CN2229450Y - Internal circulation three phase biological fluidized bed - Google Patents
Internal circulation three phase biological fluidized bed Download PDFInfo
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- CN2229450Y CN2229450Y CN95213562U CN95213562U CN2229450Y CN 2229450 Y CN2229450 Y CN 2229450Y CN 95213562 U CN95213562 U CN 95213562U CN 95213562 U CN95213562 U CN 95213562U CN 2229450 Y CN2229450 Y CN 2229450Y
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- 238000005273 aeration Methods 0.000 claims abstract description 16
- 230000007704 transition Effects 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 7
- 239000001301 oxygen Substances 0.000 abstract description 7
- 229910052760 oxygen Inorganic materials 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 4
- 239000010865 sewage Substances 0.000 abstract description 4
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 25
- 238000005243 fluidization Methods 0.000 description 18
- 239000007788 liquid Substances 0.000 description 14
- 239000007789 gas Substances 0.000 description 13
- 239000002351 wastewater Substances 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 7
- 239000007787 solid Substances 0.000 description 7
- 239000012530 fluid Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 230000003321 amplification Effects 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000003199 nucleic acid amplification method Methods 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 3
- 230000003134 recirculating effect Effects 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000269799 Perca fluviatilis Species 0.000 description 1
- 230000000703 anti-shock Effects 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000013604 expression vector Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000003475 lamination Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000000247 postprecipitation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000013598 vector Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Biological Treatment Of Waste Water (AREA)
Abstract
The utility model relates to an internal circulation three phase biological fluidized bed, which belongs to the field of the sewage treatment. The internal circulation three phase biological fluidized bed is composed of a bed body, a lifting pipe, a diversion pipe, a separation pipe, and an aeration head. The bed body is a straight cylinder with a closed lower end; the diameter of the upper end of the bed body is larger than the diameter of the lower end; the bed body is in funnel-shaped; the lifting pipe is a straight cylinder with two open ends; the diameter of the lifting pipe is smaller than the diameter of the lower end of the bed body; one end of the diversion pipe is an open straight cylinder, the diameter of which is larger than the opening of the lifting pipe; the other end of the diversion pipe is an open straight cylinder with a smaller diameter; one end of the separation pipe is an open straight cylinder, the diameter of which is larger than the diversion pipe; the other end of the separation pipe is connected by two horn cylinders; the aeration head is arranged on the bed body, and the lower part of the bed body is provided with a water inlet. The internal circulation three phase biological fluidized bed has the advantages of favorable performance, high transfer efficiency of the oxygen, less carrier loss, easier amplifying design, and convenient operating management.
Description
The utility model relates to waste water, and sewage disposal belongs to waste water, sewage treatment area.
The notion of fluidized-bed is introduced from chemical reactor, in the chemical industry notion, contact with solid particulate matter when fluid is bottom-up, make particle in fluid, be suspended state and do random motion, just claim that this state is a fluidized state, corresponding reactor just is called fluidized-bed (FLUIDIZED BED).Its biggest advantage is that mass transfer condition is good.And in the waste water aerobic biological treatment process, the quality of the mass transfer condition between microorganism, waste water and the oxygen three is the key that influences reaction unit usefulness.Therefore, early seventies both at home and abroad some scholars is the mass transfer condition that improves reactor, improves biomass in the reactor and the notion of fluidized-bed is introduced field of waste water treatment.
Aerobic biological fluid-bed is to utilize tiny inert particle to make carrier, at its a large amount of microorganism growth in surface, perch, forms microbial film, under the dynamic action of G﹠W, make the carrier fluidisation, gas, solid, liquid three-phase well contact, and have reached the purpose that improves biological treatment efficient.
Compare aerobic biological fluid-bed having the following advantages with the traditional biological facture:
(1) hydraulic detention time is short, the biomass height, and the organic loading height, so equipment volume can reduce greatly, makes capital cost, the corresponding minimizing of floor space;
(2) do not need the mud return-flow system, treatment scheme is simplified;
(3) there is not in the activated sludge process bed latch up phenomenon that exists in normal sludge bulking problem that takes place or the Biological fitler method, moves more stable;
(4) has the ability of higher anti-shock loading.According to the number of phases of medium in the fluidized-bed, biological fluidized bed can be divided into two-phase fluidized-bed and three-phase fluidized bed two big classes.
The two-phase bed mainly comprises the aerobic two-phase bed of anaerobic fluidized bed and external oxygenation, is characterized in only existing in the fluidized-bed contact between the solid-liquid two-phase, and the fluidisation of carrier only depends on the into castering action of water.
The three-phase bed mainly comprises no circulation three-phase bed and extracorporeal circulation three-phase bed, is characterized in existing in the fluidized-bed the alternate mass transfer of solid, liquid, gas three, and the fluidisation of carrier depends on the common castering action of G﹠W.
But also there is following shortcoming in existing fluidized-bed:
Because the two-phase bed is effect between the solid-liquid two-phase in the bed body, the place one's entire reliance upon castering action of ascending current of the fluidisation of carrier, for reaching fluidization preferably, must be by means of bigger quantity of circulating water, corresponding energy consumption must increase a lot.In addition, make the carrier fluidisation evenly just require the bottom water distribution very even, the corresponding design difficulty that increased has brought many difficulties also for simultaneously the amplification of fluidized-bed.
For the aerobic two-phase bed of external oxygenation, its external oxygen replenishing equipment is quite complicated,, corresponding equipment input and the operation easier of having increased.Existing simultaneously two-phase bed generally all need be provided with external demoulding device, and this makes system flow more complicated.
For no circulation three-phase bed, for making in the body carrier fluidisation fully, evenly, very strict to bottom water distribution, gas distribution equipment requirements, this has just increased the design of fluidized-bed and has amplified difficulty.In addition, head gas, liquid, solid separating effect is not good, and external solid, liquid tripping device and carrier refluxing unit need be set.
For extracorporeal circulation three-phase bed, remove outside the problem of above-mentioned existence, owing to increased extracorporeal circulation system system energy consumption is improved greatly.
To sum up 2 described, traditional biological fluidized-bed subject matter is bottom water distribution, gas distribution equipment complexity, making design and amplifying difficulty increases; The part of general water outlet need circulate and enter reactor and increased system energy consumption; Need establish special demoulding equipment and carrier refluxing unit, make system's input increase, operation move more complicated.
Energy consumption was little when the purpose of this utility model provided a kind of operation, and gas, liquid, solid separate good fluidized-bed.
The utility model inner loop three phase fluidized bed reactor is by the bed body, and riser tube, thrust-augmenting nozzle, isolated tube, aeration head are formed.The bed body is the straight tube of a lower end closed, and the diameter of its upper end is big than the lower end, becomes a funnel-form.Riser tube is the grade tube straight of a both ends open, and its diameter diameter of bed body lower end cylindrical shell is little.Thrust-augmenting nozzle one end is the uncovered straight tube of a diameter greater than riser tube, and the other end is the less uncovered straight tube of a diameter, has transition section to connect therebetween.Isolated tube one end is a diameter uncovered straight tube big than thrust-augmenting nozzle, and the other end is linked by two speaking trumpets and forms.Riser tube is placed in the intravital bottom of bed, forms a up-flow district in riser tube, forms one between riser tube and the lower bed body and falls the stream district, and it is outside that the major diameter of thrust-augmenting nozzle partly is inserted in the riser tube upper end, forms the disengaging zone in the thrust-augmenting nozzle.The speaking trumpet of isolated tube partly is enclosed within outside the thrust-augmenting nozzle, forms a recirculating zone between isolated tube and thrust-augmenting nozzle.Between isolated tube outer wall and top bed body inwall, form a settling region and a backflow seam.Aeration head is placed in a body lower end.Water-in is arranged at bed body bottom.
The operational process of the utility model fluidized-bed is as follows:
In fluidized-bed, have tiny carrier abrim (as sandstone, haydite etc.) pending waste water, pressurized air carries out aeration aerating by the aeration head of bed body bottom, because the density in up-flow district is less than falling the stream district, so in the up-flow district, gas, waste water, carrier upwards flows simultaneously, when moving to the riser tube top, part waste water, carrier and minority small bubbles flow downward falling stream district along the thrust-augmenting nozzle lower end, other has part waste water, carrier and a large amount of bubble pass through the disengaging zone, realize gas at the thrust-augmenting nozzle top, Gu, the separation of liquid, make gas evolution, waste water and carrier return to by the recirculating zone and fall the stream district, that part of liquid that is equivalent to flooding velocity is simultaneously sewed on liter by backflow and is entered the settling region outside the post precipitation supernatant liquor is discharged fluidized-bed.
Illustrate that accompanying drawing is as follows:
Fig. 1 is the utility model inner loop three phase fluidized bed reactor structural representation.
Accompanying drawings embodiment is as follows:
The utility model inner loop three phase fluidized bed reactor is made up of bed body (1), riser tube (2), thrust-augmenting nozzle (3), isolated tube (4), aeration head (5).Riser tube (2) is placed in the bottom in the body (1), is up-flow district (6) in riser tube (2), distinguishes (7) for falling stream between riser tube (2) and the bed body (1); Thrust-augmenting nozzle (3) is inserted in the outside, upper end of riser tube (2), is disengaging zone (8) in the inside of thrust-augmenting nozzle (3); Isolated tube (4) is enclosed within the outside of thrust-augmenting nozzle (3), forms a recirculating zone (9) between isolated tube (4) and thrust-augmenting nozzle (3), forms the settling region (10) and the seam (11) that refluxes between the inwall of isolated tube (4) outer wall and bed body (1); Aeration head (5) is placed in the bottom of a body (1); Water-in (12) is arranged at the bottom of bed body (1).
It is good that inner loop three phase fluidized bed reactor (ITFB) not only has a general aerobic fluidized bed mass-transfer performance, and the sludge concentration advantages of higher also has the incomparable advantage of traditional fluid bed:
1, fluidizing performance is good
In ITFB as long as in up-flow district (5) (inner tube) by enough air and guarantee inner tube (2) caliber is reasonable, just can realize good carrier fluidisation. The fluidisation of ITFB carrier and traditional fluid bed Different. ITFB carrier in inner tube is subjected to the promotion of rising bubble and circulating water flow simultaneously, no The disconnected expansion risen, and when the carrier expansion height surpassed the inner tube upper end, carrier will flow to recirculated water Enter to fall in the stream district (6), do descending motion. Therefore, guarantee enough tolerance and suitable diameter of inner pipe , just can realize the carrier fluidisation. Another characteristics of ITFB carrier fluidisation are that most of carrier all participates in following Circulation is moving, does not therefore have carrier lamination in the bed, and each carrier granular is suffered in bed Friction, shear basic identically, the required kinetic energy of carrier fluidisation only is the energy that air feed consumes basically Amount reduces greatly than traditional fluid bed energy consumption; Simultaneously, for satisfying evenly required gas distribution of fluidisation Equipment is also simply many than traditional fluid bed.
2, the transfer efficiency height of oxygen
When supplying with same tolerance, because ITFB is at interior pipe aeration, at the long-pending aeration of whole bed body section, so aeration intensity is bigger among the ITFB, two-phase bed and three-phase bed that the contact gear ratio between liquid phase and gas phase is traditional are violent less than traditional fluidized-bed for its aeration sectional area.Simultaneously, can carry some tiny bubbles secretly during a large amount of liquid circulation, solution-air be prolonged duration of contact, thereby improved the transfer efficiency of oxygen.During the experiment table, air utilization ratio can reach 10-30% among the ITFB, and dynamic efficiency can reach 2-5kgO
2/ kwh.
3, the carrier current vector is few and do not need special demoulding and carrier refluxing unit.
In ITFB, because most of participation of carrier circulates.Therefore the shearing that carrier is subjected in the whole reactor and the uniformity basically that rubs can not go out expression vector demixing phenomenon (this is the fundamemtal phenomena of traditional fluidized-bed).Simultaneously, owing to a hydraulic friction in the bed, shear more violently,, be present in the fluidized-bed the basic uniformity of density of bio-carrier in the assurance fluidized-bed with the form of suspended sludge so blocked up microbial film can peel off voluntarily.Mud under coming off can separate with carrier in the solid, liquid disengaging zone preferably through behind the degas zone, enters in the settling tank with water outlet.So in ITFB, need not increase demoulding machinery and just can guarantee in the fluidized-bed that the film on the bio-carrier can excessive increase, carrier can not run off again simultaneously, so just simplified traditional fluidized-bed required utility appliance in the system of disposing of sewage greatly.
4, amplification design is easier to
Why traditional fluidized-bed amplifies difficulty, and reason mainly contains 2 points: whole fluidised form complexity is difficult to accurate description in (1) fluidized-bed, can't instruct amplification design; (2) fluidizing device (water distribution system, gas distribution system) is for making evenly its complex structure of carrier fluidisation, and is difficult to realize when being amplified to the large section.
And ITFB is improved at above two.At first, set up interior pipe, the motion standard of carrier in the fluidized-bed and liquid has been become to rise to flow and descend flow, after change like this, just can clearly depict the characteristics of motion of carrier and liquid in the fluidized-bed on the whole.Wait the control that realizes the fluidized-bed behavior through several Control parameter such as liquid circulation velocity.When amplification design, just can expect to obtain similar fluidized-bed behavior as long as these key parameters of assurance are similar.Secondly, because the fluidisation of carrier is decided by the gas lift that aeration head discharges in the pipe among the ITFB, and interior tube section is long-pending less relatively, and the position of aeration head and form are easy to arrange when amplifying like this, can not influence the even fluidisation of carrier.
5, operational management is convenient
Because ITFB than the traditional biological fluidized-bed, has saved external oxygen replenishing equipment, demoulding and carrier refluxing unit, part effluent recycling system, and ITFB system integration degree is improved greatly, operational management is more convenient.
6, system energy consumption reduces greatly
Because ITFB system carrier fluidisation only relies on a certain amount of air of supply and can finish, need not a large amount of circulating backwaters of two-phase bed to guarantee the abundant fluidisation of carrier; Simultaneously, the transfer efficiency of oxygen improves greatly than traditional fluidized-bed.Therefore the ITFB system energy consumption is lower naturally.
Claims (1)
1, a kind of inner loop three phase fluidized bed reactor is characterized in that by the bed body, riser tube, and thrust-augmenting nozzle, isolated tube, aeration head is formed, and the bed body is the straight tube of a lower end closed, and the diameter of its upper end is big than the lower end, becomes one to leak head; Riser tube is the grade tube straight of a both ends open, and its diameter diameter of bed body lower end cylindrical shell is little; Thrust-augmenting nozzle one end is the uncovered straight tube of a diameter greater than riser tube, and the other end is the less uncovered straight tube of a diameter, has transition section to connect therebetween, and isolated tube one end is a diameter uncovered straight tube big than thrust-augmenting nozzle, and the other end is linked by two speaking trumpets and forms; Riser tube is placed in the intravital bottom of bed, and it is outside that the major diameter of thrust-augmenting nozzle partly is inserted in the riser tube upper end, and the isolated tube speaking trumpet partly is enclosed within outside the thrust-augmenting nozzle; Aeration head is placed in a body lower end, and water-in is arranged at bed body bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95213562U CN2229450Y (en) | 1995-06-23 | 1995-06-23 | Internal circulation three phase biological fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95213562U CN2229450Y (en) | 1995-06-23 | 1995-06-23 | Internal circulation three phase biological fluidized bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2229450Y true CN2229450Y (en) | 1996-06-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95213562U Expired - Lifetime CN2229450Y (en) | 1995-06-23 | 1995-06-23 | Internal circulation three phase biological fluidized bed |
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| CN (1) | CN2229450Y (en) |
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100349806C (en) * | 2005-06-27 | 2007-11-21 | 北京市环境保护科学研究院 | Filtering type highly effective separation and inside circulation triphase fluidized bed reactor |
| CN100412008C (en) * | 2006-09-01 | 2008-08-20 | 清华大学 | Composite anaerobic reactor with inner circulation |
| CN100427197C (en) * | 2003-07-01 | 2008-10-22 | 王强 | Complex type internal circulation bioreactor |
| CN101781016A (en) * | 2010-03-04 | 2010-07-21 | 陕西科技大学 | Three-phase biological fluidized bed |
| CN101973665A (en) * | 2010-09-28 | 2011-02-16 | 天津市天水环保设计工程有限公司 | A/O reactor with functions of air lift, backflow as well as rotation and mixing of reflux |
| CN102079613A (en) * | 2010-12-22 | 2011-06-01 | 上海广联建设发展有限公司 | Ozone catalytic oxidation biological fluidized bed sewage treatment plant and treatment method using same |
| CN102134149A (en) * | 2011-05-10 | 2011-07-27 | 山东建筑大学 | Composite moving bed bio-film reactor |
| CN101076498B (en) * | 2004-11-22 | 2012-06-06 | 努比亚水系统有限公司 | Aeration type biofiltering system and waste water treatment method |
| CN103755017A (en) * | 2014-01-22 | 2014-04-30 | 东南大学 | Aerobic biological fluidized bed device combining enriched oxygen aeration and oxygen filling method thereof |
| WO2014101764A1 (en) * | 2012-12-25 | 2014-07-03 | Zhu Yongqiang | Biological membrane fluidized bed wastewater treatment method |
| CN104609565A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Synchronous nitrification and denitrification treatment method of ammonia-containing wastewater |
| CN105110452A (en) * | 2015-08-12 | 2015-12-02 | 深圳市清研环境科技有限公司 | Sewage treatment apparatus and sewage treatment method therefor |
| CN105439279A (en) * | 2014-09-25 | 2016-03-30 | 扬州天朗水务设备有限公司 | Biological fluidized bed |
| CN107226523A (en) * | 2016-03-23 | 2017-10-03 | 国环清源控股有限公司 | A kind of continous way three phase fluidized bed |
| WO2018040753A1 (en) * | 2016-08-29 | 2018-03-08 | 武汉东川自来水科技开发有限公司 | Double-biomembrane sewage treatment system and method |
| CN108069505A (en) * | 2016-11-11 | 2018-05-25 | 南京理工大学 | A kind of inner loop three phase fluidized bed reactor |
| WO2020140841A1 (en) * | 2018-12-31 | 2020-07-09 | 中国石油化工股份有限公司 | Solid precipitation device and solid precipitation method |
| CN113016577A (en) * | 2021-03-24 | 2021-06-25 | 湖北卓耳节水灌溉有限公司 | Water-saving irrigation system and irrigation method |
| RU2805727C2 (en) * | 2018-12-31 | 2023-10-23 | Чайна Петролиум & Кемикал Корпорейшн | Device and method of sedimentation of solid sediments |
-
1995
- 1995-06-23 CN CN95213562U patent/CN2229450Y/en not_active Expired - Lifetime
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100427197C (en) * | 2003-07-01 | 2008-10-22 | 王强 | Complex type internal circulation bioreactor |
| CN101076498B (en) * | 2004-11-22 | 2012-06-06 | 努比亚水系统有限公司 | Aeration type biofiltering system and waste water treatment method |
| CN100349806C (en) * | 2005-06-27 | 2007-11-21 | 北京市环境保护科学研究院 | Filtering type highly effective separation and inside circulation triphase fluidized bed reactor |
| CN100412008C (en) * | 2006-09-01 | 2008-08-20 | 清华大学 | Composite anaerobic reactor with inner circulation |
| CN101781016A (en) * | 2010-03-04 | 2010-07-21 | 陕西科技大学 | Three-phase biological fluidized bed |
| CN101973665A (en) * | 2010-09-28 | 2011-02-16 | 天津市天水环保设计工程有限公司 | A/O reactor with functions of air lift, backflow as well as rotation and mixing of reflux |
| CN101973665B (en) * | 2010-09-28 | 2011-12-21 | 天津市天水环保设计工程有限公司 | A/O reactor with functions of air lift, backflow as well as rotation and mixing of reflux |
| CN102079613A (en) * | 2010-12-22 | 2011-06-01 | 上海广联建设发展有限公司 | Ozone catalytic oxidation biological fluidized bed sewage treatment plant and treatment method using same |
| CN102134149A (en) * | 2011-05-10 | 2011-07-27 | 山东建筑大学 | Composite moving bed bio-film reactor |
| CN102134149B (en) * | 2011-05-10 | 2012-07-04 | 山东建筑大学 | Composite moving bed bio-film reactor |
| WO2014101764A1 (en) * | 2012-12-25 | 2014-07-03 | Zhu Yongqiang | Biological membrane fluidized bed wastewater treatment method |
| CN104609565A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Synchronous nitrification and denitrification treatment method of ammonia-containing wastewater |
| CN103755017A (en) * | 2014-01-22 | 2014-04-30 | 东南大学 | Aerobic biological fluidized bed device combining enriched oxygen aeration and oxygen filling method thereof |
| CN103755017B (en) * | 2014-01-22 | 2015-03-18 | 东南大学 | Aerobic biological fluidized bed device combining enriched oxygen aeration and oxygen filling method thereof |
| CN105439279A (en) * | 2014-09-25 | 2016-03-30 | 扬州天朗水务设备有限公司 | Biological fluidized bed |
| CN105110452A (en) * | 2015-08-12 | 2015-12-02 | 深圳市清研环境科技有限公司 | Sewage treatment apparatus and sewage treatment method therefor |
| CN107226523A (en) * | 2016-03-23 | 2017-10-03 | 国环清源控股有限公司 | A kind of continous way three phase fluidized bed |
| WO2018040753A1 (en) * | 2016-08-29 | 2018-03-08 | 武汉东川自来水科技开发有限公司 | Double-biomembrane sewage treatment system and method |
| CN108069505A (en) * | 2016-11-11 | 2018-05-25 | 南京理工大学 | A kind of inner loop three phase fluidized bed reactor |
| WO2020140841A1 (en) * | 2018-12-31 | 2020-07-09 | 中国石油化工股份有限公司 | Solid precipitation device and solid precipitation method |
| RU2805727C2 (en) * | 2018-12-31 | 2023-10-23 | Чайна Петролиум & Кемикал Корпорейшн | Device and method of sedimentation of solid sediments |
| CN113016577A (en) * | 2021-03-24 | 2021-06-25 | 湖北卓耳节水灌溉有限公司 | Water-saving irrigation system and irrigation method |
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