CN106007235A - Method for efficiently treating plant protein wastewater - Google Patents
Method for efficiently treating plant protein wastewater Download PDFInfo
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- CN106007235A CN106007235A CN201610576937.2A CN201610576937A CN106007235A CN 106007235 A CN106007235 A CN 106007235A CN 201610576937 A CN201610576937 A CN 201610576937A CN 106007235 A CN106007235 A CN 106007235A
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Abstract
The invention discloses a method for efficiently treating plant protein wastewater, and belongs to the field of protein wastewater treatment. The method includes 'multistage pre-treatment, efficient anaerobic, anoxia and aerobic' combined technologies, so that efficient anaerobic treatment, stable running and recycling can be carried out on the plant protein wastewater. A 'multistage pre-treatment technology' mainly includes physiochemical per-treatment and biochemical pre-treatment; suspended particles in the plant protein wastewater can be efficiently intercepted by the aid of the physiochemical pre-treatment, and bean pulp resources in the plant protein wastewater can be recycled by the aid of the physiochemical pre-treatment; protein can be destructed by the aid of the biochemical pre-treatment, calcium ions and phosphate radicals can be intercepted by the aid of the biochemical pre-treatment, and anaerobic disturbance influence factors can be eliminated; the pH (potential of hydrogen) and the temperature of inlet water can be reasonably controlled by efficient anaerobic units, accordingly, anaerobic systems can assuredly efficiently and stably run, and the volume load of the anaerobic systems can reach 25 kg/(m<3>.d). Compared with the traditional processes and technologies for plant protein wastewater, the technical method has the advantages of high efficiency, stability, high resource utilization rate and the like. Besides, the plant protein wastewater can be efficiently treated by the aid of the method.
Description
Technical field
The invention belongs to protide field of waste water treatment, more particularly, it relates to a kind of vegetable protein waste water high-efficiency processing method.
Background technology
Soybean protein is a kind of important vegetable protein, owing to it contains abundant nutrient protein composition, adds at various food at present
Industrial and commercial bank's industry is widely used.China's soybean protein isolate produces and starts late, the separation protein production being constructed and put into operation
Family of producer more than 60, is mainly distributed on the areas such as Shandong, Henan, Hebei and three provinces in the northeast of China, and China's soybean protein annual production is about
1000000 tons, export volume accounts for more than half of the value of international trade.At present, domestic soybean protein production technology is mainly " the molten acid of alkali
Heavy method ", as shown in Figure 2, soybean protein production process can produce substantial amounts of waste water, mainly include raw material process water,
Bean clear water, equipment cleaning water and product overflowing liquid etc..According to statistics, often produce 1 ton of soybean protein and can produce 40 tons of whey wastewaters.
In soy protein wastewater, major pollutants are the Organic substance of high concentration, oligosaccharide, carbohydrate and inorganic salts, generally
In water quality, CODcr is up to more than 20000mg/L, and float is up to more than 5000mg/L.From practical operating experiences and waste water
Water analysis understands, and the feature of soy protein wastewater is that content of organics is high, and water quality and quantity changes greatly, rushes waste water disposal facility
Hitting property is big.But its wastewater biodegradability is preferably (B/C > 0.4), and waste water Middle nutrition element (N, P) content is high.Vegetable protein
Waste water has following characteristics: (1) protein content is high: this is that protein Process self causes, in conventional soybean protein production technology
After " alkali extraction and acid precipitation ", the most remaining substantial amounts of protein substance in water, this situation not only wastes substantial amounts of raw material, and gives
Subsequent wastewater treatment adds difficulty.(2) pH shock-absorbing capacity is strong: in soybean protein production technology after " alkali extraction and acid precipitation ", water
The protein substance soda acid shock-absorbing capacity of middle remnants is relatively strong, can obtain electronics at acid solution, alkalescence condition can be with betatopic, therefore,
If on the premise of not removing this Partial Protein, only rely on and add acid or alkali, want that it is to be stranded very much that water quality pH is adjusted to neutrality
Difficult, not only needing to consume substantial amounts of acid or alkali, and water quality pH after mixing well is unstable, change pH over time is still
Can change therewith.(3) SS content is high: remains substantial amounts of bean cake residue in proteinic wastewater, is had without at materialization unit
The removal of effect, then these float are difficult to be degraded by microorganisms in biochemical unit, and these float are in biochemical system simultaneously
Granule sludge surface, plugging particle mud mass transfer duct can be attached to, cause mud dead or village hollowing, or at water project situation
Under, particle may produce a certain degree of shear action to granule sludge, causes sludge decomposition or broken.Proteinic wastewater by
Higher in protein content, water quality is obvious from acidifying, is being easily caused the change of pH, and then impact during acidifying
The water solublity of albumen, therefore proteinic wastewater change over time, its SS content is also in constantly fluctuation, and conventional physicochemical techniques does not has
Having consideration water quality from change, therefore SS clearance is the highest.(4) defoamer: the particularity of proteinic wastewater causes centrifugal process
The substantial amounts of foam of middle generation, generally requires in production process and adds substantial amounts of defoamer.
Soybean protein enterprise generally uses " coagulation air-float+anaerobic bio-treated+Aerobic biological process+advanced treating " technique to carry out
Waste water processes.But generally there is anaerobic system in industry and be difficult to the technical barrier that efficient stable runs, existing anaerobic unit granule
Sludge decomposition phenomenon is serious, and with a large amount of fine particle mud in water outlet, anaerobic system cannot realize granule sludge propagation, cycle
Property adds granule sludge, brings huge cost of sewage disposal to protein production enterprise, even inhibits production-scale continuous expansion
Greatly.The most once process to proteinic wastewater of other institutes of many colleges and universities such as Shandong University, Tsing-Hua University launched research work, but
Theoretical discovery does not the most obtain guardian technique breakthrough, in soy protein wastewater processing procedure in industry with engineering practice field
The problems such as the air flotation effect generally existed is the best, anaerobic system volumetric loading is relatively low, granule sludge needs are periodically added, and
Face in industry and carry mark, the technical barrier of transformation, though this skilled person knows current technical problem at present, but do not have
See clearly the basic reason causing this technical problem completely, so also without the solution of being found for property of way, the most common
Albumen wastewater treatment patented technology be concentrated mainly on Optimizing Reconstruction (the soy protein wastewater processing means of anaerobic reaction device itself
And processing method, CN201510095066.8；Anaerobic methane production Anammox Combined Treatment soy protein wastewater device and side
Method, CN201410454215.0；A kind of novel high-efficiency anaerobic treatment device for soybean protein wastewater, CN201110444751.9),
These patented technologies are all merely resting on how anaerobic reactor transforms aspect, are not involved with the solution of root problem, because of
This can not solve the practical problem in industry, and those skilled in the art lack the overall assurance to albumen wastewater treatment technique and emphasis
Capture, still there is no corresponding patented technology by selecting rational method to solve current albumen industry field of waste water treatment generally
Technical barrier.
Summary of the invention
Problem to be solved
Present in existing vegetable protein wastewater treatment process: 1) surface loading of air flotation cell can not meet the requirements, Chang Hui
Being affected greatly by water variation water quality, water outlet SS is the most higher；2) anaerobic system is relatively big by air supporting effluent quality influence of fluctuations,
The particularly SS of high concentration；3) anaerobic system total hrt is the longest, organic volumetric loading and unit volume aerogenesis
Rate is on the low side；4) anaerobic unit granule sludge disintegration is serious, and with a large amount of fine particle mud in water outlet, anaerobic system cannot
Realizing the technical barriers such as granule sludge propagation, the present invention provides a kind of vegetable protein waste water high-efficiency processing method, uses " multistage pre-
Process+efficient anaerobic+anoxia+aerobic " process integration, it is achieved efficient anaerobic process, stable operation and the money of vegetable protein waste water
Source.
2. technical scheme
In order to solve the problems referred to above, the technical solution adopted in the present invention is as follows:
A kind of vegetable protein waste water high-efficiency processing method, the steps include:
(A) waste water enters flotation tank, adds aluminium polychlorid and polyacrylamide, carry out aeration agitation, air supporting in flotation tank
Scum silica frost in pond reclaims through filter-pressing device, and filtrate is back to flotation tank；
(B) in step (A), the water outlet of flotation tank enters coagulation unit, and coagulation unit includes coagulation reaction tank and coagulative precipitation tank,
Adding poly-ferric chloride and polyacrylamide in coagulation reaction tank, coagulation reaction tank water outlet enters coagulative precipitation tank, and precipitate refluxes
To flotation tank, coagulative precipitation tank water outlet enters next processing unit；
(C) in step (B), coagulation unit sedimentation tank water outlet carries out strenuous primary treatment through biochemical pretreatment reaction unit, makes to give up
Water is more conducive to the efficient process of anaerobic unit；
(D) water outlet of step (C) mesophytization pretreatment reaction unit is caused anaerobic unit and carry out anaerobic reaction；Anaerobism is intake
PH regulator on the one hand reflux by anaerobic effluent, another aspect is by adding sodium hydroxide or hydrochloric acid；
(E) anaerobic unit water outlet in step (D) is caused " anoxia+aerobic " unit, regulates influent quality by backflow,
Realize the removal of efficient denitrification denitrification and COD.
Preferably, in step (A), the reflux ratio of flotation tank is set to 80%, and in flotation tank, the dosage of aluminium polychlorid is
50～1000mg/L, the dosage of polyacrylamide is 1～20mg/L.
Preferably, in step (B), in coagulation unit process pond, the dosage of poly-ferric chloride is 50～300mg/L, polyacrylamide
The dosage of amine is 1～20mg/L, and coagulation water part is back to air flotation cell, and capacity of returns is 0～80%..
Preferably, the concrete grammar of the biochemical pretreatment mentioned in step (C) is to use hydrolyzing sludge to be entered by the albumen in waste water
Row hydrolysis, it is achieved that the destruction of albumen, realizes retaining of calcium ion and phosphate radical by sludge absorption effect simultaneously, and this unit stops
Staying the time is 2～24h, controls dissolved oxygen by hydraulic mixing and eliminates produce anaerobism in below 0.5mg/L, biochemistry pretreatment
The influence factor of interference, makes biochemical pretreated water outlet be easier to follow-up anaerobic unit.
Preferably, the anaerobic unit used in step (D) is the EGSB reactor come into the open, and filler is granule sludge, detests
Oxygen effluent recycling ratio is 2～10 times, and anaerobism inlet flow-patterm regulates to 5～7.
Preferably, for regulating the solution that sodium hydroxide is 1%～10% (mass fraction) of pH in step (D), described
Hydrochloric acid is the hydrochloric acid of 1%～36% (mass fraction).
Preferably, aerobic unit used in step (E) is A/O technique.
The present invention first passes through and analyzes the basic reason causing anaerobic system to be difficult to stable operation, is then designed by creative unit
And process combination optimization, by " materialized pretreatment+biochemistry strenuous primary treatment+efficient anaerobic+aerobic " process integration, it is achieved that
Vegetable protein waste water stable, efficiently process, provide foundation for scientific theory research and projectsization application.Technology in the industry
Personnel do not recognize the key reason of technical problem, and therefore its operational means does not has specific aim, it is impossible to solve root problem, yet
Can not have motivation selects similar process combination to realize technique effect；It addition, take to be similar to even by random combine
The application of group technology, also cannot be selected by crucial technological parameter, realize the present invention and can be obtained with beneficial effect, and
And, it is believed that key technology and key parameter that this patent is mentioned are required to the base in the basic reason fully understanding technical barrier
On plinth, could be obtained by the analysis of science and fully practice.
By analyzing with the presence of some conclusion above: (1) vegetable protein field of waste water treatment anaerobic system is difficult to the skill of stable operation
An art difficult problem；(2) current techniques personnel are not fully apparent from the basic reason of this technical problem；(3) current technological means mostly is
Anaerobic reactor designs, and considers not over entirety, does not solve this technical barrier；(4) the combination work that the technology of the present invention is mentioned
Skill is on the basis of the basic reason of the difficult problem that fully masters a skill, the most getable by scientific analysis and test of many times test,
The process integration of the present invention is not the simple combination of existing technique, but from basic reason, emphasis is in pretreatment and anaerobism section
Realize overall coordination effect, be specific to the process technique of vegetable protein waste water design, be not that Conventional waste water roadmap can
Realize, the technique of the present invention be not according to conventional treatment thinking it is conceivable that；(5) in the technical method that the present invention mentions,
The selection of many key parameters selects have bigger difference with the parameter of conventional treatment process, this think of selected mainly due to parameter
Road is different with method, and those of ordinary skill is to be difficult to simply obtained in the industry, and the selection of these process combination key parameters sets
Surely solve current technical barrier, achieve unexpected effect, it is achieved that each process section, the overall coordination of each technological parameter are made
With, there is significant beneficial effect.
3. beneficial effect
Compared to prior art, the invention have the benefit that
(1) a kind of vegetable protein waste water high-efficiency processing method of the present invention, the coagulation process backflow in three grades of pretreatment, decrease
The process load of air flotation cell, improves SS clearance, and additionally biochemical pretreatment also can change wastewater pH bar by hydrolysis
Part, promotes dissolving and the destruction of suspension albumen, reduces SS content further, effectively solves air flotation cell SS and removes halfway
Technological difficulties, can be reduced to below 1000mg/L by materialization water outlet SS content, enhance the efficiency of materialized pretreatment；
(2) a kind of vegetable protein waste water high-efficiency processing method of the present invention, by biochemical pretreatment, carries out sufficient water by albumen
Solution becomes ammonia nitrogen, it is achieved that retaining of the destruction of albumen, calcium ion and phosphate radical, alleviates the water inlet fluctuation of anaerobic unit, will detest
The unfavorable factor of oxygen process all controls at biochemical pretreatment unit；
(3) a kind of vegetable protein waste water high-efficiency processing method of the present invention, increases anaerobic effluent reflux ratio, regulation anaerobism water inlet
PH, overcomes traditional anaerobic system volumetric loading present in the albumen wastewater treatment process the highest, and COD degradation rate is on the low side
Technical barrier；
(4) a kind of vegetable protein waste water high-efficiency processing method of the present invention, use series pretreatment, including materialized pretreatment,
Biochemical pretreatment, overcomes anaerobic unit granule sludge disintegration serious, with a large amount of fine particle mud, anaerobism in water outlet
System cannot realize the technical barrier of granule sludge propagation, it is achieved that the propagation of anaerobic grain sludge during such waste water treatment,
Ensure efficient, the stable operation of anaerobic system；
(5) " the multistage preconditioning technique " of the present invention mainly includes materialized pretreatment and biochemical two parts of pretreatment: materialization is pre-
Process and achieve efficiently retaining and bean cake resource reclaim of particle in proteinic wastewater；Biochemical pretreatment achieve albumen destruction,
Retaining of calcium ion and phosphate radical, eliminates the influence factor that anaerobism produces interference；Efficient anaerobic unit is entered by conservative control
The pH of water, temperature, it is ensured that efficient, the stable operation of anaerobic system, volumetric loading can be up to 25kg/ (m3.d)；With this
The conventional process techniques of class waste water is compared, and this technical method has efficient, stable, resource utilization advantages of higher.
Accompanying drawing explanation
Fig. 1 is vegetable protein waste water high-efficiency processing method process chart in the present invention；
Fig. 2 is that " sour molten alkali deposited method " produces soybean protein process chart；
Fig. 3 is anaerobic system volumetric loading changing trend diagram in embodiment 3, illustrates to achieve anaerobic unit by group technology
Efficient, stable, the anaerobic unit treatment effeciency solving there is currently is the highest, the technical barrier of system fluctuation of service.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is further described below.
Embodiment 1
In conjunction with accompanying drawing 1, the technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the aluminium polychlorid (being called for short PAC) of 600mg/L, then add 10mg/L's in flotation tank
Polyacrylamide (be called for short PAM), scrape scum silica frost in flotation tank is reclaimed by filter-pressing device, filtrate is back to flotation tank；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 200mg/L in coagulation reaction tank, then adds the PAM of 10mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) coagulative precipitation tank supernatant 50% is back to air flotation cell, and other 50% is directly entered biochemical pretreatment reaction unit,
This unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires that the time of staying is 8h, molten
Solve oxygen less than 0.5mg/L so that the albumen in waste water is hydrolyzed, reduce waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 24h, anaerobic effluent, returns
Flow is 6 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 5～6；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 22000mg/L, SS be 3000～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 15000～17000mg/L, and ammonia nitrogen is higher than 400mg/L,
SS is less than 1000mg/L, and anaerobic unit volumetric loading can be up to 25kg/ (m3.d), anaerobic effluent COD is in 1000mg/L
Left and right, COD degradation rate about 92%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 100mg/L,
Meet local sewage drainage standard.
Embodiment 2
The technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the PAC of 1000mg/L in flotation tank, then adds the PAM of 20mg/L, the scum silica frost scraped
Being reclaimed by filter-pressing device, filtrate is back to air flotation cell；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 300mg/L in coagulation reaction tank, then adds the PAM of 10mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) coagulative precipitation tank supernatant 80% is back to air flotation cell, and other 20% is directly entered biochemical pretreatment reaction unit,
This unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires that the time of staying is 2h, molten
Solve oxygen less than 0.5mg/L so that the albumen in waste water is hydrolyzed, reduce waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 24h, anaerobic effluent, returns
Flow is 6 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 6～7；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 25000mg/L, SS be 3500～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 15000～16000mg/L, and ammonia nitrogen is higher than 427mg/L,
SS is less than 1000mg/L, and anaerobic unit volumetric loading can be up to 25kg/ (m3.d), anaerobic effluent COD is in 1000mg/L
Left and right, COD degradation rate about 90%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 100mg/L,
Meet local sewage drainage standard.
Embodiment 3
The technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the PAC of 50mg/L in flotation tank, then adds the PAM of 2mg/L, and the scum silica frost scraped leads to
Crossing filter-pressing device to reclaim, filtrate is back to air flotation cell；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 100mg/L in coagulation reaction tank, then adds the PAM of 10mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) coagulative precipitation tank supernatant is without backflow (capacity of returns of i.e. 0% is to air flotation cell), and 100% is directly entered biochemical pre-place
Reason reaction member, this unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires to stop
Time is 24h, dissolved oxygen is less than 0.5mg/L so that the albumen in waste water is hydrolyzed, and reduces waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 24h, anaerobic effluent, returns
Flow is 6 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 5～7；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 22000mg/L, SS be 3500～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 17000～20000mg/L, and ammonia nitrogen is higher than 450mg/L,
SS is less than 1500mg/L, and anaerobic unit volumetric loading can be up to 20kg/ (m3.d), anaerobic effluent COD is in 1200mg/L
Left and right, COD degradation rate about 90%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 150mg/L.
This embodiment anaerobic treatment effect refers to Fig. 3, by the anaerobic system volumetric loading changing trend diagram of Fig. 3, illustrates by group
Closing technique and achieve the efficient, stable of anaerobic unit, the anaerobic unit treatment effeciency solving there is currently is the highest, system is run not
Stable technical barrier.
Embodiment 4
The technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the PAC of 500mg/L in flotation tank, then adds the PAM of 6mg/L, and the scum silica frost scraped leads to
Crossing filter-pressing device to reclaim, filtrate is back to air flotation cell；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 50mg/L in coagulation reaction tank, then adds the PAM of 1mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) capacity of returns of coagulative precipitation tank supernatant 20% is to air flotation cell, and 80% is directly entered biochemical pretreatment reaction unit,
This unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires that the time of staying is 20h,
Dissolved oxygen is less than 0.5mg/L so that the albumen in waste water is hydrolyzed, and reduces waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 36h, anaerobic effluent, returns
Flow is 4 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 5～7；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 21000mg/L, SS be 3500～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 17000～20000mg/L, and ammonia nitrogen is higher than 450mg/L,
SS is less than 1500mg/L, and anaerobic unit volumetric loading can be up to 20kg/ (m3.d), anaerobic effluent COD is in 1200mg/L
Left and right, COD degradation rate about 90%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 100mg/L.
Embodiment 5
The technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the PAC of 800mg/L in flotation tank, then adds the PAM of 15mg/L, the scum silica frost scraped
Being reclaimed by filter-pressing device, filtrate is back to air flotation cell；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 100mg/L in coagulation reaction tank, then adds the PAM of 5mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) coagulative precipitation tank supernatant without 30% capacity of returns to air flotation cell, 70% is directly entered biochemical pretreatment reaction unit,
This unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires that the time of staying is 18h,
Dissolved oxygen is less than 0.5mg/L so that the albumen in waste water is hydrolyzed, and reduces waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 36h, anaerobic effluent, returns
Flow is 4 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 5～7；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 21000mg/L, SS be 3500～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 17000～20000mg/L, and ammonia nitrogen is higher than 450mg/L,
SS is less than 1500mg/L, and anaerobic unit volumetric loading can be up to 25kg/ (m3.d), anaerobic effluent COD is in 1200mg/L
Left and right, COD degradation rate about 90%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 100mg/L.
Embodiment 6
The technology method that a kind of vegetable protein waste water high-efficiency of the present embodiment processes, the steps include:
(A) vegetable protein company in Shandong produces waste water and initially enters air flotation cell, and flotation tank selects conventional air-dissolving air-float work
Skill, reflux ratio is 80%, adds the PAC of 600mg/L in flotation tank, then adds the PAM of 10mg/L, the scum silica frost scraped
Being reclaimed by filter-pressing device, filtrate is back to air flotation cell；
(B), during flotation tank water outlet enters the coagulation reaction tank of coagulation unit, coagulation unit uses conventional coagulation-settlement process,
Including coagulation reaction tank and coagulative precipitation tank, coagulation reaction tank uses mechanical agitation, stir speed (S.S.) 400 revs/min, keeps former water
PH condition, adds the poly-ferric chloride (be called for short PFC) of 200mg/L in coagulation reaction tank, then adds the PAM of 8mg/L,
In coagulation reaction tank after stirring reaction 10min clock, entering coagulative precipitation tank and carry out quiescent setting, supernatant connects next process,
Bottom sediment is back to flotation tank；
(C) capacity of returns of coagulative precipitation tank supernatant 50% is to air flotation cell, and 50% is directly entered biochemical pretreatment reaction unit,
This unit mainly uses hydrolysis acidification and sludge absorption to carry out biochemical strenuous primary treatment, and this unit requires that the time of staying is 12h,
Dissolved oxygen is less than 0.5mg/L so that the albumen in waste water is hydrolyzed, and reduces waste water SS the most further；
(D) the water outlet adapter after biochemical pretreatment refluxes to anaerobic unit, anaerobism time of staying 36h, anaerobic effluent, returns
Flow is 4 times of inflow, adds sodium hydroxide or hydrochloric acid to regulate inlet flow-patterm and is in 6～7；
(E) anaerobic effluent adapter uses conventional A/O technique to aerobic unit, aerobic process.
According to above flow process, influent COD be 22000mg/L, SS be 3500～5000mg/L, ammonia nitrogen 70～110mg/L,
After materialized pretreatment and biochemistry and process, waste water COD is about 18000～19000mg/L, and ammonia nitrogen is higher than 450mg/L,
SS is less than 1500mg/L, and anaerobic unit volumetric loading can be up to 25kg/ (m3.d), anaerobic effluent COD is in 1200mg/L
Left and right, COD degradation rate about 93%, anaerobic effluent is again after aerobic unit, and outputted aerobic water COD is less than 100mg/L.
Claims (9)
1. a vegetable protein waste water high-efficiency processing method, the steps include:
(A) waste water enters flotation tank, adds aluminium polychlorid and polyacrylamide, carry out aeration agitation, air supporting in flotation tank
Scum silica frost in pond reclaims through filter-pressing device, and filtrate is back to flotation tank；
(B) in step (A), the water outlet of flotation tank enters coagulation unit, and coagulation unit includes coagulation reaction tank and coagulative precipitation tank,
Adding poly-ferric chloride and polyacrylamide in coagulation reaction tank, coagulation reaction tank water outlet enters coagulative precipitation tank, and precipitate refluxes
To flotation tank, coagulative precipitation tank water outlet enters next processing unit；
(C) in step (B), coagulation unit sedimentation tank water outlet carries out strenuous primary treatment through biochemical pretreatment reaction unit, makes to give up
Water is more conducive to the efficient process of anaerobic unit；
(D) water outlet of step (C) mesophytization pretreatment reaction unit is caused anaerobic unit and carry out anaerobic reaction；Anaerobism is intake
PH regulator on the one hand reflux by anaerobic effluent, another aspect is by adding sodium hydroxide or hydrochloric acid；
(E) anaerobic unit water outlet in step (D) is caused " anoxia+aerobic " unit, regulates influent quality by backflow,
Realize the removal of efficient denitrification denitrification and COD.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 1, it is characterised in that: in step (A)
The reflux ratio of flotation tank is set to 80%.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 1 and 2, it is characterised in that: step (A)
In middle flotation tank, the dosage of aluminium polychlorid is 50～1000mg/L, and the dosage of polyacrylamide is 1～20mg/L.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 1, it is characterised in that: in step (B)
In coagulation unit process pond, the dosage of poly-ferric chloride is 50～300mg/L, and the dosage of polyacrylamide is 1～20mg/L.
5. according to a kind of vegetable protein waste water high-efficiency processing method described in claim 1 or 4, it is characterised in that: step (B)
In coagulation water part be back to air flotation cell, capacity of returns is 0～80%.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 3, it is characterised in that: in step (C)
The concrete grammar of the biochemical pretreatment mentioned is to use hydrolyzing sludge to be hydrolyzed by the albumen in waste water, it is achieved that the destruction of albumen,
Realizing retaining of calcium ion and phosphate radical by sludge absorption effect, this unit time of staying is 2～24h, is stirred by waterpower simultaneously
Mix control dissolved oxygen at below 0.5mg/L.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 6, it is characterised in that: in step (D)
The filler of the anaerobic unit used is granule sludge, and anaerobic effluent backflow ratio is 2～10 times, and anaerobism inlet flow-patterm regulates to 5～7.
A kind of vegetable protein waste water high-efficiency processing method the most according to claim 7, it is characterised in that: in step (D)
For regulating the solution that the sodium hydroxide of pH is 1%～10% (mass fraction), described hydrochloric acid is 1%～36% (mass fraction)
Hydrochloric acid.
9. according to a kind of vegetable protein waste water high-efficiency processing method described in claim 1 or 6, it is characterised in that: step (E)
Aerobic unit used by is A/O technique.
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