CN1547558A - Anaerobic treatment apparatus - Google Patents
Anaerobic treatment apparatus Download PDFInfo
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- CN1547558A CN1547558A CNA028167384A CN02816738A CN1547558A CN 1547558 A CN1547558 A CN 1547558A CN A028167384 A CNA028167384 A CN A028167384A CN 02816738 A CN02816738 A CN 02816738A CN 1547558 A CN1547558 A CN 1547558A
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- 239000003795 chemical substances by application Substances 0.000 claims abstract description 49
- 239000002351 wastewater Substances 0.000 claims abstract description 36
- 239000007787 solid Substances 0.000 claims abstract description 32
- 239000010802 sludge Substances 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 135
- 239000006260 foam Substances 0.000 claims description 48
- 239000007788 liquid Substances 0.000 claims description 41
- 239000002699 waste material Substances 0.000 claims description 11
- 239000002245 particle Substances 0.000 abstract description 62
- 238000011084 recovery Methods 0.000 abstract description 19
- 239000010815 organic waste Substances 0.000 abstract description 6
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 107
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 72
- 239000000377 silicon dioxide Substances 0.000 description 36
- 238000012545 processing Methods 0.000 description 27
- 238000000034 method Methods 0.000 description 22
- 238000000855 fermentation Methods 0.000 description 11
- 230000015572 biosynthetic process Effects 0.000 description 10
- 238000002474 experimental method Methods 0.000 description 10
- 238000001556 precipitation Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 230000004087 circulation Effects 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000000945 filler Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 101100532097 Vitis rotundifolia RUN1 gene Proteins 0.000 description 4
- 230000006378 damage Effects 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 230000004151 fermentation Effects 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 241001074903 Methanobacteria Species 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 238000005187 foaming Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000000247 postprecipitation Methods 0.000 description 1
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
An apparatus for anaerobic treatment of an organic waste or waste water which is an upflow anaerobic sludge blanket treatment apparatus having an anaerobic treatment vessel and a multi-stage gas-solid separator section formed by a plurality of baffles disposed within the treatment vessel, characterized in that each baffle occupies 1/2 or more of a cross-sectional area of the treatment vessel and has a means for supplying a deforming agent. The above apparatus allows, in a multi-stage UASB apparatus which does not interfere the good flow of sludge particles, i.e., the good contact of sludge particles with organic substances and thus uses all of sludge particles effectively for the treatment, the recovery with stability of a gas generated within a GSS section, which leads to the achievement of a stable waste water treatment even at a high COD load.
Description
Technical field
The present invention relates to anaerobic mud bed treatment unit, this anaerobic mud bed treatment unit is used for carrying out harmless treatment from the organic wastewater of discharges such as various factories, sewage, ight soil, livestock industry facility or organic waste etc., in more detail, relate to multistage solid (vapour-liquid is solid) separated part (the Gas-Solid Separator of gas-liquid that has; Below also claim GSS portion) the up-flow anaerobic sludge blanket treatment unit.
Background technology
Organic wastewater or organic waste etc. have the situation of carrying out separating treatment by anaerobic treatment.As such decomposing process, for example up-flow anaerobic sludge blanket method (Up flowAnaerobic Sludge Blanket is arranged; Also claim the UASB method later on).This is the method for popularizing gradually in recent years, be by in reactor, fill mud (mud particle), make organic wastewater in reactor, because of upwelling circulates, under anaerobic, the organism in the biological decomposition waste water, this mud are the mud that the microorganism based on the anerobe of methanobacteria etc. is carried out particlized.This UASB method is by turning to particulate state with the anerobe granulation; thereby has the feature that the concentration of the methanobacteria in the reactor can be remained on high density; its result is, even under the quite high situation of the organic concentration in waste water, also can handle efficiently.For example, in the device that this method is specialized, have potassium bichromate as oxygenant, even the COD that is measured
CrThe volume load of (hereinafter referred to as COD) is to be 10～15kg/m
3The waste water waste of/d also can high-efficient operation feature.
To being the anerobe of the anaerobic treatment of object,, roughly be divided into 2 kinds according to envrionment temperature with organic wastewater and organic waste.For example, have with the middle temperature area of 30～35 ℃ of envrionment temperatures anaeration in normal temperature bacterium as optimal temperature, with 50～55 ℃ high-temperature areas as high temperature anaerobic bacterium of optimal temperature etc.On the other hand, in the UASB of the function of utilizing these anerobes method, (for example the volume load of COD is more than or equal to 15kg/m if the organic charge capacity of being decomposed increases
3/ d), then the gas volume of Chan Shenging increases.At this moment, if do not carry out gas in the abstraction reaction device at any time effectively, then because the ejection when discharging gas etc., granular mud particle excessive fairly obvious is difficult to make the mud particle to remain in the reactor.
As the treatment Countermeasures of this situation, it is multistage to have proposed to make the UASB device itself to become, and the gas that dispersion is produced is with the method outside its discharge system.Fig. 1 is a mode chart (G.Lettinga (1995) Anaerobic digestion andwastewater treatment system, Antonie van Leeuwenhoek 67:3-28) of UASB being made multistage anaerobic processing device.Device shown in Figure 1 is the inside at the reactor 2 of tubular, be arranged alternately downward-sloping a plurality of baffle plates 3, form in each position multistagely and to have divided in the reactor and the precipitation zone 4a-4e that is divided into, the reactor 2 of this tubular is connected with former water inflow pipe 1 in the lower end.The bight of the upper end of the precipitation zone 4a-4e of each division (that is the obstruction portion that, is formed by baffle plate) forms GSS portion 5.Mud particle at inside reactor filler particles shape.If from the lower end of such device, drop into organic wastewater (former water), then, decompose the organism in the former water by being present in the effect of the anaerobion in the inner granular mud particle, produce gas.In the bottom of reactor, owing to be the state of high capacity, the gas of generation is more, so the gas that produces attached on the mud particle, makes its bulk specific gravity reduce, the gas that adheres to simultaneously is accompanied by the mud particle, and along the current that make progress, the mud particle flows upward.The mud particle that is accompanied by gas is caught by the formed GSS of baffle plate 3 portion 5, becomes bubble at the water surface, forms the bubble 5b of portion.Bubble breaks soon, and gas accumulation forms the gas phase 5a of portion in GSS portion 5.In the position that forms the gas phase 5a of portion, connect the recovery pipe arrangement 6 that produces gas, reclaim gas.The recovery pipe arrangement 6 that produces gas is connected on the outside water sealed tank 7, and gas is enclosed in the water sealed tank 7.Because of collapse of bubbles, gas and mud separate particles, the mud particle returns to original proportion, because of gravity precipitates.Be deposited to the mud particle landing from the surface of baffle plate 3 on one side on the baffle plate 3, further precipitate on one side.The mud particle of post precipitation contacts with organism in the former current once more, because the anaerobion decomposing organic matter in the mud particle, and gas is produced, the mud particle follows gas to rise.
Inside at reactor, the cyclic motion of mud particle as described above has taken place, but because reclaimed by the GSS below the reactor at the gas that is produced below the reactor, so along with moving to the reactor top, because of the influence that is caused of flowing to the mud particle of the gas that produces below reactor reduces, because organic charge capacity slowly reduces, so the generation of gas reduces, accompany therewith, the bulk specific gravity of mobile mud particle increases, the speed of upwelling that is accompanied by the mud particle of gas reduces, that is, the mobile of mud particle slows down.
So, the treating water that organism is carried out after the anaerobic treatment overflows from the upper end of reactor 2, is discharged from by treating water pipe arrangement 9.As above-mentioned, because the flowing of mud particle along with slowing down, promptly near stationary state, so in the overflow of the upper end of coming autoreactor, do not contain the mud particle, the treating water that can obtain cleaning to the moving of top of reactor.
But the UASB device of multipolarity also has problem shown below now.
(1) because the characteristic of waste water at the inner bubble that produces of GSS portion, causes the obstruction of the capture pipe arrangement of GSS portion inside or generation gas, the gas that is difficult to capture generation.
(2) because the characteristic of waste water forms scum silica frost, the gas that is difficult to capture generation in GSS portion inside.Under the few situation of gas volume particularly low, that produce, reduce, form scum silica frost easily because of the gas that produces makes the destruction of scum silica frost remove effect in load.
(3) result of above-mentioned (1), (2) has disperseed the gas that is produced as the speciality of the UASB device of multipolarity, has lost the effect that is discharged to outside the system, causes the too much excessive of mud, becomes to handle the reason that worsens.
(4) angle that is provided with at the baffle plate that constitutes GSS portion is that mud is deposited on the baffle plate, produces the mud dead angle under the mild situation, and existence can not be used the situation of the whole mud particles in the reactor effectively.
(5) under the situation of the bottom that the GSS part device is formed into always reactor, hindered good the flowing of mud particle, exist the mud particle to contact insufficient or condition of poor with organic.
(6) under the situation that the water flowing speed in reactor is low, produce shortcut stream, on the contrary, under the fast situation of water flowing,, the situation that becomes the reason that makes the result deterioration is arranged owing to can cause the excessive of mud.
In view of such truth, the present invention is to be purpose so that a kind of anaerobic processing device to be provided, this anaerobic processing device is in the good flow state of mud particle, that is, can not hinder mud particle and organic good the contact, with respect to processing, use effectively in all multipolarity UASB devices of mud particle, carry out even in high COD load, also can carrying out stable wastewater treatment to stable recovery at the inner gas that produces of GSS portion.
Summary of the invention
The present invention provides the anaerobic processing device of relevant following each mode as the method that is used to solve above-mentioned problem.
The invention of claim 1 of the present invention is relevant a kind of device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, the occupied area of each baffle plate has the mechanism that supplies with foam eliminating agent in treatment trough more than or equal to 1/2nd of the cross-sectional area of treatment trough.
The invention of claim 2 of the present invention is relevant a kind of devices that are used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is installed as and the treatment trough inwall between angle be less than or equal to 35 degree, and its occupied area is more than or equal to 1/2nd of the cross-sectional area of treatment trough.
The invention of claim 3 of the present invention is relevant devices as claimed in claim 2, also has the mechanism that supplies with foam eliminating agent in treatment trough.
The invention of claim 4 of the present invention is relevant a kind of devices that are used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is installed as and the treatment trough inwall between angle be less than or equal to 35 degree, have the mechanism that in treatment trough, supplies with foam eliminating agent.
The invention of claim 5 of the present invention is relevant to each the described device in the claim 1 to 4, it is characterized in that, vapour-liquid consolidate separated part inside or below dispose gas supply pipe, this gas supply pipe is used to be blown into the gas that does not contain aerobic.
The invention of claim 6 of the present invention is relevant to each the described device in the claim 1 to 5, and vapour-liquid is consolidated in the scope on top 50% that separated part is installed in treatment trough.
The invention of claim 7 of the present invention is relevant to each the described device in the claim 1 to 6, and the former water throughput in treatment trough is controlled at 1～5m/h.
Description of drawings
Fig. 1 is the figure that represents the configuration example of Multistage U ASB device in the past.
Fig. 2 is the figure of expression about the configuration example of the Multistage U ASB device of a mode of the present invention.
Fig. 3 is the figure of expression about the configuration example of the Multistage U ASB device of other modes of the present invention.
Fig. 4 is the figure of expression about the formation of the Multistage U ASB device of an employed mode of the present invention in embodiment 2.
Fig. 5 is the figure of formation that is illustrated in the Multistage U ASB device of employed relatively usefulness among the embodiment 2.
Fig. 6 be illustrated among the embodiment 2, COD handles achievement chart over time.
Fig. 7 is the figure that is illustrated in the formation of employed various Multistage U ASB devices among the embodiment 3.
Fig. 8 is illustrated in COD processing achievement among the embodiment 3, in the waste water experiment (RUN1) of using refreshment drink chart over time.
Fig. 9 be illustrated among the embodiment 3, in the waste water experiment (RUN2) of using food, handle achievement chart over time with COD.
Embodiment
Below, embodiments of the present invention are described, but the present invention is not limited to this.Fig. 2 is the figure of expression about the summary of an embodiment of the Multistage U ASB device of the 1st mode of the present invention.In addition, in the accompanying drawings,, give identical reference numbering to identical integrant.
In the Multistage U ASB device relevant with a mode of the present invention shown in Figure 2, by inside at the reactor 2 of tubular, a plurality of baffle plates 3 are set, and multistage formation has been divided the inside of reactor 2 and the precipitation zone that is divided into, and the reactor 2 of this tubular connects former water inflow pipe 1 in the lower end.The end of baffle plate 3 one sides is fixed on the inwall of reactor 2, and the opposing party's end is towards the inwall direction of reverse side, downward-sloping elongation.In Fig. 2,2 downward-sloping baffle plates 3 have been represented to dispose, the configuration example of multistage formation 2 precipitation zone 4a, 4b.(the obstruction portion that forms because of baffle plate 3) forms GSS portion 5 in the bight of the upper end of each section precipitation zone 4a, 4b.At inside reactor, the mud particle of filler particles shape.Organic wastewater (former water) passes supply-pipe 25, at first after former water is adjusted groove/acid-fermentation groove 23 adjustment, passes former water inflow pipe 1, drops into from the lower end of reactor 2.In addition, not former water must will be set adjust groove/acid-fermentation groove 23, also can directly reactor 2 be arrived in former water supply.In addition, particularly under unnecessary situation, also can in groove 23, not carry out the adjustment of former water.
In reactor 2, fill the particulate state mud particle that constitutes by anerobe.As the anaerobic treatment of object of the present invention is to be that the mesophilic methane fermentation of proper temperature is handled with 30 ℃～35 ℃, is that the anaerobic treatment of all temperature ranges of the high temperature methane fermentation processing etc. of proper temperature is an object with 50 ℃～55 ℃.The former water that contains organic waste etc. is imported into the lower end of reactor 2 by liquid pushing tube 1, and this reactor 2 is filled with the particulate state mud particle that is made of anerobe.Former water after the dilution water of supplying with by the circulation fluid for the treatment of water or outside system etc. suitably dilutes, can supply to reactor as required.Wishing to flow into the water flowing speed that the amount of former water is adjusted in reactor 2 inside is 1～5m/h.
In reactor 2, Jie of the particulate state mud particle by containing anerobe exists, and decomposes organic waste, produces decomposition gas.The gas that produces collects in the GSS portion 5 of upper end of precipitation zone 4a, the 4b of each section respectively, forms bubble 5b of portion and the 5a of gas phase portion on each, passes the recovery pipe arrangement 6 that produces gas from the 5a of gas phase portion, is recycled to water sealed tank 7.Gas for the generation of being reclaimed writes down its outputs by gas table 8.In section precipitation zone 4a, 4b, the part of the gas that is produced in reactor alleviates its bulk specific gravity attached on the particulate state mud particle, follows particulate state mud particle to arrive the water surface of GSS portion 5 simultaneously.Like this, the gas of generation forms bubble, and layover is in the water surface bubble 5b of portion.The bubble that compiles in the water surface bubble 5b of portion breaks soon, the gas and the particulate state mud separate particles that produce, particulate state mud particle returns to original proportion, be deposited in the water, on the other hand, the gas that produces forms the gas phase 5a of portion, and the recovery pipe arrangement 6 process water sealed tanks 7 from produce gas here with being connected are discharged to outside the system.The treating water that decomposites organism and become limpid overflows from the reactor upper end, and treated water pipe arrangement 9 is discharged to outside the system.
In addition, as shown in Figure 2,, constitute treating water circulation pipe arrangement 21,, adjust groove/acid-fermentation groove 23 circulations, as required, after adjusting again, can be recycled to reactor 2 once more at former water by pipe arrangement 24 with treating water pipe arrangement 9 branches.In addition, configuration bypass pipe 22 can be recycled to the treating water original state reactor 2.
Because the gaseous tension difference of the 5a of gas phase portion of each GSS portion 5 is so its pressure reduction can be adjusted at water sealed tank 7.Need keep higher water seal pressure according near the order of former water liquor charging side the GSS portion of below (promptly the closer to).This is to reduce (with reference to Fig. 2) that finish the peristome position in water sealed tank 7 by the recovery pipe arrangement 6 that makes the generation gas that is connected with the GSS portion of below.The adjustment of gas recovery pressure also has a lot of methods except that the method for using water sealed tank 7, for example also can the applying pressure valve etc.In anaerobic treatment of the present invention, owing to can be recovered in the generation gas that this place produces, so reduced the generation gas volume of the cross-sectional area of every reactor unit in each section precipitation zone.Particularly in the most approaching position that makes the effusive treating water pipe arrangement 9 for the treatment of water, the gas volume of the cross-sectional area of every reactor unit is very little.Therefore, the amount that particulate state mud particle is flowed out to outside the system is very little.
, wish to be configured in the baffle plate 3 of the inside of reactor 2 here, its occupied area is 1/2 a size more than or equal to the cross-sectional area of treatment trough.If the occupied area of baffle plate 3 is in below 1/2 of cross-sectional area of treatment trough, then by baffle plate, it is insufficient to catch the gas that produces in reactor, has problems in the solid separation of vapour-liquid.That is,, can not fully gas be collected in GSS portion 5 from the centre portions of reactor extracting gases upward.
In addition, the former water of handling at need is under the situation of foaminess, and 5a of gas phase portion in the GSS portion 5 and recovery pipe arrangement 6 obstructions that produce gas are difficult to reclaim the gas of generation.Therefore, in a mode of the present invention,, can be suppressed at the foaming in the GSS portion 5, can handle without barrier by foam eliminating agent being supplied in the reactor 2.As the method for in reactor 2, supplying with foam eliminating agent, for example, as shown in Figure 2, foam eliminating agent is injected pipe arrangement 10 be connected with former water liquid pushing tube 1, can in former water, add foam eliminating agent in advance.In addition, as other form, foam eliminating agent can or pass through drippage or spraying, supply to former water and adjust groove/acid-fermentation groove 23 (Fig. 2 2.), or supply to treating water circulation pipe arrangement (Fig. 2 5., 6. or 7.), or by direct drippage or spray, put into reactor 2 (Fig. 2 4.), or, supply to the GSS portion 5 (Fig. 2 3.) of reactor by drippage or spraying.As foam eliminating agent, wish to use to have the go out bubble effect corresponding with the characteristic of former water, be suitable for the bubble that goes out of fermented liquid, in middle temperature (30 ℃～35 ℃) or high temperature (50 ℃～55 ℃), can not lose the foam eliminating agent of the bubble effect of going out.As operable foam eliminating agent in the present invention, go for any one of silicon class foam eliminating agent or alcohol type foam eliminating agent.
The 1st mode of the present invention relates to the anaerobic processing device with above-mentioned feature.Promptly, the 1st mode of the present invention is relevant a kind of device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage vapour-liquid, the solid separated part of this multistage vapour-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, the occupied area of each baffle plate has the mechanism that supplies with foam eliminating agent in treatment trough more than or equal to 1/2nd of the cross-sectional area of treatment trough.
In addition, the 2nd mode of the present invention is characterized in that, be baffle plate is mounted to and the treatment trough inwall between angle be less than or equal to 35 the degree.Promptly, the 2nd mode of the present invention is relevant a kind of device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage vapour-liquid, the solid separated part of this multistage vapour-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is mounted to and the treatment trough inwall between angle be less than or equal to 35 degree, and its occupied area is more than or equal to 1/2nd of the cross-sectional area of treatment trough.
If with reference to Fig. 2, the 2nd mode of the present invention is described, then in relevant mode, is less than or equal to 35 degree by inwall and the angle θ between the baffle plate 3 that makes reactor 2, baffle plate 3 is installed, make its inwall towards reverse side, downward-sloping, can eliminate following problems, promptly on the baffle plate 3 that forms precipitation zone 4a, 4b, particulate state mud particle deposition from the top precipitation is come causes flowability insufficient, the dead angle that produces the mud particle.If the inwall of reactor 2 and the angle between the baffle plate 3 then because produce the accumulation of above-mentioned mud particle, are easy to generate the dead angle of mud particle, so be difficult to carry out 30kg/m more than 35 degree
3The above high capacity of/d is handled.If the angle θ between the inwall of baffle plate 3 and reactor 2 is less than or equal to 35 degree, then form by baffle plate because surmounted the inclination at the slope of repose of mud particle, also since the mud particle landing on one side from the surface of baffle plate that is deposited on the baffle plate flow down on one side, so mud can not be stacked on the baffle plate.Relatively wish between this baffle plate and the reactor wall angle 30 the degree below, more wish 27 the degree below.
In addition, even in the 2nd mode of the present invention, also hope is configured in the baffle plate 3 of the inside of reactor 2, and its occupied area is the size more than 1/2 for the cross-sectional area of treatment trough.If the occupied area of baffle plate 3 is in below 1/2 of cross-sectional area of treatment trough, then the seizure carried out of the baffle plate by the gas that produces in reactor is insufficient, has problems in the solid separation of vapour-liquid.That is,, can not fully gas be collected in the GSS portion 5 from the centre portions of reactor extracting gases upward.
In addition, in the 2nd mode of the present invention, adding foam eliminating agent is not must condition.But, identical with the 1st mode, if foam eliminating agent can be supplied in the reactor, be suppressed at the foaming in the GSS portion 5, then better.
Have again, the 3rd mode of the present invention is relevant a kind of device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage vapour-liquid, the solid separated part of this multistage vapour-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is installed as and the treatment trough inwall between angle be less than or equal to 35 degree, have the mechanism that in treatment trough, supplies with foam eliminating agent.
In addition,, forming under the situation of scum silica frost easily, existing surface 5b of bubble portion and inner formation scum silica frost GSS portion 5 in, be difficult to reclaim the situation of the gas of generation because former water is the reason of high SS etc.Under these circumstances, by gas supply pipe being configured in the inside or the below of GSS portion 5, supply gas can or destroy scum silica frost, or prevents the formation of scum silica frost.As the gas that can be used for such purpose, can use the oxygen of nonnitrogenous gas etc., not the gas that can impact to the biological treatment of methane fermentation etc.In addition, also can be with the gas that produces because of anaerobic treatment, as destroying scum silica frost or preventing that the gas that forms usefulness from using.The configuration example of the anaerobic processing device of relevant mode, as shown in Figure 3.
In device shown in Figure 3, by passing recovery pipe arrangement 6 and the water sealed tank 7 that produces gas, the gas of the generation of being reclaimed is remained in the gas conservator 11, from passing the supplying tubing 13 that produces gas here, supply to the diffuser 12 of the below that is arranged on each GSS portion, as bubble, or supply with from the below of GSS portion, or supply to the recovery pipe arrangement 6 that produces gas, directly supply to the inside of GSS portion, thereby reach or destroy scum silica frost in GSS portion, or prevent the formation of scum silica frost.
The supplying tubing 13 that produces gas is connected with the recovery pipe arrangement 6 of the generation gas of each GSS portion, under the situation of the scum silica frost in destruction is removed the 5-1 of GSS portion, valve-off 14a, be blown in the 5-1 of GSS portion by the gas that will produce, with in the 5-1 of GSS portion all as the 5-1a of gas phase portion, depress the 5-1b of bubble portion downwards, scum silica frost can be discharged from the 5-1 of GSS portion.Because the scum silica frost that will discharge is enclosed in the 5-2 of GSS portion above it, so follow valve-off 14b, be blown in the 5-2 of GSS portion by the gas that will produce equally, with in the 5-2 of GSS portion all as the 5-2a of gas phase portion, depress the 5-2b of bubble portion downwards, scum silica frost can be discharged from the 5-2 of GSS portion, itself and treating water are together flowed out.
In addition, be connected under the situation of diffuser 12 in the supplying tubing 13 that will produce gas, this diffuser 12 is configured in the below of each GSS portion, and owing to the bubble that is blown into from diffuser 12 destroys scum silica frost, the liquid stream in ruined scum silica frost and the reactor 2 is together discharged as treating water.Under the situation of this method, the not switching of tube valve 14.If Open valve 14 carries out above-mentioned operation, then, reclaim the gas that is blown into from diffuser 12 by producing the recovery pipe arrangement 6 of gas.On the other hand, if valve-off 14, carry out above-mentioned operation, then add the execution of the scum silica frost that bubble produced that is blown into from diffuser 12, also can expect directly to supply gas to the discharge effect of the scum silica frost that inside produced of GSS portion by passing the recovery pipe arrangement of generation gas.To destroy scum silica frost or to prevent to form scum silica frost is purpose, to GSS portion 5 in or the frequency of diffuser supply gas, also according to the character situation of handling waste water, from 1 time on the 1st to 1 week 1 time, all have destruction to remove the effect of the scum silica frost of GSS portion 5 inside.
In addition, in relevant Multistage U ASB device of the present invention, wish that relatively the solid separated part of vapour-liquid only forms on the top of treatment trough.This is because as if the bottom that the solid separated part of vapour-liquid is installed in up to treatment trough, the good flow that then hinders the mud particle in treatment trough causes mud and organic loose contact, has the unsettled situation of handling.From then on viewpoint is set out, and in relevant Multistage U ASB device of the present invention, wishes the solid separated part of vapour-liquid is installed in the scope on top 70% of treatment trough, and what relatively wish is in the scope on top 50%, and what more wish is in the scope on top 30%.
In addition, in Multistage U ASB device of the present invention, hope is controlled at 1～5m/h with the former water throughput in treatment trough.If the throughput in groove is too small, then exist at sludge blanket and produce shortcut stream, can not effectively use all situations of sludge blanket.In addition, if throughput in groove is excessive, then because the upwelling speed of liquid greater than the sedimentation speed of particulate state mud particle, particulate state mud particle and the outflow for the treatment of water one, so can not stably mud be remained in the groove, have the unsettled situation of handling.From then on viewpoint is set out, and hope is controlled at 1～5m/h with the former water throughput in treatment trough, more wishes to be controlled at 2～3m/h.
Below, by embodiment, specifying variety of way of the present invention, the present invention only is defined in these embodiment.
Embodiment 1
Use device shown in Figure 2, carry out the anaerobic treatment of waste water.At cross-sectional area 0.16m
2, high 6.25m (tankage 1m
3) barrel type reactor 2 in, 2 baffle plates 3 are installed, make it downward-sloping, it is 0.112m that each of this baffle plate 3 occupies cross-sectional area
2(cross-sectional area of reactor 70%).The setting angle of baffle plate 3 (θ) is 45 degree.Water temperature in the reactor 2 is controlled at 35 ℃.The mud particle of filler particles shape in reactor 2.
As former water, use acid-fermentation treating water (COD=10, the 000mg/L of the refreshment drink waste water of foaminess; SS=500mg/L).The treating water that will overflow from the upper end of reactor 2 by with former water inflow reactor 2, is 2m/h with the water flowing speed setting as circulation fluid.According to the COD load, set the ratio of raw water flow and treating water quantity of circulating water.
The result of table 1: embodiment 1
| Foam eliminating agent injects | Do not have | Have |
| COD volume load (kg/m 3/d) | ????15 | ????25 |
| COD removes rate (%) | ????90 | ????90 |
| Treating water VSS (mg/L) | ????300～400 | ????300～400 |
Can understand from the result of last table,, in Multistage U ASB treatment unit,, can obtain excellent handling property by foam eliminating agent is supplied in the treatment trough according to the present invention.Under the situation of not supplying with foam eliminating agent, because of the rising of load, produce bubble in the inside of GSS portion, handling property is reduced.
In anaerobic processing device shown in Figure 2, as reactor 2, use the reactor of Fig. 4 and structure shown in Figure 5, experimentize.In reactor shown in Figure 42, the baffle plate 3 of 2 inclinations is installed, the angle (θ) that makes device sidewall and baffle plate 3 is 30 degree.3 on baffle plate is configured on the position on top 50% of reactor 2.On the other hand, in reactor shown in Figure 52, around the overall height of reactor 2, the baffle plate 3 of 5 inclinations is installed, the angle (θ) that makes device sidewall and baffle plate 3 is 45 degree.
All be that cross-sectional area with reactor is 0.16m
2, highly be 6.25m (capacity 1m
3), the cross-sectional area that forms the baffle plate of GSS portion is 0.112m
2(cross-sectional area of reactor 70%) experimentizes.
The mud particle of filler particles shape in reactor 2.Former water liquid pushing tube that former water is connected from the lower end with reactor 21 flows into, and obtains treating water from the processing water pipe 9 on reactor 2 tops.
In reactor 2, form GSS portion 5 by baffle plate, in the top, the relief outlet of the recovery pipe arrangement 6 of the generation gas of setting and external communications, the gas that this GSS portion 5 produces when being collected in decomposition, purifying organic.By being arranged on the gas table 8 on the water sealed tank 7, measure the amount of the gas that is produced by each GSS portion 5.Water temperature in the reactor 2 is controlled at 35 ℃.As former water, use in the acid-fermentation treating water (COD=7000mg/L) of saccharic class waste water, added the former water of inorganic nutrients salts (nitrogen, phosphorus etc.).As circulation fluid, by making together inflow reactor 2 of itself and former water, is 2m/h with the water flowing speed setting with treating water.According to the load of COD, set the ratio of raw water flow and treating water quantity of circulating water.As B series, will use the resulting result of reactor 2 (setting angle of baffle plate is 45 degree) of Fig. 5 to be reported as follows the resulting result of reactor 2 (setting angle of baffle plate is 30 degree) that uses Fig. 4 as A series.
Fig. 6 represent to test through with the variation of the processing achievement of COD.Two series all are on one side with reference to treating water COD concentration, Yi Bian improve the organism charge capacity gradually.
After experiment,, can handle with roughly the same charge capacity by about the 120th day.After about 120 days, as if the 30kg/m that loads on of COD
3More than/the d, then in A series, treating water COD increases.
At the inwall of the baffle plate that 5 inclinations are installed, reactor 2 and the angle of baffle plate 3 is in the A series of 45 degree, as shown in Figure 5, because of the mud of piling up, produces the dead angle on baffle plate 3, owing to can not use the mud particle all effectively, handles unstable.Therefore, the COD load drops to 25kg/m
3/ d.
On the other hand, in B series, be 35kg/m in the COD load
3During/d, can carry out stable treated.Table 2 is illustrated in the comparison of the processing achievement in the steady state.
The result of table 2: embodiment 2
| A series | B series | |
| The setting angle of baffle plate | ????45° | ????30° |
| COD volume load (kg/m 3/d) | ????25 | ????35 |
| COD removes rate (%) | ????90 | ????90 |
| Treating water VSS (mg/L) | ????300～400 | ????300～400 |
In the setting angle of baffle plate was 30 ° B series, the COD load was 35kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.On the other hand, in the setting angle of baffle plate was 45 ° A series, the COD load was 25kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.Like this, be below 35 degree by the setting angle that makes baffle plate, be that 45 situations about spending are compared with the setting angle of baffle plate, can obtain high COD and remove rate.
In the method for B series, and be not limited to running under high COD load, the processing achievement for the treatment of water COD is stable.In addition, the method for the treatment of water VSS concentration and A series is roughly the same, even comparing with the method for A series, under the few situation of the quantity of GSS portion, the particulate state sludge quantity in up-flow anaerobic sludge blanket method (UASB) groove is also stable.This is because in the position nearest with making the effusive treating water pipe arrangement for the treatment of water 9, the gas volume of the unit cross-sectional area of each reactor reduces, and makes the discharge minimizing of particulate state mud to system outside.
Then, using B series, is 7000g/L in former water COD concentration, and the COD load is 30kg/m
3/ d, when water flowing speed is 0.5～7m/h, the comparison of the processing achievement in the frequent state when handling, as shown in table 3.
Table 3
| Water flowing speed (m/h) | ??0.5 | ????1 | ????2 | ????3 | ????5 | ????6 | ????7 |
| COD removes rate (%) | ??80 | ????85 | ????90 | ????92 | ????85 | ????78 | ????70 |
| Treating water VSS (mg/L) | ??300 | ????340 | ????320 | ????340 | ????500 | ????1500 | ????2100 |
In the angle of baffle plate and reactor wall in the B series of 30 degree, remove rate in the stabilizing treatment more than 85% in order to carry out COD, in water flowing speed is 1～5m/h, wishes that COD removes rate under the situation more than 90%, can understand hope with the water flowing speed setting at 2～3m/h.This is because under the situation that water flowing speed is lacked than 1m/h, flow owing to produce shortcut at sludge blanket, thereby can not effectively use sludge blanket all.In addition, under the water flowing speed situation higher than 5m/h, the VSS for the treatment of water is more than the 1500mg/L, because can not make the sludge quantity in the reactor 2 keep stable, so the property handled deterioration.
As reactor 2, use various forms of reactors shown in Figure 7.A series is that the baffle plate of 2 inclinations is installed, and making the inwall of reactor 2 and the angle of baffle plate 3 is 30 degree.B series is foam eliminating agent to be injected pipe arrangement 10 be connected with the former water liquid pushing tube 1 of the reactor 2 of A series, goes into the ratio that the water yield is 10mg/L with every reactor stream, and the silicon class foam eliminating agent as foam eliminating agent is added in the former water.C series is that diffuser 12 further is installed on the reactor 2 of B series, by passing the supplying tubing 13 that produces gas, supplies with the gas that produces, and destroys the scum silica frost of removing in GSS portion.All be that GSS portion is configured in the scope on top 50% of reactor 2.
In experiment, use device shown in Figure 3.In reactor 2, the mud particle of filler particles shape.By the former water liquid pushing tube 1 that the lower end with reactor 2 is connected, supply with former water, the processing water pipe 9 by reactor 2 tops obtains treating water.In reactor 2, by baffle plate 3, form GSS portion 5, connect the recovery pipe arrangement 6 that produces gas, the gas (with reference to Fig. 3) that this GSS portion 5 produces when being collected in decomposition, purifying organic in the top.
In each series, the cross-sectional area of reactor is 0.16m
2, height is 6.25m (capacity 1m
3), the cross-sectional area that forms the baffle plate of GSS portion is 0.112m
2(cross-sectional reactor area 70%).By being arranged on the gas table 8 on the water sealed tank 7, the gas volume that metering is produced by each GSS portion 5.Water temperature in the reactor 2 is controlled at 35 ℃.As former water, use acid-fermentation treating water (RUN1 at the refreshment drink waste water of foaminess; COD=10,000mg/L SS=500mg/L) and easily forms the acid-fermentation treating water (RUN2 of the food mfg waste water of scum silica frost; COD=10,000mg/L, SS=300mg/L) in, added the former water of inorganic nutrients salts (nitrogen, phosphorus etc.).As circulation fluid, by making together inflow reactor 2 of itself and former water, is 2m/h with the water flowing speed setting with treating water.According to the load of COD, set the ratio of raw water flow and treating water quantity of circulating water.
Fig. 8 and Fig. 9 represent to test the variation of process and COD processing achievement.Two series all are on one side with reference to treating water COD concentration, Yi Bian improve the organism charge capacity gradually.
In the RUN1 (Fig. 8) that uses refreshment drink waste water,, can handle with roughly the same charge capacity up to through about the 80th day after the experiment.After about 80 days, if the load of COD is 20kg/m
3/ d, then in A series, treating water COD increases.In not adding the A series of foam eliminating agent, because the rising of load, the gas volume of generation increases, at the GSS portion 5 inner bubbles that produce, the recovery pipe arrangement 6 that has blocked GSS portion 5 and produced gas.Therefore, because can not reclaim the gas of generation, so be discharged to atmosphere from the top of reactor 2 in GSS portion.Its result is that the particulate state sludge quantity in the reactor 2 flows out in a large number, owing to the mud that can not stably keep in the reactor 2, so handling property reduces.Therefore, though 15kg/m is reduced in the COD load
3/ d can not produce bubble, but because at the GSS portion 5 inner scum silica frost that form, can not reclaim the gas of generation in GSS portion 5, so as mentioned above, handling property is still low.On the other hand, in the B that has added foam eliminating agent, C series, be 35kg/m in the load of COD
3During/d, can stably handle.Under difficult situation, by adding foam eliminating agent, can carry out high capacity and handle, because the gas volume that produces increases, so have the 5 inner effects that form scum silica frost that prevent that gas because of this generation brings in GSS portion with the waste water that forms scum silica frost.Therefore, B series is identical with the handling property of C series.Table 4 is the comparisons that are illustrated in the processing achievement in the frequent state.
Table 4: the processing experiment (RUN1) of refreshment drink waste water
| A series | B series | C series | |
| Foam eliminating agent adds | Do not have | Have | Have |
| Scum silica frost is removed | Do not have | Do not have | Have |
| COD volume load (kg/m 3/d) | ????15 | ????35 | ????35 |
| COD removes rate (%) | ????90 | ????90 | ????90 |
| Treating water VSS (mg/L) | ????300～400 | ????300～400 | ????300～400 |
In being added with the B series of foam eliminating agent, the load of COD is 35kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.On the other hand, in not adding the A series of foam eliminating agent, the load of COD is 15kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.Like this,, compare, can obtain high COD and remove rate with the situation of not using foam eliminating agent by adding foam eliminating agent.In the method for the B series that is added with foam eliminating agent, whether no matter turn round with high COD load, the processing achievement for the treatment of water COD is still stable.In addition, treating water VSS concentration is roughly the same with the situation of not adding foam eliminating agent.
Then, in the RUN2 (Fig. 9) that uses food mfg waste water, after through about the 80th day after the experiment, if the load of COD is 15kg/m
3More than/the d, then in not adding the A series of foam eliminating agent, treating water COD increases.Can consider this be because, by the formation of bubble GSS portion 5 in and scum silica frost, resemble above-mentioned insufficiently owing to produce the recovery of gas, therefore can not stably keep the sludge quantity in the reactor 2, thereby cause the handling property reduction.Therefore, though 10kg/m is reduced in the COD load
3/ d can not produce bubble, but because at GSS portion 5 inner formation scum silica frost, thereby handling property is still reduced.
In being added with the B series of foam eliminating agent,, be 20kg/m with the COD load set through about the 110th day after the experiment
3/ d.From the 110th day～the 120th day, begin to form scum silica frost in GSS inside, then handle and worsen, after the 120th day, treating water COD increases.Can consider this be because, though can be suppressed at the bubble of GSS portion 5 inside owing to then form scum silica frost, the recovery that produces gas resemble above-mentioned and insufficient, thereby can not stably keep sludge quantity in the reactor 2, cause the handling property reduction.
From the C series of the underfeed gas of GSS portion, be 35kg/m in the load of COD
3During/d, can stably handle.Under the situation of the waste water that forms easily scum silica frost, add and added foam eliminating agent, by producing destruction that gas carries out and remove scum silica frost in the GSS portion 5, thereby can carry out the high capacity processing because of being blown into.Table 5 is the comparisons that are illustrated in the processing achievement in the frequent state.
Table 5: the processing experiment (RUN2) of food mfg waste water
| A series | B series | C series | |
| Foam eliminating agent injects | Do not have | Have | Have |
| Scum silica frost is removed | Do not have | Do not have | Have |
| COD volume load (kg/m 3/d) | ????10 | ????15 | ????35 |
| COD removes rate (%) | ????90 | ????90 | ????90 |
| Treating water VSS (mg/L) | ????300～400 | ????300～400 | ????300～400 |
In being added with the B series of foam eliminating agent, the COD load is 35kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.On the other hand, in not adding the A series of foam eliminating agent, the COD load is 10kg/m
3/ d, the COD rate of removing is 90%, treating water VSS=300～400mg/L.Have, in the method that prevents the C series that scum silica frost forms, whether no matter turn round with high COD load, the processing achievement for the treatment of water COD is still stable again.In addition, treating water VSS concentration and method in the past are much at one.
According to the 1st mode of the present invention, it is a kind of up-flow anaerobic sludge blanket treatment unit with the solid separated part of multistage vapour-liquid, the solid separated part of this vapour-liquid is to form on treatment trough by baffle plate, by foam eliminating agent is supplied in the treatment trough, even in high COD load, also can carry out anaerobic treatment stably.In addition, according to the 2nd mode of the present invention, by making the baffle plate and the angle between the treatment trough inwall that form the solid separated part of vapour-liquid be less than or equal to 35 degree, can prevent that the mud particle from piling up on baffle plate, produce the dead angle of mud particle, thereby keep the good flow state of mud particle,, can effectively utilize the mud particle all with respect to processing.Have again, be less than or equal to 35 degree, in treatment trough, supply with foam eliminating agent simultaneously, can seek further stably to handle by making the angle between baffle plate and the treatment trough inwall.Have again, prevent the device that scum silica frost forms by further configuration, even in high COD load, also can more stably handle.
Claims (7)
1. device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, the occupied area of each baffle plate has the mechanism that supplies with foam eliminating agent in treatment trough more than or equal to 1/2nd of the cross-sectional area of treatment trough.
2. device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is installed as and the treatment trough inwall between angle be less than or equal to 35 degree, and its occupied area is more than or equal to 1/2nd of the cross-sectional area of treatment trough.
3. device as claimed in claim 2 is characterized in that, also has the mechanism that supplies with foam eliminating agent in treatment trough.
4. device that is used for organic wastewater or waste are carried out anaerobic treatment, it is up-flow anaerobic sludge blanket treatment unit with anaerobic treatment groove and the solid separated part of multistage gas-liquid, the solid separated part of this multistage gas-liquid is formed by a plurality of baffle plates that are installed in this treatment trough, it is characterized in that, each baffle plate is installed as and the treatment trough inwall between angle be less than or equal to 35 degree, have the mechanism that in treatment trough, supplies with foam eliminating agent.
5. as each the described device in the claim 1 to 4, it is characterized in that, the inside of the solid separated part of vapour-liquid or below dispose gas supply pipe, this gas supply pipe is used to be blown into the gas that does not contain aerobic.
6. as each the described device in the claim 1 to 5, it is characterized in that the solid separated part of vapour-liquid is installed in the scope on top 50% of treatment trough.
7. as the described device that is used for organic wastewater or waste are carried out anaerobic treatment of in the claim 1 to 6 each, it is characterized in that, the former water throughput in treatment trough is controlled at 1～5m/h.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP350063/2001 | 2001-11-15 | ||
| JP2001350063 | 2001-11-15 |
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|---|---|
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| JP (1) | JP4162234B2 (en) |
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| WO (1) | WO2003042116A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102616929A (en) * | 2012-03-21 | 2012-08-01 | 天津科技大学 | High-concentration waste water anaerobic fermentation device capable of realizing gas by-pass split-flow |
| CN103153882A (en) * | 2010-09-27 | 2013-06-12 | 株式会社爱博 | Apparatus for methane fermentation treatment |
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| US7374682B2 (en) | 2003-03-31 | 2008-05-20 | Ebara Corporation | Method and apparatus for the methane fermentation treatment of wastewater containing sulfur compound |
| JP4428188B2 (en) * | 2004-10-13 | 2010-03-10 | 荏原エンジニアリングサービス株式会社 | Organic wastewater treatment method and treatment apparatus |
| WO2006049322A1 (en) * | 2004-11-05 | 2006-05-11 | Ebara Corporation | Biological denitrification method and apparatus |
| JP2011206657A (en) * | 2010-03-29 | 2011-10-20 | Chugoku Electric Power Co Inc:The | Gas-liquid separator |
| CN102674543A (en) * | 2012-05-25 | 2012-09-19 | 桂林电子科技大学 | Magnetoelectric induction bioreactor for rejuvenating bacteria |
| JP6378957B2 (en) * | 2014-07-16 | 2018-08-22 | 水ｉｎｇ株式会社 | Defoamer charging device and defoamer charging method |
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| JPS61174995A (en) * | 1985-01-29 | 1986-08-06 | Nippon Beet Sugar Mfg Co Ltd | Anaerobic digestion vessel |
| JPH07204682A (en) * | 1994-01-18 | 1995-08-08 | Toshiba Corp | Anaerobic water treatment apparatus |
| JP4080046B2 (en) * | 1998-01-26 | 2008-04-23 | 株式会社荏原製作所 | Anaerobic treatment method and apparatus |
| JP4433550B2 (en) * | 2000-03-10 | 2010-03-17 | 栗田工業株式会社 | Anaerobic treatment of plant extract extraction wastewater |
| JP2002079290A (en) * | 2000-07-07 | 2002-03-19 | Sumitomo Heavy Ind Ltd | Underwater aeration device |
| JP3955431B2 (en) * | 2000-09-08 | 2007-08-08 | 株式会社荏原製作所 | Anaerobic treatment method and apparatus |
| JP4408328B2 (en) * | 2000-11-17 | 2010-02-03 | 住友重機械エンバイロメント株式会社 | Organic wastewater treatment method and apparatus |
-
2002
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103153882A (en) * | 2010-09-27 | 2013-06-12 | 株式会社爱博 | Apparatus for methane fermentation treatment |
| CN103153882B (en) * | 2010-09-27 | 2014-12-03 | 株式会社爱博 | Apparatus for methane fermentation treatment |
| CN102616929A (en) * | 2012-03-21 | 2012-08-01 | 天津科技大学 | High-concentration waste water anaerobic fermentation device capable of realizing gas by-pass split-flow |
| CN102616929B (en) * | 2012-03-21 | 2013-09-11 | 天津科技大学 | High-concentration waste water anaerobic fermentation device capable of realizing gas by-pass split-flow |
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| JP4162234B2 (en) | 2008-10-08 |
| JPWO2003042116A1 (en) | 2005-03-10 |
| WO2003042116A1 (en) | 2003-05-22 |
| CN100412006C (en) | 2008-08-20 |
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Effective date of registration: 20100701 Address after: Tokyo, Japan Patentee after: EBARA ENGINEERING SERVICE CO.,LTD. Address before: Tokyo, Japan Patentee before: Ebara Corp. |
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Granted publication date: 20080820 |