CN105621601A - Biomembrane process wastewater treatment method using mixed suspension carrier - Google Patents
Biomembrane process wastewater treatment method using mixed suspension carrier Download PDFInfo
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- CN105621601A CN105621601A CN201410588707.9A CN201410588707A CN105621601A CN 105621601 A CN105621601 A CN 105621601A CN 201410588707 A CN201410588707 A CN 201410588707A CN 105621601 A CN105621601 A CN 105621601A
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a biomembrane process wastewater treatment method using a mixed suspension carrier. The method comprises the following steps: sequentially treating wastewater to be treated in a biochemical reaction pool and a precipitation pool, discharging a supernatant in the precipitation pool, and returning at least parts of sludge at the bottom of the precipitation pool to the biochemical reaction pool, wherein a 1# suspension carrier and a 2# suspension carrier are placed in the biochemical reaction pool, the bottom of the biochemical reaction pool is provided with an aeration oxygen supply device, the 1# suspension carrier is an organic material suspension carrier, and the 2# suspension carrier is an inorganic material suspension carrier. The method can effectively reduce the content of suspensions in water finally obtained after treatment, and also has the advantages of excellent wastewater treatment effect, fast biomembrane formation starting peed, high treatment efficiency and occupied area saving.
Description
Technical field
The present invention relates to field of waste water treatment, in particular it relates to a kind of biomembrance process method of wastewater treatment using mix suspending carrier.
Background technology
Biochemical procss for treating waste water is divided into activated sludge process and two kinds of fundamental types of biomembrance process. Biomembrance process can be divided into static bed biomembrane method and fluid bed biological film method, and according to the carrier of loading microorganisms kinestate in mobile bed biofilm reactor, fluid bed biological film method can be divided into again fluidized bed bio embrane method and suspension bed biomembrance process. Owing to the power consumption of fluidized bed bio embrane method is excessive, operation controls complexity, limits its popularization and application in wastewater biochemical processes.
Suspension bed biomembrance process does not have the disadvantages mentioned above of fluidized bed bio embrane method, and has benefited from advancing by leaps and bounds of organic chemical industry's materials processing technology, obtains quick development in recent years. Suspension bed biomembrance process is to load the some proportion ratio of the density of microbe carrier and the density of water (proportion be) microbe carrier close to 1 in biochemical reaction tank, utilize and be grown in carrier biofilm and be free on the microorganism of carrier and the oxygen of ample supply, pass through biochemical action, pollutant in waste water are assimilated and decomposes, reach purification of waste water purpose. The representative processes of suspension bed biomembrance process is MBBR (MovingBedBiofilmReactor is called for short MBBR) technique.
The suspension bed biomembrance process device of application uses single microbe carrier at present, and carrier generally processes with the organic material such as polyethylene, polypropylene, and concrete shape, size then change various. For improving the serviceability (such as specific surface area, roughness, surface charging property etc.) of microbe carrier, correlation technique research staff proposes the manufacture method that some are modified to suspending carrier in recent years, and these methods are many to prepare adding portion inorganic material in raw material at carrier.
For making microbe carrier keep even suspension state in suspension bed biomembrance process plant running process, need stronger aeration intensity, therefore the scouring force in biochemical reaction tank is stronger, biomembrane easily comes off from carrier surface, and the advantageous effects thus brought is the feature that suspension bed biomembrance process has amount of activated sludge; Adverse influence be the biomembrane come off compared with traditional active sludge flco, comparatively in small, broken bits, loose, settling property is poor, thereby result in process water outlet in float not only concentration higher and not easily settlement separate. For ensureing the removal of float in water in practical application, suspension bed biomembrance process device water outlet generally requires and carries out further coagulating kinetics.
Existing many sections of patent applications in the application of suspension bed biomembrance process and carrier making and bibliographical information in prior art. Such as:
CN101565238A (a kind of novel internal circulation moving bed biological film reactor) discloses a kind of novel internal circulation moving bed biological film reactor. Reactor is divided into anoxic zone and aerobic zone, and centre is combined perforated plate by three layers and separated, and combination perforated plate top arranges porosity adjusting bolt, regulates for porosity. Inside reactor fills floating stuffing. Anoxic zone front bottom end installs undercurrent pump, and centre arranges deflector, under the impetus of undercurrent pump, forms waterpower circulation clockwise in anoxic zone; Installing aeration head bottom rear end, aerobic zone, centre arranges deflector, under the effect of aeration, forms waterpower circulation counterclockwise in aerobic zone. In twoth district under driving to circulation, mixed liquor is from aerobic zone inner circulating reflux to anoxic zone, while efficient organics removal, it is achieved the nitration denitrification elimination of nutrient nitrogen. Reactor front bottom end arranges water inlet, and top, rear end arranges downflow weir and outlet, and bottom arranges mud discharging mouth. Structure of reactor is compact, and treatment effeciency is high.
CN103466787A (combined type aeration MBBR) discloses a kind of combined type aeration MBBR, the reactor body of manhole is offered including side, top, the sidewall of reactor body is provided with the water inlet pipe with reactor body inner space and outlet pipe, circulation deflector it is provided with in reactor body, described circulation deflector side is provided with perforated pipe aerating regulation system near reactor body inner bottom place, perforated pipe aerating regulation system is provided above micro-pore aeration system, reactor body inner top is provided with and prevents floating stuffing from floating in reactor the backwashing system on liquid level. move on the basis of biofilm reactor in tradition, aerating system is improved, upgrades, and increase backwashing system. by increasing simple tubing, the difficult problem such as solve at the bottom of the tradition internal floating stuffing sedimentation basin of MBBR, " climbing wall " floats, dissolved oxygen is not enough, the more perfect practical application of MBBR.
CN101066800A (modified microbial membrane carrier) proposes a kind of method using three kinds of raw materials (high density polyethylene (HDPE), No. 1 material, No. 2 material) to manufacture biofilm carrier. Wherein No. 1 compound particles expected for following composition: waste stone dust, coke blacking, slag powders, iron powder, high density polyethylene (HDPE), the compound particles that No. 2 material are following composition: slag powders, Pulvis Talci, iron powder, high density polyethylene (HDPE). The microbial membrane carrier wet density of the present invention is close to water, surface hydrophilicity is strong, and microorganism tack is good, biofilm easy, difficult drop-off, and long time running is without sludge blockage phenomenon, biomembrane activity is high, film minimal thickness, only at 10-200 ��m, considerably improves its clearance to nitrogen phosphorus, and sludge settling performance is good, mud generation amount is few, 40-80% fewer than original activated sludge process generation amount, treatment effeciency improves 30-50%, and operating cost reduces by 30%; It is service life 50 years, puts into and reaction tank does not need change and manual maintenance.
CN102827410A (biological affine hydrophilic magnetic suspension filler and preparation method thereof) discloses a kind of biological affine hydrophilic magnetic suspension filler, solves the problem that filler scavenging effect of the prior art is not good. This invention mainly contains the component of following parts by weight: high density polyethylene (HDPE) 66.2-91.7, activated carbon 3-5, polyvinyl alcohol 2-5, ferroso-ferric oxide 2-5, starch 1-3, paraffin 1-2, chitin 0.2-2, Aluminate coupling agent 0.2-2, also includes��0.2 and the white carbon black of > 0 weight portion; The preparation method that this patent application additionally provides biological affine hydrophilic magnetic suspension filler. The feature that the biofilm speed of this patent application is fast, micro organism quantity is many, shock-resistant good stability, excess sludge are few.
" MBBR application in sewage disposal " (Xi'an University's journal-natural science edition, 2nd phase in 2011) in describe the technological principle of MBBR and be different from the process characteristic of other biological membrane reactor, discuss the material of filler in MBBR, size, shape, proportion, quantity and effective ratio area thereof, stirring type and alr mode, the size of organic loading, the impact on MBBR operational effect of the factors such as hydraulic detention time, review independent MBBR technique, the technique in MBBR and activated sludge pond altogether, the group technology of MBBR and other techniques application present situation in sewage disposal, indicate developing direction and the trend of this technology.
But, in practice it has proved that, utilize the biomembrance process method of wastewater treatment of above-mentioned conventional suspension carrier to process the content of float in the water outlet obtained still higher, still need to the content processed further to reduce float.
Summary of the invention
The invention aims to overcome the biomembrance process method of wastewater treatment using conventional suspension carrier in art methods to process the defect that in the water outlet obtained, the content of float is higher, a kind of biomembrance process method of wastewater treatment using mix suspending carrier is provided, the method effectively reduction can process the suspension content in the water outlet obtained, there is the water treatment effect of excellence, and have that start-up speed is fast, treatment effeciency is high and save the advantages such as floor space.
The present inventor has been surprisingly found that under study for action, in the biomembrance process method of wastewater treatment using suspending carrier, pending waste water is processed successively in biochemical reaction tank and sedimentation tank, by placing 1# suspending carrier (i.e. organic material suspending carrier) and 2# suspending carrier (i.e. inorganic material suspending carrier) in biochemical reaction tank and installing aeration oxygen supply equipment bottom biochemical reaction tank simultaneously, discharge the supernatant of sedimentation tank and the mud bottom sedimentation tank is back at least partly the mode of biochemical reaction tank, effectively reduction can process the suspension content in the water outlet obtained, there is the water treatment effect of excellence, and it is fast to have start-up speed, treatment effeciency is high and saves the advantages such as floor space.
Therefore, to achieve these goals, the invention provides a kind of biomembrance process method of wastewater treatment using mix suspending carrier, described method includes: processed in biochemical reaction tank and sedimentation tank successively by pending waste water, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back to biochemical reaction tank at least partly, wherein, biochemical reaction tank is placed 1# suspending carrier and 2# suspending carrier, and aeration oxygen supply equipment is installed bottom biochemical reaction tank, described 1# suspending carrier is organic material suspending carrier, described 2# suspending carrier is inorganic material suspending carrier.
Existence due to 2# suspending carrier (i.e. inorganic material suspending carrier), the method of the present invention not only overcomes and uses the biomembrance process method of wastewater treatment of conventional suspension carrier to process the shortcoming that in the water outlet that obtains, suspension content is higher, and has that start-up speed is fast, treatment effeciency is high and saves the advantages such as floor space:
1) existence of little particulate inorganic material suspending carrier can improve the settling property of biological floe in biochemical reaction tank water outlet, thus promoting the solid-liquid separation capability of sedimentation tank, overcome conventional carrier fluidization biofilm reactor and process the shortcoming that in water outlet, suspension content is high, there is the water treatment effect of excellence.
2) due to inorganic material suspending carrier surface positively charged, it is easy to the apposition growth of microorganism, can make biochemical reaction tank is kept here more microorganism flco during starting biofilm, thus the rapid biofilm being conducive to system overall starts.
3) due to little particulate inorganic material suspending carrier in biochemical reaction tank as the gathering core of free microorganism flco and biomembranous carrier, improve the total amount of microorganism in biochemical reaction tank, both the biochemical reaction tank process of refinement degree to Pollutants in Wastewater it had been favorably improved, the removal speed of pollutant can be improved again, such that it is able to improve the overall treatment efficiency of system, save floor space.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Fig. 1 is the process chart of the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Detailed description of the invention
Hereinafter the specific embodiment of the present invention is described in detail. It should be appreciated that detailed description of the invention described herein is merely to illustrate and explains the present invention, it is not limited to the present invention.
The invention provides a kind of biomembrance process method of wastewater treatment using mix suspending carrier, the method includes: processed in biochemical reaction tank and sedimentation tank successively by pending waste water, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back to biochemical reaction tank at least partly, wherein, biochemical reaction tank is placed 1# suspending carrier and 2# suspending carrier, and aeration oxygen supply equipment is installed bottom biochemical reaction tank, described 1# suspending carrier is organic material suspending carrier, and described 2# suspending carrier is inorganic material suspending carrier.
What those skilled in the art should understand that is, 1# suspending carrier and the 2# suspending carrier placed in biochemical reaction tank can adhere to medium as biomembrane, microorganism is at suspending carrier surface attachment biofilm growth formation, and the microorganism in biomembrane plays pollution removal effect in growth and breeding process; The aeration oxygen supply equipment installed bottom biochemical reaction tank can provide oxygen for microbial growth breeding, makes suspending carrier keep even suspension state simultaneously.
In the inventive method, for 1# suspending carrier (i.e. organic material suspending carrier), there is no particular limitation, can be the commonly used in the art various suspending carriers processed for primary raw material with organic material, preferably, the organic material of 1# suspending carrier includes polyethylene and/or polypropylene.
In order to improve the treatment effect to waste water further, under preferable case, 1# suspending carrier is column suspending carrier or spherical suspending carrier, the diameter of column suspending carrier is preferably 0.5-15cm, more preferably 0.5-5cm, the thickness of column suspending carrier is preferably 0.2-10cm, more preferably 0.3-3.0cm; The diameter of spherical suspending carrier is preferably 0.5-15cm, more preferably 0.5-6cm.
In the inventive method, 1# suspending carrier is disposable placement, no longer supplements in the processing procedure to waste water. Under preferable case, the proportion of the 1# suspending carrier ratio of the density of water (density of proportion and suspending carrier with) is 0.96-0.99, in stacking volume, in biochemical reaction tank, the filling rate of 1# suspending carrier is preferably 10-70%, more preferably 25-45%.
In the inventive method, it will be understood by those skilled in the art that stacking volume refers to the space size that suspending carrier occupies under natural packing state. Filling rate refers to the ratio of the stacking volume of the suspending carrier of filling and the dischargeable capacity of biochemical reaction tank.
In the inventive method, for 2# suspending carrier (i.e. inorganic material suspending carrier), there is no particular limitation, it can be the fine-grained carrier using inorganic material to process, in order to improve the treatment effect to waste water further, under preferable case, 2# suspending carrier includes one or more in haydite, zeolite, activated carbon, volcanic rock and anthracite, more preferably activated carbon.
In the inventive method, in order to ensure that 2# suspending carrier is suspended motion state in biochemical reaction tank and improves the treatment effect to waste water further, it is preferable that in situation, the particle diameter of 2# suspending carrier is 0.01-0.9mm, more preferably 0.05-0.4mm.
In the inventive method, 2# suspending carrier is continuous or periodic in processing procedure to be added, it is preferable that in situation, before process starts, and in the dischargeable capacity of biochemical reaction tank every cubic metre, the amount of the 2# suspending carrier placed in biochemical reaction tank is 0.5-50kg; After process starts, often to process the waste water of 1 cubic metre, the amount of the 2# suspending carrier added in biochemical reaction tank is 0.02-2Kg. It is further preferred that 2# suspending carrier is activated carbon, before process starts, in the dischargeable capacity of biochemical reaction tank every cubic metre, the amount of the activated carbon placed in biochemical reaction tank is 0.5-20kg, more preferably 2-10kg; After process starts, often to process the waste water of 1 cubic metre, the amount of the 2# suspending carrier added in biochemical reaction tank is 0.05-0.5Kg.
In the inventive method, 1# suspending carrier and 2# suspending carrier are all commercially available. 1# suspending carrier is main carriers, and 2# suspending carrier is assistant carrier.
In the inventive method, for aeration oxygen supply equipment, there is no particular limitation, it is possible to for various aeration oxygen supply equipments commonly used in the art, for instance can be perforated pipe aerating regulation system.
In the inventive method, determine (including COD height, biochemical treatment performance quality etc.) the COD load of biochemical reaction tank according to the concrete condition of pending waste water quality, it is preferable that in situation, the COD load of biochemical reaction tank is 0.2-20KgCOD/m3D, more preferably 1-4KgCOD/m3��d��
In the inventive method, concrete condition according to pending waste water quality determines (including COD height, biochemical treatment performance quality etc.) hydraulic detention time of biochemical reaction tank, under preferable case, the condition carrying out processing in biochemical reaction tank includes: the hydraulic detention time of biochemical reaction tank is 2-50h, it is further preferred that the hydraulic detention time of biochemical reaction tank is 8-25h.
In the inventive method, 2# suspending carrier is present in biochemical reaction tank water outlet with aerosol form, can according to the size of 1# suspending carrier and 2# suspending carrier, control in biochemical reaction tank water outlet containing 2# suspending carrier without 1# suspending carrier, with 1# suspending carrier be disposable placement, 2# suspending carrier in processing procedure continuous or periodic add consistent. For the method that controls in biochemical reaction tank water outlet containing 2# suspending carrier without 1# suspending carrier, there is no particular limitation, as long as make in biochemical reaction tank water outlet containing 2# suspending carrier and without 1# suspending carrier, this is conventionally known to one of skill in the art, and therefore not to repeat here.
In the inventive method, sedimentation tank hydraulic detention time can according to the design standard value of common biochemical second pond, under preferable case, the condition carrying out processing in sedimentation tank includes: the hydraulic detention time of sedimentation tank is 45-200min, more preferably 80-120min.
What those skilled in the art should understand that is, the mode carrying out processing in sedimentation tank may include that biochemical reaction tank water outlet (the 2# suspending carrier containing flowing out with water) enters sedimentation tank and carries out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly (including 2# suspending carrier and the microorganism of surface attachment, the residual flco of microorganism and other float) front end of biochemical reaction tank. That is, 2# suspending carrier flows out biochemical reaction tank with waste water, returns directly to recycle in biochemical reaction tank as the component of clarifier sludge through precipitate and separate rear portion.
In the inventive method, it is preferable that in situation, the reflux ratio of the mud bottom sedimentation tank is 10-300%, it is preferred to 20-100%.
In the inventive method, the method also includes: the mud not being back to biochemical reaction tank bottom sedimentation tank is carried out recycling, reclaims and obtains 2# suspending carrier, and is back in biochemical reaction tank reuses reclaiming the 2# suspending carrier obtained.
What those skilled in the art should understand that is, the mud not being back to biochemical reaction tank bottom sedimentation tank is sent into 2# suspending carrier clean and reuse unit, it is carried out processing to remove the epontic biomembrane of 2# suspending carrier, and reclaims 2# suspending carrier to recycle 2# suspending carrier. Meanwhile, discharge the mud produced in 2# suspending carrier clean and reuse process, and waste water 2# suspending carrier clean and reuse process produced returns sewage treatment plant's upstream processing unit and processes.
In the inventive method, there is no particular limitation for the method processed for clean and reuse, as long as epontic for 2# suspending carrier biomembrane can be removed and 2# suspending carrier can be reclaimed, under preferable case, the method that clean and reuse processes includes mechanical cleaning recycling and/or Chemical cleaning recycling. Mechanical cleaning recycling can include Air Exposure and/or mechanical agitation. For Air Exposure and churned mechanically condition, there is no particular limitation, it is possible to for various conditions commonly used in the art, this is conventionally known to one of skill in the art, does not repeat them here. Chemical cleaning reclaims and can include with diluted acid or diluted alkaline immersion etc. For the kind of diluted acid and diluted alkaline, there is no particular limitation, can be various diluted acids commonly used in the art and diluted alkaline, such as diluted acid can be one or more in dilute hydrochloric acid, dilute sulfuric acid and dust technology, and diluted alkaline can be one or more in dilute sodium hydroxide, rare potassium hydroxide and rare calcium hydroxide. Diluted acid and rare paper mill wastewater can be 0.05-0.1mol/L, and the time of immersion can be 10-100min.
Embodiment
The present invention is further illustrated for below example, but and is not so limited the present invention.
In following example and comparative example, the mensuration of waste water COD adopts dichromate titration (GB11914-89), the mensuration of ammonia nitrogen adopts Na's colorimetry (GB7479-87), the mensuration of float adopts gravimetric method (GB11901-89), and the mensuration of oil content adopts " in oil field extracted water determination method for oil content (SY/T0530-2011) ".
Fine grained activated carbon (particle diameter is 0.05-0.10mm) is purchased from Hua Long filtrate factory of Gongyi City.
Fine grained haydite (particle diameter is 0.15-0.25mm) is purchased from Zhonghai Asphalt (Taizhou) Co., Ltd..
Particulate zeolite (particle diameter is 0.15-0.30mm) is purchased from Zhonghai Asphalt (Taizhou) Co., Ltd..
Fine grained volcanic rock (particle diameter is 0.15-0.35mm) is purchased from Zhonghai Asphalt (Taizhou) Co., Ltd..
Diameter be 2.5cm, thickness 0.8cm column suspending carrier purchased from Zhonghai Asphalt (Taizhou) Co., Ltd., proportion is 0.98.
Diameter be the spherical suspending carrier of 2.5cm purchased from Zhonghai Asphalt (Taizhou) Co., Ltd., proportion is 0.98.
Embodiment 1
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 500-620mg/L, ammonia nitrogen is 20-35mg/L, oil content is 10-20mg/L, suspension content is 80-170mg/L, and water temperature is 20-25 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank; in biochemical reaction tank, disposable placement diameter to be 2.5cm, thickness be 0.8cm, proportion are the column suspending carrier of 0.98; in stacking volume; in biochemical reaction tank, the filling rate of column suspending carrier is 35%; before process starts; dischargeable capacity in biochemical reaction tank every cubic metre; biochemical reaction tank is placed the fine grained activated carbon of 2kg; being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 1.2-1.5KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 10h, after process starts, often to process the waste water of 1 cubic metre, adds the fine grained activated carbon of 50g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank is first soaked 20min with the dilute hydrochloric acid that concentration is 0.05mol/L, then the mode adopting the stirring of aeration Aided Machine is carried out recycling, recovery obtains fine grained activated carbon, and be back in biochemical reaction tank reuse reclaiming the fine grained activated carbon that obtains, discharge the mud produced in fine grained activated carbon clean and reuse process simultaneously, and waste water fine grained activated carbon clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 1.5h, the reflux ratio of the mud bottom sedimentation tank is 50%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 30-45mg/L, ammonia nitrogen is 0.1-2.0mg/L, oil content is 0.5-1.5mg/L, suspension content is 15-35mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Embodiment 2
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 1200-1400mg/L, ammonia nitrogen is 30-45mg/L, oil content is 10-20mg/L, suspension content is 100-250mg/L, and water temperature is 15-20 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank; in biochemical reaction tank disposable placement diameter to be 2.5cm, proportion be 0.98 spherical suspending carrier; in stacking volume; in biochemical reaction tank, the filling rate of spherical suspending carrier is 45%; before process starts; dischargeable capacity in biochemical reaction tank every cubic metre; biochemical reaction tank is placed the fine grained activated carbon of 6kg; being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 3.8-4.0KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 25h, after process starts, often to process the waste water of 1 cubic metre, adds the fine grained activated carbon of 500g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank is first soaked 20min with the dilute hydrochloric acid that concentration is 0.05mol/L, then the mode adopting the stirring of aeration Aided Machine is carried out recycling, recovery obtains fine grained activated carbon, and be back in biochemical reaction tank reuse reclaiming the fine grained activated carbon that obtains, discharge the mud produced in fine grained activated carbon clean and reuse process simultaneously, and waste water fine grained activated carbon clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 80min, the reflux ratio of the mud bottom sedimentation tank is 100%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 30-40mg/L, ammonia nitrogen is 4-5mg/L, oil content is 2-3mg/L, suspension content is 20-40mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Embodiment 3
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 500-620mg/L, ammonia nitrogen is 20-35mg/L, oil content is 10-20mg/L, suspension content is 80-170mg/L, and water temperature is 20-25 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank; in biochemical reaction tank, disposable placement diameter to be 2.5cm, thickness be 0.8cm, proportion are the column suspending carrier of 0.98; in stacking volume; in biochemical reaction tank, the filling rate of column suspending carrier is 25%; before process starts; dischargeable capacity in biochemical reaction tank every cubic metre; biochemical reaction tank is placed the fine grained activated carbon of 10kg; being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 1.0-1.3KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 8h, after process starts, often to process the waste water of 1 cubic metre, adds the fine grained activated carbon of 350g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank is first soaked 20min with the dilute hydrochloric acid that concentration is 0.05mol/L, then the mode adopting the stirring of aeration Aided Machine is carried out recycling, recovery obtains fine grained activated carbon, and be back in biochemical reaction tank reuse reclaiming the fine grained activated carbon that obtains, discharge the mud produced in fine grained activated carbon clean and reuse process simultaneously, and waste water fine grained activated carbon clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 2h, the reflux ratio of the mud bottom sedimentation tank is 20%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 30-40mg/L, ammonia nitrogen is 0.1-2.5mg/L, oil content is 0.5-2mg/L, suspension content is 18-38mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Embodiment 4
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 460-560mg/L, ammonia nitrogen is 20-30mg/L, oil content is 10-20mg/L, suspension content is 100-200mg/L, and water temperature is 22-26 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank, in biochemical reaction tank, disposable placement diameter to be 2.5cm, thickness be 0.8cm, proportion are the column suspending carrier of 0.98, in stacking volume, in biochemical reaction tank, the filling rate of column suspending carrier is 50%, before process starts, dischargeable capacity in biochemical reaction tank every cubic metre, biochemical reaction tank is placed the fine grained haydite of 6kg, being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 1.0-1.2KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 12h, after process starts, often to process the waste water of 1 cubic metre, adds the fine grained haydite of 500g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank adopts the mode of aeration Aided Machine stirring be carried out recycling, recovery obtains fine grained haydite, and be back in biochemical reaction tank reuse reclaiming the fine grained haydite that obtains, discharge the mud produced in fine grained haydite clean and reuse process simultaneously, and waste water fine grained haydite clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 1.5h, the reflux ratio of the mud bottom sedimentation tank is 60%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 35-55mg/L, ammonia nitrogen is 2-4mg/L, oil content is 1-2mg/L, suspension content is 15-40mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Embodiment 5
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 1200-1400mg/L, ammonia nitrogen is 30-45mg/L, oil content is 10-20mg/L, suspension content is 100-250mg/L, and water temperature is 15-20 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank, in biochemical reaction tank disposable placement diameter to be 2.5cm, proportion be 0.98 spherical suspending carrier, in stacking volume, in biochemical reaction tank, the filling rate of spherical suspending carrier is 10%, before process starts, dischargeable capacity in biochemical reaction tank every cubic metre, biochemical reaction tank is placed the particulate zeolite of 15kg, being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 5.1-5.2KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 30h, after process starts, often to process the waste water of 1 cubic metre, adds the particulate zeolite of 500g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank is first soaked 20min with the dilute hydrochloric acid that concentration is 0.05mol/L, then the mode adopting the stirring of aeration Aided Machine is carried out recycling, recovery obtains particulate zeolite, and be back in biochemical reaction tank reuse reclaiming the particulate zeolite that obtains, discharge the mud produced in particulate zeolite clean and reuse process simultaneously, and waste water particulate zeolite clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 200min, the reflux ratio of the mud bottom sedimentation tank is 150%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 40-54mg/L, ammonia nitrogen is 4-7mg/L, oil content is 2-4mg/L, suspension content is 30-40mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Embodiment 6
The present embodiment is for illustrating the biomembrance process method of wastewater treatment using mix suspending carrier of the present invention.
Pending waste water is (in actual production, wastewater treatment process is dynamic processes, each index of waste water is generally within certain scope) basic condition: COD is 380-460mg/L, ammonia nitrogen is 20-30mg/L, oil content is 10-20mg/L, suspension content is 70-150mg/L, and water temperature is 15-20 DEG C.
Perforated pipe aerating regulation system is installed bottom biochemical reaction tank; in biochemical reaction tank, disposable placement diameter to be 2.5cm, thickness be 0.8cm, proportion are the column suspending carrier of 0.98; in stacking volume; in biochemical reaction tank, the filling rate of column suspending carrier is 30%; before process starts; dischargeable capacity in biochemical reaction tank every cubic metre; biochemical reaction tank is placed the fine grained volcanic rock of 9kg; being passed in biochemical reaction tank by aforementioned pending waste water and process, the COD load of biochemical reaction tank is 0.9-1.1KgCOD/m3D, the hydraulic detention time of biochemical reaction tank is 10h, after process starts, often to process the waste water of 1 cubic metre, adds the fine grained volcanic rock of 600g in biochemical reaction tank, biochemical reaction tank water outlet is passed in sedimentation tank and carry out precipitate and separate, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back at least partly the front end of biochemical reaction tank, and the mud not being back to biochemical reaction tank bottom sedimentation tank is first soaked 10min with the dilute sodium hydroxide that concentration is 0.1mol/L 80 DEG C, then the mode adopting the stirring of aeration Aided Machine is carried out recycling, recovery obtains fine grained volcanic rock, and be back in biochemical reaction tank reuse reclaiming the fine grained volcanic rock that obtains, discharge the mud produced in fine grained volcanic rock clean and reuse process simultaneously, and waste water fine grained volcanic rock clean and reuse process produced returns sewage treatment plant upstream processing unit and processes, wherein, sedimentation tank hydraulic detention time is 1.5h, the reflux ratio of the mud bottom sedimentation tank is 60%.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 25-45mg/L, ammonia nitrogen is 0.5-2mg/L, oil content is 1-2mg/L, suspension content is 15-30mg/L, it is better than national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
Comparative example 1
Method according to embodiment 1; the difference is that; biochemical reaction tank is not placed fine grained activated carbon (namely not placing any kind of 2# suspending carrier), correspondingly, the mud not being back to biochemical reaction tank bottom sedimentation tank is not carried out recycling yet.
System stable operation recorded after 20 days: sedimentation tank water outlet COD is 50-70mg/L, ammonia nitrogen is 2.5-4.5mg/L, oil content is 1.5-3.0mg/L, suspension content is 75-85mg/L, suspension content is unsatisfactory for national grade one discharge standard (COD��60mg/L, ammonia nitrogen��15mg/L, oil content��10mg/L, suspension content��70mg/L).
By the embodiment of the present invention 1 compared with comparative example 1, known: in the biomembrance process method of wastewater treatment using suspending carrier, biochemical reaction tank is placed 1# suspending carrier (organic material suspending carrier) and 2# suspending carrier (inorganic material suspending carrier) simultaneously, can effectively reduce the suspension content processed in water outlet, be substantially improved the treatment effect of waste water.
The method of the present invention effectively reduction can process the suspension content in the water outlet that obtains, has a water treatment effect of excellence, and has that start-up speed is fast, treatment effeciency is high and saves the advantages such as floor space.
The preferred embodiment of the present invention described in detail above; but, the present invention is not limited to the detail in above-mentioned embodiment, in the technology concept of the present invention; technical scheme can being carried out multiple simple variant, these simple variant belong to protection scope of the present invention.
It is further to note that, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, it is possible to be combined by any suitable mode, in order to avoid unnecessary repetition, various possible compound modes are no longer illustrated by the present invention separately.
Additionally, can also carry out combination in any between the various different embodiment of the present invention, as long as it is without prejudice to the thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (13)
1. the biomembrance process method of wastewater treatment using mix suspending carrier, it is characterized in that, described method includes: processed in biochemical reaction tank and sedimentation tank successively by pending waste water, discharge the supernatant of sedimentation tank, and the mud bottom sedimentation tank is back to biochemical reaction tank at least partly, wherein, biochemical reaction tank is placed 1# suspending carrier and 2# suspending carrier, and aeration oxygen supply equipment is installed bottom biochemical reaction tank, described 1# suspending carrier is organic material suspending carrier, and described 2# suspending carrier is inorganic material suspending carrier.
2. method according to claim 1, wherein, described method also includes: the mud not being back to biochemical reaction tank bottom sedimentation tank is carried out recycling, reclaims and obtains 2# suspending carrier, and is back in biochemical reaction tank reuses reclaiming the 2# suspending carrier obtained.
3. method according to claim 1 and 2, wherein, described 1# suspending carrier is disposable placement, and in stacking volume, in biochemical reaction tank, the filling rate of 1# suspending carrier is 10-70%, it is preferred to 25-45%.
4. method according to claim 1 and 2, wherein, described 2# suspending carrier is continuous or periodic in processing procedure to be added, before process starts, in the dischargeable capacity of biochemical reaction tank every cubic metre, the amount of the 2# suspending carrier placed in biochemical reaction tank is 0.5-50kg; After process starts, often to process the waste water of 1 cubic metre, the amount of the 2# suspending carrier added in biochemical reaction tank is 0.02-2Kg.
5. method according to claim 1 and 2, wherein, described 1# suspending carrier is column suspending carrier or spherical suspending carrier, the diameter of described column suspending carrier is 0.5-15cm, being preferably 0.5-5cm, the thickness of described column suspending carrier is 0.2-10cm, it is preferred to 0.3-3.0cm; The diameter of described spherical suspending carrier is 0.5-15cm, it is preferred to 0.5-6cm.
6. method according to claim 1 and 2, wherein, the organic material of described 1# suspending carrier includes polyethylene and/or polypropylene.
7. method according to claim 1 and 2, wherein, described 2# suspending carrier includes one or more in haydite, zeolite, activated carbon, volcanic rock and anthracite.
8. method according to claim 7, wherein, the particle diameter of described 2# suspending carrier is 0.01-0.9mm, it is preferred to 0.05-0.4mm.
9. method according to claim 1 and 2, wherein, the COD load of biochemical reaction tank is 0.2-20KgCOD/m3D, it is preferred to 1-4KgCOD/m3��d��
10. method according to claim 9, wherein, the condition carrying out processing in biochemical reaction tank includes: the hydraulic detention time of biochemical reaction tank is 2-50h, it is preferred to 8-25h.
11. method according to claim 1 and 2, wherein, the condition carrying out processing in sedimentation tank includes: the hydraulic detention time of sedimentation tank is 45-200min, it is preferred to 80-120min.
12. method according to claim 11, wherein, the reflux ratio of the mud bottom sedimentation tank is 10-300%, it is preferred to 20-100%.
13. method according to claim 2, wherein, the method that described clean and reuse processes includes mechanical cleaning recycling and/or Chemical cleaning recycling.
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| CN108726660A (en) * | 2018-08-07 | 2018-11-02 | 浙江海拓环境技术有限公司 | A kind of MBBR reactors for electroplating wastewater processing |
| CN110980963A (en) * | 2019-11-26 | 2020-04-10 | 浙江永续环境工程有限公司 | Sewage treatment process applying active microbial inoculum |
| CN112850892A (en) * | 2019-11-28 | 2021-05-28 | 上海市南洋模范中学 | Digestion bed device and process for floating ball self-generation microbial film |
| CN114536584A (en) * | 2022-01-28 | 2022-05-27 | 青岛思普润水处理股份有限公司 | Moving bed biofilm suspension carrier for sewage treatment and preparation method thereof |
| CN114906976A (en) * | 2022-03-14 | 2022-08-16 | 安徽工业大学 | Device and method for treating heavy metal sewage by using plastic fragments of biological membrane |
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| CN108726660A (en) * | 2018-08-07 | 2018-11-02 | 浙江海拓环境技术有限公司 | A kind of MBBR reactors for electroplating wastewater processing |
| CN110980963A (en) * | 2019-11-26 | 2020-04-10 | 浙江永续环境工程有限公司 | Sewage treatment process applying active microbial inoculum |
| CN112850892A (en) * | 2019-11-28 | 2021-05-28 | 上海市南洋模范中学 | Digestion bed device and process for floating ball self-generation microbial film |
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| CN114536584B (en) * | 2022-01-28 | 2023-08-22 | 青岛思普润水处理股份有限公司 | Moving bed biomembrane suspension carrier for sewage treatment and preparation method thereof |
| CN114906976A (en) * | 2022-03-14 | 2022-08-16 | 安徽工业大学 | Device and method for treating heavy metal sewage by using plastic fragments of biological membrane |
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