment device is biogas slurry caused by processing system.In embodiment, depth anaerobism Reactor 3 uses anaeration in normal temperature, and biogas slurry becomes dilute biogas slurry, work of dilute biogas slurry in gravity after the processing of depth anaerobic reactor 3 With lower inflow aerobic nitrification reactor 4.Depth anaerobic reactor 3 and aerobic nitrator 4 constitute A/O technique groups Close, for dephosphorization and continue to remove the organic matter in sewage, electron acceptor is provided for follow-up anaerobic ammonia oxidation process；By aerobic Rear biogas slurry flows into anaerobic ammonia oxidation reactor 5, and the advantages of being handled using anaerobic ammonia oxidation process biogas slurry is not Use in the case of biogas slurry carbon source to TN and NH3Removed.
Pretreatment unit is illustrated below.
With reference to referring to figs. 2 and 3 pretreatment unit also includes homogenate part 6, and water is led in the dirty slurry outlet of homogenate part 6 Solve fluidizing component 1.Homogenate part 6 is used for the solid in organic waste by stirring, cutting or other modes are disperseed, And it is easy to the follow-up processing for entering hydrolysis fluidizing component 1 into dirty pulpous state with water mixing.
Homogenate part 6 includes equal stock tank 61 and homogenate tank 62.The equal inside of stock tank 61 is provided with agitating paddle, the outlet of equal stock tank 61 Provided with cutting pump 63, the outlet of cutting pump 63 can also be back to homogenate pond 61 while being provided with feed pump 64 by pipeline, give Expect that the outlet of pump 64 connects homogenate tank 62 by pipeline, the outlet of homogenate tank 62 connects hydrolysis fluidizing component 1 by pipeline.It is organic Discarded object can mix with water in equal stock tank 61, is pre-mixed by agitating paddle 65, export afterwards and in the defeated of cutting pump 63 Send and be homogenised for after stirring；In whipping process, organic waste circulates between equal stock tank 61 and cutting pump 63, organic waste The impurity that thing is brought into is crushed under the repetition cutting of cutting pump 63；Agitated and cutting organic waste is diluted to dirty slurry, The stirring cutting of continuous reflux cycle is starched in dirt, until equal stock tank 61 fills dirty after starching and stirring and terminate, dirt slurry starches feed pump 64 through dirt It is pumped into homogenate tank 62.Agitator also is provided with homogenate tank 62, to keep the uniform of dirty slurry.
The pipeline for connecting homogenate tank 62 and hydrolysis fluidizing component 1 is provided with feed pressure-producing part.Described feed pressurization part Part can be by the input of dirt slurry to hydrolysis fluidizing component 1, while is pressurized to suitable pressure to dirt slurry so that dirt slurry, hydrolysis fluidisation Part 1 has suitable pressure value.Preferable feed pressure-producing part is high-pressure plunger pump 66.
Above-mentioned hydrolysis fluidizing component 1 has hydrolyzate outlet, ammonia outlet 121, dirty slurry entrance 122 and steam inlet, Wherein dirty slurry entrance connection high-pressure plunger pump 66, by the dirty slurry input after homogenate to hydrolysis fluidizing component 1.In hydrolysis fluidizing component In 1, dirt slurry is heated so that the nutrition in dirt slurry is hydrolyzed into the materials such as polysaccharide, organic acid and peptide and enzyme.In protein When being hydrolyzed, nitrogen NH therein4 +It is broken down into unstable free ammonia HN3·H2O (hydration ammonia), unstable is free Ammonia under the action of heat, is further changed to ammonia and discharged by ammonia outlet 121.
Pretreatment unit also includes heat exchanger 17.Heat exchanger 17 is plate type heat exchanger, will hydrolyze the hydrolyzate of fluidizing component 1 Outlet subsequent technique device, while entrance 122 is starched into the outlet dirt of homogenate part.Into the dirt of dirty slurry entrance 122 Slurry can be heated using the heat in hydrolyzate, cost-effective so as to which the system rationally utilizes heat.
Description hydrolysis fluidizing component 1 below.
Hydrolysis fluidizing component 1 includes fluidized bed body 11, shell 12 and steam distributor 13.
The fluidized bed body 11 is that openning shape forms overfall 14 to be container-like, on its top, spill-over in fluidized bed body 11 Hydrolyzate can from overfall 14 to outside flow out.It is provided with the bottom of fluidized bed body 11 and lets out mud mouth, dirt slurry entrance 122 leads to In fluidized bed body 11 and external feed pipe；The feed pipe, which is higher than, lets out the position of mud mouth but also close to the bottom of fluidized bed body 11.
Described steam distributor 13 is arranged on the bottom of fluidized bed body 11, and its steam injection direction is preferably upward and logical Into fluidized bed body 11, the water vapour risen from the bottom to top is formed, steam distributor 13 is defeated by the external water vapour in steam inlet Enter pipe 111, for the water vapour of high pressure-temperature to be imported inside fluidized bed body 11.
Described shell 12 is placed on the outside of fluidized bed body 11 and causes fluidized bed body 11 to be located at middle part, and the roof of shell 12 is with overflowing In the height direction from a distance, the outer wall of shell 12 is with the outer wall of fluidized bed body 11 from a distance so as to shape for head piece 14 Into spill cavity, the hydrolyzate flowed out from overfall 14 can enter in spill cavity.The bottom of shell 12, which is additionally provided with, leads to spill cavity Hydrolyzate exports, for the hydrolyzate in spill cavity to be exported into shell 12.Ammonia outlet 121 is arranged on the top of shell 12 and connection Spill cavity, caused ammonia discharge in hydrolyzing, ammonia outlet 121 is connected to drain valve 123, for controlling the discharge of ammonia.
The process that fluidisation so is hydrolyzed using the hydrolysis fluidizing component 1 is as follows：
Dirt slurry input fluidized bed body 11, now fluidized bed body 11 can be high in high temperature by way of heating pressurization in advance Pressure condition, or can directly input HTHP dirty slurry in the fluidized bed body 11 of closing；The water vapour of high temperature passes through steaming Vapour distributor 13 enters fluidized bed body 11 and dirt slurry is further heated up；The now organic matter meeting accelerated decomposition of dirty slurry, organic materialization Key fracture is learned, the organic matter of long chain is become the organic matter of short molecular chain, partly is difficult to decompose in traditional anaerobic reactor Material obtain very big raising by becoming biochemical material, the biodegradability of dirt slurry after fluidized bed body 11；Part is Hydrolyzate through having decomposed can then cross fluidized bed body 11, and into spill cavity, undecomposed material, can be after because proportion is larger It is continuous to stay in fluidized bed body 11 and decompose；Due to that can become containing ammonia in high-temperature high-pressure state, hydrolyzate partial organic substances and ammonia Gas, these are discharged by ammonia outlet 121, ammonia described ammonia crystallizer 16 arrived after draining into, are crystallized；Operation The indissoluble organic matter in part (cellulose etc.) is had after a period of time and inorganic matter (fixed carbon, stone flour etc.) remains in fluidisation Bed body 11, in order to ensure hydrolysis effect, opened in certain production cycle and let out mud mouth progress spoil disposal.
Above-mentioned process can also be simply summarized as：Dirt slurry enters fluidized bed body 11, wherein lighter suspension is in temperature Upward ascension under being promoted for high temperature and high pressure steam is spent, and overflows fluidized bed body 11, flow direction lets out mud mouth positioned at bottom, and granularity is larger Decline again by steam flush and hydrolysis, so circulation along internal chamber wall with the material of weight；During dirt slurry rises with steam, Steam carries out heat exchange with dirty slurry, and condenses into water and be mixed into dirty slurry.
The principle of said process is as follows：Dirt is starched in the fluid mapper process of device due to being acted on by heating power, in dirt slurry Nutrition is hydrolyzed into the materials such as polysaccharide, organic acid and peptide and enzyme.When protein is hydrolyzed, nitrogen NH therein4 +It is decomposed Into unstable free ammonia HN3·H2O (hydration ammonia), unstable free ammonia under the action of heat, are further changed to ammonia simultaneously Periodically discharged by the air bleeding valve for being located at tower top, the related reaction equation of hydrolytic deaminzation is as follows：
1)、NH4 ++OH-→NH3·H2O
2)、NH3·H2O→NH3↑+H2O
Making hydrolysis of organic matter acidifying by pyrohydrolysis, high-temperature water vapor can be used as solid-state in this embodiment into hydrolyzate Organic matter fluidizing gas and NH3Stripping gas, while be also hydrolysis temperature offer media.High-temperature water vapor is also high pressure, To maintain the pressure in fluidized bed body 11,120~190 DEG C are warming up to the dirty slurry in fluidized bed body 11.
Above-mentioned heat exchanger 17 has interconnected cold import, heat outlet and interconnected hot import, cold outlet. Wherein, homogenate tank 62 is led in the dirty slurry entrance 122 of the hot outlet of heat exchanger 17, cold import, and the hot import of heat exchanger 17 passes through The outlet of pipeline connection hydrolyzate, release of pressure tower 15 discussed below is led in cold outlet.
Above-mentioned high-pressure plunger pump 66 is used to after dirt slurry is forced into suitable pressure value input in fluidized bed body 11, makes stream Change bed body 11 " default " pressure.
Dirt slurry is forced into 0.5~1.5Mpa by high-pressure plunger pump 66, subsequently into heat exchanger 17, to fluidize pyrohydrolysis Pyrohydrolysis liquid afterwards preheats dirty slurry to 100~150 DEG C as thermal source；Carried out afterwards according to above-mentioned hydrolytic process；By water Hydrolyzate after solution enters the row of heat exchanger 17 cooling (heat is used to preheat newly to enter dirty slurry), and temperature is down to outside 40~60 DEG C and delivered to Subsequent technique.
In above-mentioned implementation, with reference to above-mentioned reaction equation 2：NH4 ++OH-→NH3·H2O, the formula is reversible, in pH value For in 4.5-5.8 sour environment, for hydrolysis temperature when declining, free ammonia, which can be reacted to ammonium again, rises hydrolyzate pH, Such as formulas below 3：
3)、NH3·H2O→NH4 ++OH-
According to formula reaction equation 1), 2), 3) understand, dirt slurry in ammonium emission be can by adjust acid-base value realize, ammonia Precipitation and dissolved oxygen amount (DO), the hydrolysis temperature of hydrolyzate it is closely related.Hydrogen-oxygen is so proportionally added into before booster plunger pump Change effective control that sodium solution changes the acid-base value of dirty slurry and controls hydrolysis temperature that hydrolyzate ammonia nitrogen can be achieved, pH should be adjusted To 5.8-6.8 faintly acid.
Pretreatment unit also includes release of pressure tower 15 and ammonia crystallizer 16.
The entrance of described release of pressure tower 15 is communicated by pipeline with the hydrolyzate outlet of fluidized bed body 11, to receive hydrolysis stream Change the hydrolyzate that part 1 is discharged.Because hydrolyzate out has certain pressure, the release of pressure tower 15 can be by hydrolyzate Pressure is discharged, while plays a part of temporary hydrolyzate, and buffer time and maintenance time are provided for subsequent technique.It is specific next Say, the top of release of pressure tower 15 is provided with a shower nozzle 151, and hydrolyzate is passed through in shower nozzle 151 to spray into the inner chamber of release of pressure tower 15, release of pressure tower 15 hydrolyzate is discharged from bottom.
The ammonia outlet 121 of fluidizing component 1 is hydrolyzed by pipeline communication ammonia crystallizer 16, valve is additionally provided with the pipeline, Periodically to be discharged.Ammonia crystallizer 16 is container-like, injection sulfuric acid in it, ammonia and sulfuric acid reaction generation ammonium sulfate, its Chemical equation is as follows：
2NH3+H2SO4→NH42SO4。
It can be dried after being arranged outside the ammonium sulfate of generation, make fertilizer.
Release of pressure tower 15 is provided with gas vent at top, and the gas vent leads to ammonia crystallizer 16.Institute's shape after hydrolyzate volatilization Into gas also contain ammonia, form solid-state so as to being together discharged into ammonia crystallizer 16.
The top of homogenate tank 62 is provided with the exhaust outlet 621 for leading to ammonia crystallizer 16, to the ammonia that will be volatilized in homogenate tank 62 Discharged Deng gas.The bottom of homogenate tank 62 is provided with mud discharging mouth, and impurity, residue are discharged.Mud discharging mouth is connected with letting out mud mouth by discharge pipeline Logical, the bottom ash of discharge can be transported outward, or for being dried to fertilizer.
Release of pressure tower 15 is provided with liquid outlet in bottom, and liquid outlet is connected to discharging tube, and the discharging tube can be passed through anaerobism dress In putting 2, and backflow part 152 is provided between anaerobic device 2 and homogenate part 6, for example is reflux pump, backflow part 152 will The hydrolyzate that release of pressure tower 15 is discharged is back to homogenate part 6, as dilution organic waste.
Hydrolyzate BOD after above pretreatment unit and technique synchronous with COD indexs will not decline, in hydrolyzate TN and NH3It is changed into adjustable index etc. index, so as to greatly strengthen the biodegradability of organic waste.
Anaerobic device 2 in embodiment is CSTR (continuously stirred tank reactor (CSTR)), also known as complete mixing flow reactor, its work Principle is to carry out eliminating organic pollutant by anaerobic activated sludge in digester.Generally, medium temperature CSTR anaerobic techniques Hydraulic detention time is 32 days, and the hydrolysis time of suspension is about 10d-15d in sewage, and acidificatoin time is about 4h, and anaerobic bacteria produces Gas peak period is about in 15d.Organic waste by techniques such as hydrolysis acidifications due to being pre-processed in embodiment, in order to subtract Few investment, the effect of anaerobic technique is improved, embodiment uses high temperature CSTR anaerobic techniques, and hydraulic detention time is about 15d.
Hydrolyzate is entered in CSTR tanks by release of pressure tower 15 through pipeline, is entered by stirring with original anaerobic activated sludge in pond Row sufficiently contact.The metabolic conversion that organic matter in hydrolyzate passes through methane backeria is biogas, and hydrolyzate is mixed into sludge Thick biogas slurry containing certain solid matter.
Biogas slurry treatment device is illustrated below.
With reference to figure 4, and Fig. 1-Fig. 3 is combined, depth anaerobic reactor 3 is multistage depth anaerobic reactor, also referred to as IC anaerobism Reactor, it has inlet, methane outlet, liquid outlet and liquid return hole, and three-phase is additionally provided with the top of depth anaerobic reactor 3 Separator.Depth anaerobic reactor 3 is a kind of efficient multistage inner circulation reactor, compared to former traditional anaerobic reactor, it With take up an area less, organic loading is high, impact resistance is stronger, performance is more stable, operational administrative is simpler.When processing COD is During high concentrated organic wastewater during 10000-15000mg/L, traditional general volumetric loading of anaerobic reactor is 5-8kgCOD/m3； IC anaerobic reactor volumetric loading rates are up to 15-30kgCOD/m3。
Aeration devices 41 are set in described aerobic nitrification reactor 4, aeration devices 41 are located at bottom, can be densely covered with it is micro- The aeration tube in hole, aeration tube are connected with the air compressor 43 of outside by pipeline.The top of depth anaerobic reactor 3 goes out liquid Mouth leads to the entrance of the bottom of aerobic nitrification reactor 4 by way of flow by gravity.
Described anaerobic ammonia oxidation reactor 5, its inlet communicate with the liquid outlet of aerobic nitrification reactor 4, to receive Biogas slurry after aerobic nitrification.The liquid outlet of anaerobic ammonia oxidation reactor 5 leads to transfer container 51.
Above-mentioned depth anaerobic reactor 3 uses anaeration in normal temperature, hydrolyzate (biogas slurry) warp after the processing of anaerobic device 2 Cross after depth anaerobic reactor 3 handles, biogas caused by anaerobic processes is by being located at the three phase separator gas collection of reactor head Area discharges through pipeline, as subsequent technique；
The dilute biogas slurry treated by depth anaerobic technique, aerobic nitrification reactor 4 is flowed under gravity.Depth Anaerobic reactor 3 and aerobic nitrator 4 constitute A/O process combination, for dephosphorization and continue to remove in sewage Organic matter, provide electron acceptor for follow-up anaerobic ammonia oxidation process；
Biogas slurry after aerobic flows into anaerobic ammonia oxidation reactor 5, using anaerobic ammonia oxidation process to biogas slurry at The advantages of reason, is in the case of without using biogas slurry carbon source to TN and NH3Removed.
In above process, biogas slurry sprays the oxygen in air with aeration tube and fully contacted, and oxygen is in aerobic nitrification device Play a part of as follows：
1), to NH4 +Carry out oxidation generation nitrite NO2 -, electron acceptor is provided for anaerobic ammonia oxidation process；
2), aerobic nitrification reactor 4 forms the solid phosphorus techniques of A/O with depth anaerobic reactor 3；
3), effect of the oxygen in aerobic nitrification reactor 4 also includes further removing organic matter and the increase in sewage The dissolved oxygen (DO) of sewage.
In addition, the combination of depth anaerobic reactor 3, anaerobic ammonia oxidation reactor 5 and aerobic nitrification reactor 4 can also regard Make with A/O dephosphorization technology.
Above-mentioned aerobic nitrification reactor 4 is provided with the mud discharging mouth positioned at bottom, and the mud discharging mouth of aerobic nitrification reactor 4 passes through Pipeline and the reflux pump 42 being arranged on pipeline pass to the sludge reflux mouth of depth anaerobic reactor 3.
Biogas slurry treatment device also includes biogas slurry pond 7 and solid-liquid separator 8, and the concentrated solution outlet of anaerobic device 2 passes through pipeline It is passed through in biogas slurry pond 7, the biogas slurry outlet of solid-liquid separator 8 communicates with the inlet of depth anaerobic reactor 3.
Specifically, the bottom of depth anaerobic reactor 3 is also provided with mud discharging mouth, the mud discharging mouth of depth anaerobic reactor 3 with it is good The mud discharging mouth of oxygen nitrator 4 is passed to after being connected in parallel by pipeline in the biogas slurry pond 7 for adding original biogas slurry.It is corresponding , corresponding valve is set on pipeline, and to control spoil disposal, while it is row that valve, which can also control the spoil disposal of aerobic nitrator 4, Into depth anaerobic reactor 3 or biogas slurry pond 7.
The biogas slurry outlet that solid-liquid separator 8 has biogas residue outlet, leads to the suction inlet in biogas slurry pond 7 and lead to filtering pond 71. The solid-liquid separator 8 is spiral dewaterer, and the charging aperture of the spiral dewaterer connects biogas slurry pond 7 as suction inlet by pipeline In, elevator pump is set between spiral dewaterer and biogas slurry pond 7, can by thick biogas slurry, from the mud discharging mouth of aerobic nitrification reactor 4 The sludge of discharge, the sludge from the discharge of the mud discharging mouth of depth anaerobic reactor 3 input and separation of solid and liquid are carried out into spiral dewaterer；Spiral shell The discharging opening for revolving dewaterer forms biogas residue outlet, and biogas residue outlet with external pipe and can be led to and drying device (not shown), warp After crossing separation of solid and liquid, inorganic matter, fixed carbon in thick biogas slurry and the bulky grain organic matter not being hydrolyzed are trapped, and are sent to organic Fertile production technology is handled.
The liquid outlet of spiral dewaterer forms biogas slurry outlet, and biogas slurry outlet is led in filtering pond 71 by pipeline, given afterwards Biogas slurry in filtering pond 71 is promoted to the inlet of depth anaerobic reactor 3 by material pump 72.
The lettuce inputted from filtering pond 71 to depth anaerobic reactor 3 sometimes may be higher, and is unfavorable for detesting Oxygen reacts, and is that this can be in the relatively low liquid of the other input concentration in the bottom of depth anaerobic reactor 3 (water etc.), to dilute biogas slurry Concentration.
Depth anaerobic reactor 3 is provided with liquid return hole, and refluxing unit 52 is provided between transfer container 51 and liquid return hole, processing During the reclaimed water that has handled anaerobic ammonia oxidation reactor 5 of refluxing unit 52 carry out reuse, use water so as to save.In addition, Reclaimed water in transfer container 51 is also used as the approach such as long-term irrigation.
The methane outlet of depth anaerobic reactor 3 is connected to by pipeline and generating equipment (not shown), connects generating equipment Back-fire relief water seal 31 is provided with the pipeline of methane outlet.
In order to strengthen the ammonia nitrogen removal efficiency of anaerobic ammonia oxidation reactor 5, filler is set as ANAMMOX in reactor The bacterium bed of (red bacterium).The principle of anaerobic ammonia oxidation process belongs to any technique commonly known, is no longer to be retouched in detail in this embodiment State.
In embodiment, initially entering the biogas slurry in biogas slurry pond 7 needs to carry out the regulation of ammonia nitrogen, so that follow-up depth anaerobism tool Standby feasibility, the regulation of the ammonia nitrogen are realized by pretreatment unit.
Contain polyP bacteria in the sludge of aerobic nitrification reactor 4, can be cultivated in the reactor in advance, can also The sludge for having cultivated polyP bacteria is directly injected into reactor.After biogas slurry in aerobic nitrification reactor 4 enters aerobic state, PolyP bacteria is stored in internal PHB and carries out aerobic decomposition and discharge big energy, and these energy parts are rised in value for polyP bacteria, portion It is allocated as in the form of poly- phosphorus gathering in polyP bacteria body for the phosphatic energy in its active absorption biogas slurry, phosphate；Aerobic dirt Substantial amounts of polyP bacteria is included in mud, may be reached by the discharge of sludge and remove phosphatic purpose.
PolyP bacteria is also contained by the sludge discharged in aerobic nitrification reactor 4, then under the mode of backflow, be back to Also contain polyP bacteria in the sludge of depth anaerobic reactor 3 so that depth anaerobic reactor 3 can also realize the purpose of dephosphorization.
The anaerobic system of above example generally speaking has the following advantages that：
1), hydrolyzed using fluidisation, significantly reduce slurries can suspension (SS), and make some insoluble under conventional skill Property COD be converted into the soluble COD for being easy to biochemical, make the more conventional height of factor of created gase of technique.
2) saturation degree and pH of ammonium, are adjusted by adding NaOH, allows the process combination such as high temperature and steam stripping to refer to ammonia nitrogen Mark adjustable, enhance the biodegradability of hydrolyzate.
3) the use of depth anaerobic technique and aeration aerobic process is, that phosphorus is cured in biogas residue, and turns into organic fertilizer.
4), solves the problems, such as ammonia nitrogen in biogas slurry at low cost using aerobic and anaerobic ammonia oxidation process combination.
5), by fluidizing hydrolysis process, controllable artificial hydrolysis and acidifying is realized, reduces slurries to greatest extent Hydraulic detention time, in the case where increasing gas production, reduce the investment of anaerobic system.
The simply preferred embodiment of the present invention described above, it does not form limiting the scope of the invention.

Claims (10)

  1. A kind of 1. high temeperature chemistry anaerobic system, it is characterised in that：Filled including pretreatment unit, anaerobic device (2) and biogas slurry treatment Put, the pretreatment unit includes hydrolysis fluidizing component (1), and anaerobic device is led in the hydrolyzate outlet of hydrolysis fluidizing component (1) (2) entrance, the biogas slurry treatment device include be sequentially connected depth anaerobic reactor (3), aerobic nitrification reactor (4) and Anaerobic ammonia oxidation reactor (5), the concentrated solution outlet of anaerobic device (2) lead to the entrance of depth anaerobic reactor (3).
  2. 2. high temeperature chemistry anaerobic system according to claim 1, it is characterised in that：The pretreatment unit also includes homogenate Hydrolysis fluidizing component (1) is led in part (6), the dirty slurry outlet of the homogenate part (6).
  3. 3. high temeperature chemistry anaerobic system according to claim 2, it is characterised in that：The homogenate part (6) includes homogenate Pond (61) and homogenate tank (62), the outlet of equal stock tank (61) are provided with cutting pump (63), and the outlet of cutting pump (63) is provided with feed pump (64), the outlet of feed pump (64) connects homogenate tank (62) by pipeline, and the outlet of homogenate tank (62) is connected by pipeline to be hydrolyzed Fluidizing component (1).
  4. 4. high temeperature chemistry anaerobic system according to claim 1, it is characterised in that：The hydrolysis fluidizing component (1) includes Fluidized bed body (11), shell (12) and steam distributor (13), fluidized bed body (11) top are provided with overfall (14), bottom Provided with mud mouth is let out, pretreatment unit is provided with the dirty slurry entrance led in fluidized bed body (11)；Shell (12) is placed on fluidized bed body (11) it is outside, spill cavity is formed between shell (12) and fluidized bed body (11), shell (12) top is communicated with the ammonia of spill cavity Gas exports (121), and shell (12) bottom is additionally provided with the hydrolyzate outlet for leading to spill cavity, and steam distributor (13) is arranged on fluidisation Bed body (11) bottom and external water vapour input pipe (111).
  5. 5. high temeperature chemistry anaerobic system according to claim 4, it is characterised in that：The pretreatment unit also includes release of pressure Tower (15) and ammonia crystallizer (16), the ammonia outlet (121) of the fluidized bed body (11) lead to ammonia crystallizer (16), fluidized bed body (11) hydrolyzate outlet release of pressure tower (15), the outlet anaerobic device (2) of release of pressure tower (15).
  6. 6. high temeperature chemistry anaerobic system according to any one of claim 1 to 5, it is characterised in that：The depth anaerobism Reactor (3) has inlet, methane outlet, liquid outlet and liquid return hole, and aeration devices are set in the aerobic nitrification reactor (4) (41), the liquid outlet of depth anaerobic reactor (3) leads to the entrance of aerobic nitrification reactor (4), the Anammox reaction The inlet of device (5) communicates with the liquid outlet of aerobic nitrification reactor (4), and the liquid outlet of anaerobic ammonia oxidation reactor (5) leads to Transfer container (51).
  7. 7. high temeperature chemistry anaerobic system according to claim 6, it is characterised in that：The aerobic nitrification reactor (4) sets There is mud discharging mouth, the mud discharging mouth of aerobic nitrification reactor (4) passes to depth by pipeline and the reflux pump (42) being arranged on pipeline The sludge reflux mouth of anaerobic reactor (3).
  8. 8. high temeperature chemistry anaerobic system according to claim 6, it is characterised in that：The transfer container (51) is detested with depth Refluxing unit (52) is provided between the liquid return hole of oxygen reactor (3).
  9. 9. high temeperature chemistry anaerobic system according to claim 6, it is characterised in that：Biogas slurry treatment device also includes biogas slurry pond (7) and solid-liquid separator (8), the solid-liquid separator (8) have biogas residue outlet, biogas slurry outlet and the suction for leading to biogas slurry pond (7) Entrance, the concentrated solution outlet of anaerobic device (2) are passed through in biogas slurry pond (7) by pipeline, the outlet of the biogas slurry of solid-liquid separator (8) with The inlet of depth anaerobic reactor (3) communicates.
  10. 10. high temeperature chemistry anaerobic system according to claim 9, it is characterised in that：The depth anaerobic reactor (3) sets There is mud discharging mouth, the mud discharging mouth of the mud discharging mouth and aerobic nitrification reactor (4) of depth anaerobic reactor (3) is connected in parallel by pipeline After pass in biogas slurry pond (7).
CN201710828327.1A 2017-09-14 2017-09-14 A kind of high temeperature chemistry anaerobic system Pending CN107417051A (en)

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KR20050006347A (en) * 2003-07-08 2005-01-17 한국건설기술연구원 BNR(Biological Nutrient Removal) system and method by organic acids generated from sewage sludge
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CN101985381A (en) * 2010-09-29 2011-03-16 天津大学 Integrated treating device and method of fuel ethanol distillation wastewater of corn straw and high ammonia nitrogen pretreatment wastewater
CN102351386A (en) * 2011-09-15 2012-02-15 吉化集团公司 Potato type ethanol wastewater treatment method and system
CN104944732A (en) * 2015-06-29 2015-09-30 同济大学 Energy-saving recycling treatment disposal system and energy-saving recycling treatment disposal process for organic solid waste
CN105906155A (en) * 2016-06-14 2016-08-31 上海澄华环境工程有限公司 Wastewater treating process capable of reducing sludge quantity
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CN101050026A (en) * 2007-04-17 2007-10-10 北京市环境保护科学研究院 Deepness denitrogenation method for treating organic wastewater in high concentration
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