CN1045083A - Disposing waste water by biological fluidized bed with sponge carrier method and device thereof - Google Patents
Disposing waste water by biological fluidized bed with sponge carrier method and device thereof Download PDFInfo
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- CN1045083A CN1045083A CN90100795A CN90100795A CN1045083A CN 1045083 A CN1045083 A CN 1045083A CN 90100795 A CN90100795 A CN 90100795A CN 90100795 A CN90100795 A CN 90100795A CN 1045083 A CN1045083 A CN 1045083A
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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
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Abstract
The present invention relates to a kind of disposing waste water by biological fluidized bed with sponge carrier method and device thereof.
In the modified version three-phase biological fluidized bed reactor, be furnished with gac/pore rubber sponge carrier, under normal pressure or pressurized conditions, carry out perforated pipe aerating regulation or jet-flow aeration, carry out aerobic and facultative anaerobic biochemical reaction pair waste water simultaneously and handle.The present invention handles waste water in the particulate fluidization mode, and its carrier is difficult for running off, without stripping machine.Be applicable to the wastewater treatment of industrial enterprise such as big-and-middle-sized chemical industry, petrochemical industry, pharmacy, printing and dyeing, food.
Description
What the present invention relates to is a kind of disposing waste water by biological fluidized bed technology, and referring more particularly to the sponge is the disposing waste water by biological fluidized bed method and the device thereof of carrier.
At present, the method for disposing of sewage is a lot, and wherein degradation of organic substances is the most general with biochemical treatment, not only economy but also be suitable for big yield and handle.Two kinds of biological treatment branch anaerobic process and aerobic methods.The former less energy consumption be applicable to the sewage that COD is high, but the residence time is long, and investment is high, and effluent quality and emission standard have a long way to go.The latter is opposite, is applicable to sewage of low concentration, and water outlet is clean, is expected to reach discharging standards.
Aerobic biochemical technology is divided into activated sludge process and biomembrance process two big classes.The former invests low, but biomass is less, and device volume is big, and occupation of land is many, and mud easily expands.Biomembrance process has the biological filter, blodisc, contact oxidation method.These methods are owing to the content height of MLVSS, and volumetric loading is also bigger, stable operation.But biomembrance process has and is difficult for long film or film and looks and contain very much, upgrades difficulty, even obstruction, liquid-solid loose contact.For overcoming above-mentioned shortcoming, biological fluidized bed method has appearred.Biological fluidized bed method is the new technology that the seventies grows up, and it is based on biomembrance process, draws the fluidization technology of chemical industry operation, is ideal method comparatively in the current biochemical treatment waste water.Biological fluidized bed is used small-particle usually, and (0.1～1mm) sand, charcoal, pottery, artificial resin, glass micropore etc. are carrier [" disposing waste water by biological fluidized bed experimental study " literary composition, author: Beijing Chemical Research Institute's environmental protection institute, the unit of providing: Science and Technology of Shanghai information institute, the number of asking for: 283285], though it has overcome some shortcomings of aforementioned biomembrance process, but also there are some weakness in self, is equipped with the demoulding device as needs; Tiny as particle, density is low, run off easily; If the carrier granularity is big, the density height, and also energy consumption is big, and [" Biological Fluidized Bed Used in Wastewater Treatment technical development overview " author: the Cui Lian of environmental protection institute of orchidization chemical research institute rises, Mo Guangcheng.Orchidization science and technology the 4th volume first phase P47-52].And grain fluidized bedly in operation, keep the good also non-easy thing of particulate fluidization.
The present invention is intended to overcome the deficiency of above-mentioned biological fluidized bed method, and a kind of new carrier is provided, a kind of new disposing waste water by biological fluidized bed method and the device that adapts with this method thereof.The present invention does not need the demoulding device, and carrier can not run off, and energy consumption is low, can further improve the efficient of Biological Fluidized Bed Used in Wastewater Treatment and reduce operating cost.
Disposing waste water by biological fluidized bed method of the present invention, be in the modified version three-phase biological fluidized bed reactor, with gac/pore silicon rubber sponge is carrier, generate microbial film with surperficial under the waste water concurrent conditions and outside surface within it, air passes through perforated pipe or jet-flow aeration or deep aerating under normal pressure or pressurized conditions, gas-water ratio is 10～20: the 1(volume ratio), air is from the annular space bubbling, after being promoted to inner core again, descending along inner core enters annular space again and circulates, and carries out simultaneously aerobicly handling with facultative anaerobic biochemical reaction pair waste water.In circulating, gac/pore rubber sponge carrier also flows with water liquid flow direction, has driven a large amount of active sludge and has contacted with air filled cavity, has accelerated biochemical reaction rate.Carrier is collision, phase mutual friction mutually in flowing or in violent motion, makes biofilm detachment, the renewal of carrier outside, and carrier separates by sieve tray with mud with treating water.Meanwhile, its carrier inside also produces the facultative anaerobic biochemical reaction, carries out deoxidation, dephosphorization.Above-mentioned perforated pipe aerating regulation intensity is 10～20m
3/ m
2H, jet-flow aeration intensity is 30～50m
3/ m
2H, deep aerating intensity is 10m
3/ m
2More than the h.
Aforesaid three kinds of aeration modes are in view of the consideration to following factor.Three-phase biologic fluidized-bed sludge quantity is big, requires the oxygen amount of supply also big.On selecting, aeration mode taken into full account the utilization ratio of oxygen.Under the condition of identical tolerance, bubble diameter is to influence the important factor that oxygen transmits.Therefore the present invention has selected trickle bubble aeration mode, adopting the roots blower pressure head is the perforated pipe aerating regulation of 3～5m, or utilizes the tail gas (1～3kg/cm that jet-flow aeration is carried out in water outlet and discharge at the biological contact oxidation tower top of pressurizeing of pressurization biological contact oxidation tower (CN8821135.8 patentee Shanghai Normal University)
2) carry out circulation power and the oxygenation source of deep aerating as biological fluidized-bed reactor.Calculation formula is:
P=H
o+ H
f+ H
k(in the water column height)
P-compressed air outlet blast
H
o-fluidized-bed still water level height
H
f-through pressure that aeration loses.
For realizing aforesaid method, the present invention provides the modified version that is applicable to the inventive method three-phase biological fluidized bed reactor again.It comprises fluidized-bed periphery, fluidized-bed inner core, fluidised bedplate, gas distribution pipe, water-in, water outlet.It is characterized in that: being furnished with in the three-phase biological fluidized bed reactor and accounting for volume is gac/pore rubber sponge carrier of 20～40%.The water outlet place is equipped with and makes gac/pore rubber sponge carrier and treating water, broken film, the isolating sieve tray of mud above the fluidized-bed periphery.Fluidised bedplate is to the outstanding streamlining projection that is of inner core direction.Annular space between fluidized-bed periphery and inner core bottom be the streamlining projection around be furnished with one～three ring-type gas distribution pipe.Above-mentioned its inner core of modified version three-phase biological fluidized bed reactor and the ratio of annular space area are 1: 2～4.Three-phase biological fluidized bed reactor (hectostere volumetrical device in full) to maximizing can be made into cuboid, wherein is divided into number and picks up lattice.Odd number lattice bottom aeration upwards flows treating water, and never the even numbers lattice of aeration descend again, and the head-to-tail formation refluxes then.
Above-mentioned pore rubber sponge carrier can be the pore silicon rubber sponge sheet of rectangle, square, polygonal different thickness, and its physical dimension, size change with aerobic and double oxygen speed ratio.Because the pore silicon rubber sponge is made carrier, its surface sight density has increased its practicality as carrier almost with water etc.Commercially available powdered carbon is mixed with the pore silicon rubber sponge, and activated carbon granule is very fast to be adsorbed among each pore of sponge, gac/pore rubber sponge carrier.When carrier and sewage coexistence, a large amount of microorganism that can grow on the inside and outside surface of carrier, passing in time just can grow up to microbial film at carrier outside surface and internal surface.This duration has the proportion of biomembranous gac/pore rubber sponge carrier to be a bit larger tham water, and its free falling velocity is 1～2cm/s in the hydrostatic, therefore, and easily forms particulate fluidization, and (aeration intensity is 10m only to rely on the energy of aeration
3/ m
2More than the h), just can obtain good fluid effect.As adopt jet-flow aeration, and when fluidisation is violent, the also easily long film of carrier surface.Simultaneously, bigger carrier portability part bubble flows together, promotes water-gas distribution, increases the dissolved oxygen amount in the water.
Because gac/pore rubber sponge carrier accounts for 20～40% of fluidized-bed reactor effective volume, length has a large amount of microorganisms or microbial film on the surface of carrier, sectional area is very big in addition, the pore sponge is at water exercise, drive again that active sludge a large amount of in the water moves together and can sedimentation, so total sludge quantity substantially exceed activated sludge process (be generally 2～4g/L), contact oxidation method (4～6g/L), can reach 10～30g/L.Modified version three-phase biological fluidized bed reactor volumetric loading of the present invention is very high, reaches 5kgCOD/m approximately
3More than it, but sludge loading is still lower.Microbial biomass in the water is big, and adopts inner circulation fluidizedly, and the flow model of water is a complete mixing flow, so can bear the waste water of higher concentration, very strong impact resistance is arranged.Because gac/pore sponge carrier amount is more in reactor, in water, do the fast speed motion, its surperficial phase mutual friction, the surface biological film upgrades and is exceedingly fast.Therefore, the present invention need not dispose the required demoulding device of general fluidized-bed.
Because gac/growth of pore rubber sponge carrier surface microorganism rapidly, the surface biological film upgrades fast, the microbial film thickness of sponge appearance only has only several μ m, so the organism in the waste water is easy to see through film and enters cavernous body inside, the gac that its inside is adhered to has improved again organic enrichment and capacity of decomposition.Therefore, also produce hold concurrently oxygen or anaerobic reaction, carry out denitrogenation, dephosphorization in sponge carrier inside.The product of double oxygen or anaerobic biochemical reaction is got back to gac/pore rubber sponge carrier surface again and is carried out the aerobic biochemical reaction again easily to the outside diffusion.Therefore the inventive method can be handled the organism (as: wastewater from chemical industry) that is difficult to degrade, and makes water outlet COD content be lower than 100mg/L, obtains higher volumetric loading and good treatment effect.
Because the single volume of gac/pore rubber sponge carrier is big, be easy to separate by sieve tray and treating water etc., avoid general fluidized-bed carrier to run off easily or separated shortcoming such as trouble.Carrier is a rubber item with sponge, and tool is corrosion-resistant, under no high light condition, can not wear out, and the life-span can reach more than 5 years.Because sponge carrier of the present invention can utilize packing, processing industry depleted scrap stock to make, therefore, the price of its carrier is more cheap than general carrier.
Modified version three-phase biological fluidized bed reactor of the present invention, its shape, structure all have uniqueness.Fluidised bedplate is the streamlining projection to inner core side is outstanding, can guarantee unimpeded in cyclic motion of liquid, solid, gas three-phase material effectively and prevent reaction dead angle, bottom effectively.The design formula of streamlining projection base plate is:
y＝ 1/(A) （1+cosBX）
A＝0.1～1.0
B＝0.1～1
- (π)/(2B) ≤X≤ (π)/(2B)
The sieve tray of modified version three-phase biological fluidized bed reactor, the distribution density in its aperture and hole changes with aerobic and double oxygen speed ratio.General aperture can be grasped at 4～6mm.The distribution density in hole is (2～6) * 10
3Hole/m
2The aperture on one～three ring-type gas distribution pipe and the distribution density in hole are with the positive correlation that is varied to of organic concentration in volume, air pressure and the water of fluidized-bed reactor.
In sum, a kind of disposing waste water by biological fluidized bed with sponge carrier method of the present invention and device thereof have following advantage: (1) single carrier sectional area is big, and light specific gravity, carrier are difficult for running off.(2) biofilm, demoulding upgrade soon, do not need to use stripping machine.(3) particulate fluidization easily makes reactor maximize.(4) gas only need overcome water resistance, and the device operation energy consumption is low.(5) method is easy, and apparatus structure is simple, can be applicable to the kinds of processes flow process, and is workable.(6) the device production cost is low, not easy to wear.The inventive method and device thereof can be widely used in the wastewater treatment of industry different scales such as chemical industry, petrochemical industry, pharmacy, printing and dyeing, food, different concns.
For further specifying method of the present invention and device thereof, provide relevant accompanying drawing of the present invention here.
Accompanying drawing one: modified version three-phase biological fluidized bed reactor and settling bowl series arrangement figure.
Accompanying drawing two: modified version three-phase biological fluidized bed reactor and settling bowl polyphone drawing in side sectional elevation.
Accompanying drawing three: sieve tray structure iron.
Accompanying drawing four: streamlining projection base plate longitudinal diagram.
Accompanying drawing five: the combination flow chart of example one.
Accompanying drawing six: the combination flow chart of example two.
Accompanying drawing seven: the combination flow chart of example three.
Accompanying drawing eight: the graph of a relation in the COD～reaction times of example four.
Accompanying drawing one is label, letter explanation to the accompanying drawing seven:
A, fluidized bed body B, settling bowl
C, pressurization biological contact oxidation tower D, air flotation pool
1, water-in 2, inlet mouth
3, gac/pore rubber sponge carrier 4, inner core
5, water outlet 6, settling bowl water outlet
7, mud backflow 8, the outlet of sedimentation mud
9, fluidised bedplate 10, annular space
11, streamlining projection 12, one～three ring-type gas distribution pipe
13, sieve tray 14, sieve aperture
15, tail gas outlet (biochemical tower C pressurizes) 16, water outlet (biochemical tower C pressurizes)
Below provide and use example of the present invention, be intended to further embody innovation and creation and practicality.
Example one:
The pharmacy waste water of certain pharmaceutical factory of traditional Chinese medicine, after pre-treatment, COD is 1200～1600mg/L in the waste water, (aeration intensity is 3～4kg/cm) for combination process that employing accompanying drawing five provides and above-mentioned inventive method processing aeration.Its result makes COD below 100mg/L, reaches discharging standards.
Example two:
The dyeing waste water of certain printing and dyeing mill, COD are at 450～500mg/L, and its major ingredient is difficult biochemical organism, and combination process that employing accompanying drawing six provides and above-mentioned inventive method are handled, and (aeration intensity is 3～4kg/cm to jet-flow aeration
2).Discharge water COD is lower than 100mg/L, meets discharging standards.
Example three:
The fermentation waste water of certain microbiotic pharmacy factory mixes with rare water, the about 1000mg/L of COD, and combination process that employing accompanying drawing seven provides and above-mentioned inventive method are handled, perforated pipe aerating regulation, aeration intensity is 1～2kg/cm
2Its result, discharge water COD is lower than 300mg/L.Meet discharging standards.
Example four: (being the pilot plant test data)
Adopt the waste water of certain food factory, handle, relevant experimental data now is provided with method of the present invention:
Table 1, COD(mg/L)-reaction times (h) experimental data
The graph of a relation in relevant COD-reaction times is an accompanying drawing eight.
Table 2, COD clearance (%) and reaction times
Water sample 5,6 volumes are removed load and are respectively: 4.36,16.38kgCOD/m
3D
The combination process of the example one～three that more than provides and the testing data of related example four have proved popularity and handiness that method of the present invention and device thereof are used in the waste water treatment engineering design, have conspicuous effect and higher utility.
Claims (2)
1, a kind of method of three-phase biologic fluidized-bed processing waste water, it is characterized in that: in the modified version three-phase biological fluidized bed reactor, account for volumetric ratio and be gac/pore rubber sponge carrier of 20～40%, with under the waste water concurrent conditions at its surface and the inner generation of sponge microbial film, air passes through aeration under normal pressure or pressurized conditions, gas-water ratio is 10～20: 1 (volume ratio), air filled cavity is from the annular space bubbling, after being promoted to inner core again, descending along inner core enters annular space again and circulates, and carries out simultaneously aerobicly handling with facultative anaerobic biochemical reaction pair waste water.Described gac/pore rubber sponge carrier also circulates with the flow direction of water, drives a large amount of active sludge and contacts with air filled cavity, has accelerated biochemical reaction rate.Described gac/pore rubber sponge carrier collides mutually, rubs in flowing, and its outside biofilm detachment is upgraded.Described carrier separates by sieve tray with treating water, mud.Described facultative anaerobic biochemical reaction is carried out denitrogenation, dephosphorization in gac/pore rubber sponge carrier inside.Described aeration is that (intensity is 10m to deep aerating
3/ m
2More than the h), or perforated pipe aerating regulation (intensity is 10～20m
3/ m
2H), or jet-flow aeration (intensity is 20～50m
3/ m
2H).
2, the described modified version three-phase biological fluidized bed reactor of a kind of claim 1, comprise the fluidized-bed periphery, the fluidized-bed inner core, fluidised bedplate, gas distribution pipe, water-in, water outlet, it is characterized in that: being furnished with in the modified version three-phase biological fluidized bed reactor and accounting for volumetric ratio is gac/pore rubber sponge carrier of 20～40%, the water outlet place is equipped with and makes gac/pore rubber sponge carrier and treating water above the fluidized-bed periphery, the isolating sieve tray of mud, fluidised bedplate is to the outstanding streamlining projection that is in inner core side, annular space bottom between fluidized-bed periphery and the inner core promptly is furnished with one～three ring-type gas distribution pipe around the streamlining projection, inner core is 1: 2～4 with the area ratio of fluidized-bed annular space.Described gac/pore rubber sponge carrier, in the pore silicon rubber sponge sheet of rectangle, square or polygonal different thickness, its physical dimension, size change with aerobic and double oxygen speed ratio with charcoal absorption, and its bulk density is 10～20kg/m
3Described sieve tray aperture is 4～6mm, and the distribution density in hole is (2～6) * 10
3Hole/m
2On described one～three ring-type gas distribution pipe, be furnished with pore, the aperture becomes positive correlation with the distribution density in hole with volume, air pressure and the organism of reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN90100795A CN1020714C (en) | 1990-02-16 | 1990-02-16 | Method and apparatus for disposing waste water by biological fluidized bed with sponge carrier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN90100795A CN1020714C (en) | 1990-02-16 | 1990-02-16 | Method and apparatus for disposing waste water by biological fluidized bed with sponge carrier |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1045083A true CN1045083A (en) | 1990-09-05 |
| CN1020714C CN1020714C (en) | 1993-05-19 |
Family
ID=4876801
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN90100795A Expired - Fee Related CN1020714C (en) | 1990-02-16 | 1990-02-16 | Method and apparatus for disposing waste water by biological fluidized bed with sponge carrier |
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|---|---|
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1810679B (en) * | 2005-01-25 | 2010-06-16 | 上海市农业科学院环境科学研究所 | Frame-type biological pollutant holding and eliminating grating for purifying contaminated water |
| CN101817588A (en) * | 2010-05-10 | 2010-09-01 | 东南大学 | Activated sludge reaction separation method and device for sewage by sponge substrate |
| CN105330017A (en) * | 2015-11-26 | 2016-02-17 | 中国农业科学院农业环境与可持续发展研究所 | Anaerobic reactor as well as cultivation waste water treatment system and method |
| CN107601759A (en) * | 2017-08-29 | 2018-01-19 | 绍兴鑫广科技有限公司 | A kind of dyeing and printing sewage multi-stage combination processing system and handling process |
| CN110436624A (en) * | 2019-07-31 | 2019-11-12 | 华南理工大学 | Granule sludge composite biological film expanded bed reactor and its wastewater treatment method |
| CN110980948A (en) * | 2019-12-14 | 2020-04-10 | 浙江永续环境工程有限公司 | Facultative oxygen type flowing biological bed reactor |
-
1990
- 1990-02-16 CN CN90100795A patent/CN1020714C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1810679B (en) * | 2005-01-25 | 2010-06-16 | 上海市农业科学院环境科学研究所 | Frame-type biological pollutant holding and eliminating grating for purifying contaminated water |
| CN101817588A (en) * | 2010-05-10 | 2010-09-01 | 东南大学 | Activated sludge reaction separation method and device for sewage by sponge substrate |
| CN105330017A (en) * | 2015-11-26 | 2016-02-17 | 中国农业科学院农业环境与可持续发展研究所 | Anaerobic reactor as well as cultivation waste water treatment system and method |
| CN107601759A (en) * | 2017-08-29 | 2018-01-19 | 绍兴鑫广科技有限公司 | A kind of dyeing and printing sewage multi-stage combination processing system and handling process |
| CN110436624A (en) * | 2019-07-31 | 2019-11-12 | 华南理工大学 | Granule sludge composite biological film expanded bed reactor and its wastewater treatment method |
| CN110436624B (en) * | 2019-07-31 | 2024-04-19 | 华南理工大学 | Granular sludge composite biological membrane expanded bed reactor and wastewater treatment method thereof |
| CN110980948A (en) * | 2019-12-14 | 2020-04-10 | 浙江永续环境工程有限公司 | Facultative oxygen type flowing biological bed reactor |
| CN110980948B (en) * | 2019-12-14 | 2022-02-18 | 浙江永续环境工程有限公司 | Facultative oxygen type flowing biological bed reactor |
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| Publication number | Publication date |
|---|---|
| CN1020714C (en) | 1993-05-19 |
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