CN1769208A - Three-phase front end processor for internal recycle anaerobic reactor - Google Patents
Three-phase front end processor for internal recycle anaerobic reactor Download PDFInfo
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- CN1769208A CN1769208A CNA2005100295507A CN200510029550A CN1769208A CN 1769208 A CN1769208 A CN 1769208A CN A2005100295507 A CNA2005100295507 A CN A2005100295507A CN 200510029550 A CN200510029550 A CN 200510029550A CN 1769208 A CN1769208 A CN 1769208A
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Abstract
The invention discloses a three-phase front processor for inner-loop anaerobic reactor, which contains at least two layers of inversed V-type horizontal pneumatic troughs of cross distribution and a 'pi'-type horizontal collector trough connecting to a lift leg on the top, one end of the pneumatic trough connecting vertically to the side plate of the collector trough, and the lower end between adjacent horizontal pneumatic troughs having passages for liquid and particles. The device is characterized in that the passage opening connecting below middle of the pneumatic trough and the side-plate of collector trough is trapezoidal, the lower side of trapezoidal passage opening is higher than that of the pneumatic trough, the other side of the pneumatic trough is equipped with a triangular block which has constant section to the pneumatic trough, and a gas chamber is formed above the trapezoidal passage opening of the pneumatic trough. The merit of the invention is characterized in that it is beneficial for the growing of particle sludge, to decrease substantially the leak of minute particle sludge and improve the liquid stream in biochemical reaction field.
Description
Technical field
The present invention relates to internal recycle (IC) anaerobic treatment equipment, especially relate to a kind of three-phase front end processor efficiently that is used for eddy flow internal recycle (EIC) anaerobic reactor.
Background technology
The cost of the volume organic loading of raising anaerobic reactor and clearance, reduction reactor is scientific and technical personnel's a striving direction always.In s-generation representative processes---on the basis of upflow sludge blanket anaerobic reactor (UASB), emerge third generation anaerobic reactor.Their typical case's representative has sludge bulking bed bioreactor (EGSB), internal-circulation anaerobic reactor (IC), anaerobic baffled reactor (ABR).Though EGSB has the high advantage of volume organic loading, exist that operation control is strict, difficult design when reactor volume amplifies, lack precision processing and low, the shortcoming that has back-end processing and mud reflow treatment device of clearance usually.ABR does not have feedback function but connect between compartment because technique subsection can be pursued higher clearance, and size of compartments is restive, and the technology operational conditions differs greatly, and general volume organic loading is not as EGSB and IC.
Usually IC operation, first reaction chamber (promptly descending reaction chamber, main reaction region) working condition is similar to EGSB; Second reaction chamber (promptly going up reaction chamber, auxilliary reaction zone) is the precision processing district, and running condition is similar to UASB.Owing to adopted and effectively utilized gas to carry the internal circulation system of energy, realized becoming the agitation energy of turbulent energy into the systemic circulation main reaction region, need not outside energy realizes the mud backflow and further improves main reaction region mixing mass transfer characteristic, the feedback characteristics of internal recycle makes the robustness of operation strengthen again, and its comprehensive advantage is arranged.
We improve IC from following three aspects, form eddy flow internal-circulation anaerobic reactor (EIC) embryo.Example (overlaps 1000m more
3Above EIC) show: cyclone gas-liquid is separated in when avoiding the granule sludge surging force, has improved gas-liquid separation and cyclic utilization rate; Reflux and mix the eddy flow water distribution, can evenly improve mass transfer effect by water distribution; Many circulations, many eddy flows system, the amplification that has solved wide range physical dimension meets the needs of from the different angles of energy, space utilization, or outer energizing quantity minimizes, and equilibrium the mud load.And disclose corresponding patent (ZL03227936.1, CN1562495A, ZL200420023281.4).
The basis of high efficiency anaerobic reactor is the operation with the granule sludge form, and the state of sludge loss then is one of key of decision high efficiency anaerobic reactor clearance height.Known rational physical environment (comprising that structure is formed) and operational conditions are the prerequisites of granule sludge growth and existence.Appropriate UASB, ABR physical structure and startup and operation scheme can generate and move in the granule sludge mode.Internal-circulation anaerobic reactor, difficult because of the cultivation of granule sludge, all be to start usually with granule sludge.Even if steady running, recycle system stress field interior and that reaction zone is interior has very big difference, and the granule sludge in the reaction chamber enters the easier fragmentation of the recycle system, is the inevitable outcome of shearing force increase and the inside and outside stress field drastic change of particle.Though the precision processing district is arranged, the fine particle mud after the fragmentation still runs off easily.Therefore, the clearance of internal-circulation anaerobic reactor has only about 80% usually.
Existing triphase separator, all at UASB under granule sludge and floc sludge state, carry out three-phase and effectively separate and design.High effective three phase separator, general structure is complicated, and still in updating.Triphase separator patent CN1406879A, ZL200420026297.0 that example is announced in the recent period.For internal-circulation anaerobic reactor, existing gas-liquid separator in the internal circulation system, and front end physical channel (recycle system before the gas-liquid separator) need carry secretly or promote and impel energy to utilize maximized mixed solution in a large number.This anaerobic reactor generally also has two three-phase front end processors.The mixed solution that main reaction region and auxilliary reaction zone three-phase front end processor are handled, the situation difference of solid form, concentration and biochemical reaction, also variant with UASB.Three-phase front end processor, if only consider to collect fully gas and energy transformation function, adopt gas skirt simple in structure, be prone to then that granule sludge is difficult to cultivate, tiny mud is easy to generate and run off, cause the volume organic loading to be difficult to improve, problem that clearance is lower.Reasonably functional objective design, at handled state of matter, the correct analysis of material interphase interaction and force transmission, resolve the physical Design of three-phase front end processor, be the anaerobic reactor that is equipped with internal circulation system, improve one of key of volume organic loading and purification rate, simplified construction, reduction cost.
Summary of the invention
The objective of the invention is to internal circulation system, provide a kind of improving volume organic loading and purification rate three-phase front end processor more effective, simple in structure for internal-circulation anaerobic reactor.
The object of the present invention is achieved like this: three-phase front end processor of the present invention, comprise the two-layer at least inverted v-shaped level set air drain of intersection configuration and the horizontal collecting tray of " π " shape that the top is connected with riser tube of being, one end of pneumatic trough is vertically connected on the side plate of collecting tray, horizontal Neighbor Set air drain leaves fluid and particle path between the lower end, feature is: being shaped as of the porthole that the middle and lower part of pneumatic trough and collecting tray are connected on side plate is trapezoidal, is provided with and the prismatic trilateral sprue of pneumatic trough at the other end of pneumatic trough; Be in operation, above the trapezoidal channel mouth of pneumatic trough, form air chamber.
Inverted v-shaped pneumatic trough lower ending opening width L
1Greater than fluid and the particle path width L between the same layer pneumatic trough lower end
2, the best is (1/3) L
1≤ L
2≤ (2/3) L
1
The bottom of trapezoidal channel mouth is higher than inverted v-shaped pneumatic trough lower end line along the line, and is in service, easily forms the gas-liquid-solid three-phase interfacial layer; The summit along the line, top of the width l of the side plate of inverted v-shaped pneumatic trough, trapezoidal channel mouth is to the length l of triangular apex
1With the side of trapezoidal channel mouth length l along the line
2Between the pass be: 0.61≤l
1≤ 0.751,0.851≤l
1+ l
2≤ 0.91 (l＞0.6m).
The gas production rate V of the biochemical reaction zone of pneumatic trough length L, three-phase front end processor alignment processing, the cross-sectional area of biochemical reaction zone are S, pneumatic trough apex angle, then the gas flow of trapezoidal channel mouth is 21LVSin (α/2)/S, and the horizontal pressure gradient difference of trapezoidal channel saliva advection is proportional to maximum possible ultimate pressure ρ (l-l
1) Cos (α/2).
The orthogonal thereto in the horizontal direction configuration of the pneumatic trough of the pneumatic trough of main reaction region three-phase front end processor and auxilliary reaction zone three-phase front end processor.
The pneumatic trough apex angle of auxilliary reaction zone three-phase front end processor: 90 °≤α≤120 °, the pneumatic trough apex angle of main reaction region three-phase front end processor: 60 °≤α≤90 °.
Under the normal operating condition, the handled mixed solution of three-phase front end processor has following characteristics: main reaction region, granule sludge is to be in expanded state (solid accounts for the 70%-90% of solidliquid mixture volume) and intensive floating attitude (solid accounts for the 50%-70% of solidliquid mixture volume, equal diameter ball be in contact with one another minimum to arrange the volume that takes up space be 52%).Auxilliary reaction zone bottom granule sludge also is in the floating attitude of comparatively dense (dense phase of fluidization bottom).Because reactor is higher, the delamination of gravity makes the object that arrives auxilliary reaction zone three-phase front end processor, only may be the fine particle mud (in the general diameter 1mm) that springs up or fine mud with handle after the sparse mixed flow of waste water.Therefore, the liquid that three-phase front end processor is upper and lower, solid passage only need to consider the unobstructed of granule sludge fluctuation circulation and sparse mixed flow.Generally speaking, the gas that the main reaction region biochemical reaction is generated is about 4 times of the gas that produced of auxilliary reaction zone biochemical reaction, and this is the another difference that main and auxiliary three-phase front end processor faces.
According to three-phase front end processor of the present invention, the transversal section of the gas in the air chamber is basic identical, and pneumatic trough is to the continuous seizure effect of bubble, and generation is forced to horizontal direction and quickens flowing to the collecting tray porthole gradually.
Auxilliary reaction zone pneumatic trough, when starting operation under main reaction region pneumatic trough and the normal operating condition in the main reaction region pneumatic trough away from the collecting tray part because gas flow rate is lower, the liquid-gas interface horizontal direction is static relatively.The relative immobilized liquid-gas interface of level, the gas in discharging bubble, the tail of rising bubble inhale and the microvovtex that forms to the relatively poor mud of settleability and the subparticle mud of rising bubble interfacial adsorption, tangible absorption seizure effect is also arranged, form the gas-liquid-solid three-phase interfacial layer.This interfacial layer has more than the more violent gas-liquid turbulent flow in inside to distribute except that itself having shortened distance between granule sludge, having strengthened the intergranular interaction, and the latter is stronger to the interaction between granule sludge.Two kinds of effects are all grown, are strengthened and the obvious facilitation of having dried the collision of granule sludge.And the three-phase front end processor of auxilliary reaction zone is to molecule sludge absorption seizure effect, also obviously reduced mud loss, improved clearance.
As everyone knows, the three phase flow of horizontal direction is because the influence of gravity makes three-phase separate the mobile tendency.From distance collecting tray distal-most end, the gas flow horizontal direction is slowly quickened from zero in the pneumatic trough.Because viscous force and inertia is different, when gas flow rate reached some amount, liquid is horizontal flow thereupon; When liquid arrived certain flow rate, drag force could drive granule sludge and move horizontally.Generally, place, porthole heterogenetic flow pattern is stratified flow and wavy layering flow pattern.At this moment, the gas, liquid, solid interfacial layer by liquid-gas interface forms settleability relatively poor particle absorption seizure bifurcated also can occur at place, nearly porthole and disappear.This has just greatly changed the three-phase ratio that enters collecting tray.Because the collection fully of gas, the air content in the collecting tray, enter liquid in the collecting tray, the ratio between solid by the biochemical gas production rate decision of reaction zone, then depend on the horizontal flow state of porthole.The biochemical reaction zone gas production rate of three-phase front end processor correspondence is that the cross-sectional area of V, biochemical reaction zone is that the floorage of S, single pneumatic trough is S
1, the pneumatic trough drift angle is that α, pneumatic trough length are that the mixed solution density of L, three-phase front end processor correspondence is ρ, because S
1=21LSin (α/2), then the gas flow of porthole is necessary for S
1V/S, the flow velocity of gas depend on porthole area and horizontal gradient pressure reduction.The horizontal pressure gradient difference of horizontal flow is proportional to maximum possible ultimate pressure ρ (l-l
1) Cos (α/2).Because of than, the pneumatic trough apex angle is being adjusted the seizure bubbles volume of pressure reduction and pneumatic trough, α is also just controlling the horizontal flow pattern of polyphasic flow in the pneumatic trough and the heterogeneous inflow state of porthole to a great extent.
Collecting tray has and the similar horizontal flow characteristic of pneumatic trough, polyphasic flow in the collecting tray is because the influence of gravity, further reduce the mud ratio that enters mixed solution in the recycle system by riser tube, improved granule sludge existence and the more consistent characteristic of particle diameter, also improved the clearance of reactor.
According to three-phase front end processor of the present invention, the pneumatic trough horizontal direction orthogonal collocation of main and auxiliary reaction zone.In the auxilliary reaction zone, the vertical liquid flowing water in bottom square arrives the top to waviness difference and quadrature can occur and reverse, and produces orderly little vortex distribution.This liquid stream has been strengthened the sinking of mass transfer process and molecule mud, further improves the degree of the auxilliary meticulous biochemical reaction of reaction zone.
Therefore the present invention have help the granule sludge growth and with this form operation, the liquid stream that helps reducing the molecule sludge loss significantly and improve biochemical reaction zone, simple in structure, advantage that laid down cost is low.It only is position and the shape that simple gas skirt changes access opening, forms the horizontal polyphasic flow of pressure air chamber and cumulative speed, realizes the required objective function of anaerobic reactor.The present invention is in a kind of internal circulation system of anaerobism sewage treatment equipment, realizes the three-phase front end processor of high organic loading and clearance for wastewater treatment.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2 looks diagrammatic cross-section for the right side of Fig. 1;
Fig. 3 is horizontal liquid stream and a liquid-gas interface feature synoptic diagram in the pneumatic trough;
Fig. 4 is the structural representation of eddy flow internal-circulation anaerobic reactor.
Embodiment
Below in conjunction with embodiment and contrast accompanying drawing the present invention is described in further detail.
Three-phase front end processor of the present invention, comprise the two-layer at least inverted v-shaped level set air drain 1 of intersection configuration and the horizontal collecting tray 2 of " π " shape that the top is connected with riser tube 5 of being, one end of pneumatic trough 1 is vertically connected on the side plate 12 of collecting tray 2, horizontal Neighbor Set air drain leaves fluid and particle path 10 between 1 lower end, being shaped as of the porthole 4 that the middle and lower part of pneumatic trough 1 and collecting tray 2 are connected on side plate 12 is trapezoidal, is provided with and pneumatic trough 1 prismatic trilateral sprue 11 at the other end of pneumatic trough 1; Be in operation, above the trapezoidal channel mouth 4 of pneumatic trough 1, form air chamber 3.
Inverted v-shaped pneumatic trough 1 lower ending opening width L
1Greater than the fluid between same layer pneumatic trough 1 lower end and the width L of particle path 10
2, the best is (1/3) L
1≤ L
2≤ (2/3) L
1
Following along the line 8 of trapezoidal channel mouth 4 is higher than inverted v-shaped pneumatic trough 1 lower end line, and the length l of triangular apex is arrived on the width l of the side plate 6 of inverted v-shaped pneumatic trough 1,7 summits along the line, the top of trapezoidal channel mouth 4
1Length l with the side of trapezoidal channel mouth 4 along the line 9
2Between the pass be: 0.61≤l
1≤ 0.751,0.851≤l
1+ l
2≤ 0.91 (l＞0.6m).
The gas production rate V of the biochemical reaction zone of pneumatic trough 1 length L, three-phase front end processor alignment processing, the cross-sectional area of biochemical reaction zone are S, pneumatic trough 1 apex angle, then the gas flow of trapezoidal channel mouth 4 is 21LV Sin (α/2)/S, and the horizontal pressure gradient difference of trapezoidal channel mouth 4 horizontal flows is proportional to maximum possible ultimate pressure ρ (l-l
1) Cos (α/2).
The orthogonal thereto in the horizontal direction configuration of the pneumatic trough of the pneumatic trough of main reaction region 13 three-phase front end processors and auxilliary reaction zone 14 three-phase front end processors.
The pneumatic trough apex angle of auxilliary reaction zone three-phase front end processor: 90 °≤α≤120 °, the pneumatic trough apex angle of main reaction region three-phase front end processor: 60 °≤α≤90 °.
The pending waste water that enters anaerobic reactor is with after pump around circuit waste water mixes, the main reaction region that enters expanded state or incipient fluidization mud, and with anaerobic sludge generation biochemical reaction.The bubble that biochemical reaction produces, the three-phase mixed solution of the mud composition that waste liquid that main reaction region was handled and settleability are relatively poor travels up to the three-phase front end processor of main reaction region.
Upwards mobile three-phase mixed solution will be divided into two partly.Some does not contain bubble, and the two-phase mixed solution that the relatively poor mud of waste liquid that main reaction region was handled and settleability is formed will upwards flow by the gap of pneumatic trough, pass the main reaction region three-phase front end processor.Another part, as shown in Figure 3, in pneumatic trough, because the merging of bubble and the constantly effect of release at the interface, being forced to produce trilateral sprue place is horizontal gas stream zero, trapezoidal channel mouth Peak Flow Rate.And relative in the horizontal direction immobilized liquid-gas interface adsorbs the seizure effect owing to what rising bubble produced to the relatively poor granule sludge of settleability, has formed the gas-liquid-solid three-phase interfacial layer.Mud density in the gas-liquid-solid three-phase interfacial layer can be higher than buoyant mud density below it, has increased intergranular effect probability.Rising bubble in the merging of three phase boundary layer, discharge form more than reaction zone inside more violent many turbulent flows.Intensive gas, liquid micro cyclone have two effects: shear-stress strengthens, the particle spin that vortex causes, force the spin granule sludge vortex and close or the extinction process in obtain energy, collision polymeric reactive force greatly strengthens, for the reinforcement of granule sludge, dry and increase and created favourable condition, the granule sludge that settleability is obviously improved will sink.Meanwhile, in the horizontal direction, because the existence of viscous force is with different, interfacial layer and be close to three-phase mixed solution in the zone and have and be lower than gas stream and the huge three-phase horizontal flow of speed difference that drags of diffusion progressively.Because gravity is to vertical dual function than Maelstrom of the influence and the formation of trapezoidal channel mouth place of horizontal three-phase stream, at place, nearly porthole, the gas-liquid-solid three-phase interfacial layer will disappear, and forms layering liquid and flows and wavy stratified flow.Greatly this a part of three-phase mixed solution of change takes place in ratio, will enter collecting tray by the trapezoidal channel mouth.The three-phase mixed solution that mud further reduces in the collecting tray is because density difference enters the recycle system by riser tube.
Because entering internal circulation system by riser tube significantly shunts, the flow that enters auxilliary reaction zone by the main reaction region three-phase front end processor descends significantly.Aforementioned two-phase liquid stream climbing speed declining to a great extent and rising bubble to the removal of mud lifting effect, make under action of gravity, can form the dense phase of fluidization bottom by the granule sludge that arrives auxilliary reaction zone at auxilliary reaction zone bottom.Residue soluble organic in the rising waste liquid has further been removed the soluble organic in the liquid at auxilliary reaction zone and granule sludge generation biochemical reaction.The bubble that auxilliary reaction zone biochemical reaction is produced, the small mud granule that the waste water after meticulous biochemical reaction is handled, rising bubble and liquid stream thereof are carried secretly travels up to auxilliary reaction zone three-phase front end processor.
Similar substantially with situation in the aforementioned main reaction region three-phase front end processor, different is the bubble much less that auxilliary reaction zone is produced, and the gas speedup declines to a great extent, and causes horizontal flow velocity less, and liquid-gas interface forms three phase boundary layer absorption capture surface and increases significantly.And this moment, molecule mud distributes in rising liquid and is inhomogeneous, and is mainly entrained with the small vortex of nearly bubble by the wake flow of bubble.Because the pneumatic trough of auxilliary reaction zone three-phase front end processor and the pneumatic trough orthogonal collocation of main reaction region three-phase front end processor, will form the rising micro cyclone of distribution, bubble and the molecule mud that carries thereof are easy to enter in these micro cyclones that rise that distribute, and take place and close.A part of is that the solution of main phase will enter the recycle system by auxilliary reaction zone three-phase front end processor, riser tube with gas-liquid.Do not contain bubble, the waste water that contains after the precision processing of molecule sludge concentration very little (concentration of floating contained molecule mud in the auxilliary reaction zone liquid) will be by assisting the reaction zone three-phase front end processor.
In like manner, the rising flow velocity will further descend, and it has further precipitating action to the above mud of the μ m order of magnitude.Waste water solution after the generally only remaining precision processing of arrival water outlet.And the three-phase mixed solution that enters the recycle system passes through gas-liquid separator separates, and the backflow waste liquid enters main reaction region to be mixed with pending waste water.
Claims (6)
1, a kind of three-phase front end processor that is used for internal-circulation anaerobic reactor, comprise the two-layer at least inverted v-shaped level set air drain (1) of intersection configuration and the horizontal collecting tray of " π " shape (2) that the top is connected with riser tube (5) of being, one end of pneumatic trough (1) is vertically connected on the side plate (12) of collecting tray (2), leave fluid and particle path (10) between horizontal Neighbor Set air drain (1) lower end, it is characterized in that: being shaped as of the porthole (4) that the middle and lower part of pneumatic trough (1) and collecting tray (2) are connected on side plate (12) is trapezoidal, is provided with and the prismatic trilateral sprue of pneumatic trough (1) (11) at the other end of pneumatic trough (1); Be in operation, form air chamber (3) in the top of the trapezoidal channel mouth (4) of pneumatic trough (1).
2, three-phase front end processor as claimed in claim 1 is characterized in that: inverted v-shaped pneumatic trough (1) lower ending opening width L
1Greater than the fluid between same layer pneumatic trough (1) lower end and the width L of particle path (10)
2, the best is (1/3) L
1≤ L
2≤ (2/3) L
1
3, three-phase front end processor as claimed in claim 1, it is characterized in that: following (8) along the line of trapezoidal channel mouth (4) are higher than inverted v-shaped pneumatic trough (1) lower end line, and the length l of triangular apex is arrived on the width l of the side plate (6) of inverted v-shaped pneumatic trough (1), (7) summit along the line, the top of trapezoidal channel mouth (4)
1Length l with the side of trapezoidal channel mouth (4) (9) along the line
2Between the pass be: 0.61≤l
1≤ 0.751,0.851≤l
1+ l
2≤ 0.91 (l＞0.6m).
4, three-phase front end processor as claimed in claim 1, it is characterized in that: the gas production rate V of the biochemical reaction zone of pneumatic trough (1) length L, three-phase front end processor alignment processing, the cross-sectional area of biochemical reaction zone are S, pneumatic trough (1) apex angle, then the gas flow of trapezoidal channel mouth (4) is 21LV Sin (α/2)/S, and the horizontal pressure gradient difference of trapezoidal channel mouth (4) horizontal flow is proportional to maximum possible ultimate pressure ρ (l-l
1) Cos (α/2).
5, three-phase front end processor as claimed in claim 1 is characterized in that: the orthogonal thereto in the horizontal direction configuration of pneumatic trough of the pneumatic trough of main reaction region (13) three-phase front end processor and auxilliary reaction zone (14) three-phase front end processor.
6, three-phase front end processor as claimed in claim 5, it is characterized in that: the pneumatic trough apex angle of auxilliary reaction zone (14) three-phase front end processor: 90 °≤α≤120 °, the pneumatic trough apex angle of main reaction region (13) three-phase front end processor: 60 °≤α≤90 °.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100295507A CN100368317C (en) | 2005-09-06 | 2005-09-06 | Three-phase front end processor for internal recycle anaerobic reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100295507A CN100368317C (en) | 2005-09-06 | 2005-09-06 | Three-phase front end processor for internal recycle anaerobic reactor |
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| Publication Number | Publication Date |
|---|---|
| CN1769208A true CN1769208A (en) | 2006-05-10 |
| CN100368317C CN100368317C (en) | 2008-02-13 |
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ID=36750804
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|---|---|---|---|
| CNB2005100295507A Expired - Fee Related CN100368317C (en) | 2005-09-06 | 2005-09-06 | Three-phase front end processor for internal recycle anaerobic reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663684A (en) * | 2012-09-18 | 2014-03-26 | 中国石油化工股份有限公司 | Three-phase separator of cylindrical internal-recycling anaerobic reactor |
| CN104862207A (en) * | 2014-02-25 | 2015-08-26 | 中国科学院青岛生物能源与过程研究所 | Hanging-bag microalgae photoreactor and hanging-bag microalgae culture system |
| CN104955592A (en) * | 2013-02-25 | 2015-09-30 | 里弗雷克特里知识产权两合公司 | Refractory impact pad |
| CN107162181A (en) * | 2017-05-03 | 2017-09-15 | 北京金泽环境能源技术研究股份有限公司 | A kind of three phase separator for internal-circulation anaerobic reactor |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2774924B1 (en) * | 1998-02-16 | 2000-05-05 | Procedes Et Services Proser | SEPARATOR FOR THREE-PHASE MIXTURE TO BE USED UNDER SEA LEVEL |
| CN2360139Y (en) * | 1999-02-03 | 2000-01-26 | 河南省科学院河南省计划委员会地理研究所 | Combined gas, liquid, and solid three-phase separater |
| NL1018909C2 (en) * | 2001-09-07 | 2003-03-17 | Paques Water Systems B V | Three-phase separator and biological waste water treatment plant. |
| CN2581437Y (en) * | 2002-10-25 | 2003-10-22 | 清华大学 | Internal circulation anaerobic reactor |
| CN2690388Y (en) * | 2004-04-12 | 2005-04-06 | 马三剑 | Wave plate three phase separator |
| CN2700319Y (en) * | 2004-05-28 | 2005-05-18 | 陈协 | Multi rotational flow adaptive multicycle anaerobic reactor |
-
2005
- 2005-09-06 CN CNB2005100295507A patent/CN100368317C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663684A (en) * | 2012-09-18 | 2014-03-26 | 中国石油化工股份有限公司 | Three-phase separator of cylindrical internal-recycling anaerobic reactor |
| CN103663684B (en) * | 2012-09-18 | 2015-05-13 | 中国石油化工股份有限公司 | Three-phase separator of cylindrical internal-recycling anaerobic reactor |
| CN104955592A (en) * | 2013-02-25 | 2015-09-30 | 里弗雷克特里知识产权两合公司 | Refractory impact pad |
| CN104862207A (en) * | 2014-02-25 | 2015-08-26 | 中国科学院青岛生物能源与过程研究所 | Hanging-bag microalgae photoreactor and hanging-bag microalgae culture system |
| CN107162181A (en) * | 2017-05-03 | 2017-09-15 | 北京金泽环境能源技术研究股份有限公司 | A kind of three phase separator for internal-circulation anaerobic reactor |
| CN107162181B (en) * | 2017-05-03 | 2018-05-11 | 北京金泽环境能源技术研究股份有限公司 | A kind of three phase separator for internal-circulation anaerobic reactor |
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| Publication number | Publication date |
|---|---|
| CN100368317C (en) | 2008-02-13 |
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