CN100528323C - Fluid bed reacting tower - Google Patents
Fluid bed reacting tower Download PDFInfo
- Publication number
- CN100528323C CN100528323C CNB2005100757099A CN200510075709A CN100528323C CN 100528323 C CN100528323 C CN 100528323C CN B2005100757099 A CNB2005100757099 A CN B2005100757099A CN 200510075709 A CN200510075709 A CN 200510075709A CN 100528323 C CN100528323 C CN 100528323C
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- CN
- China
- Prior art keywords
- fluid bed
- bed reacting
- reacting tower
- fluidising chamber
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00654—Controlling the process by measures relating to the particulate material
- B01J2208/00681—Agglomeration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1946—Details relating to the geometry of the reactor round circular or disk-shaped conical
Abstract
A fluidized-bed reaction tower with stabilized gas flow optimized gas and solid distribution and advanced discharge of collected material features that its fluidizing chamber has a conic sleeve casing and an inserted conic body in said conic sleeve casing to form a ring space between them, resulting in constant, incremental or decremental flow speed of gas.
Description
Technical field
The present invention relates to fluid bed reacting tower, it has a fluidising chamber, a gas feed and a gas vent.Gas feed in case of necessity and gas vent can be designed as a plurality of.
Background technology
In the described reaction tower running, one is known as fluid bed, forms in fluidising chamber.We are appreciated that it is the mixture of gas and solid matter, is in turbulent condition.Because fluid bed has turbulent flow, make very good that the solid matter, gas and the water that enter fluid bed mix between mutually, so might produce best mass transfer or absorption here.Classical fluidized bed, recirculating fluidized bed or so-called reverse-flow type recirculating fluidized bed reaction tower all are used to various chemical processes.In most cases, gas passes reaction tower from bottom to top.After the gas access, reaction tower has a shrinking zone, and it can be made up of a fluidisation plate (perforated plate), perhaps forms (below be described as nozzle bottom) by single or multiple nozzles.At this constriction zone, gas velocity should be enough high so that top solid particle can not fall.Above the shrinking zone, a fluidising chamber is arranged, it can be a cylinder, cone, or a tapered segment is followed a column part again.On fluidising chamber, many reaction towers have a gas outlet tube, points sideways on sidewall.The gas outlet tube that arrange other design centre is to point to the top.The major defect of the fluid bed reacting tower design known to everybody is: the gas of changes in flow rate (for example being caused by up-stream system) causes the fluid bed fluctuation through regular meeting; thereby reduce the efficient and/or the lasting interference of initiation of technological process, as operation to up-stream system to moving.Solution is gas recirculation (gas returns) or increases auxiliary air in the inlet air flow of reaction tower, passes through the minimum air flow amount of reaction tower like this, in most of the cases can not be lower than 60% of full load rate.And because the fluctuation that the system that is connected with reaction tower usually needs flow between 30% to 100%, so to expend sizable energy and cost of equipment, with the technical process in the stopping reaction tower (increasing gas flow rate) extremely greater than 60%.
Summary of the invention
First purpose of the present invention, create a kind of fluid bed reacting tower exactly, its fluid bed can be close under the stable parameter (especially stable gas flow rate) operation, even under the charge flow rate that changes (for example 30% to 100%) situation, also can carry out the optimization adjustment.
For realizing above-mentioned first goal of the invention, fluid bed reacting tower 1 of the present invention, its fluidising chamber 4 comprises a taper shape or parabola shaped sheath body 3, it also is the insert 2 of circular cone or parabolic shape that this sheath body accommodates one.By this design, formed an annular space that constitutes fluidising chamber 4 between sheath body 3 and insert 2, and produced a kind of gas flow rate, this gas flow rate can remain unchanged, or keep to reduce, keep increasing, this depends on the geometry of two kinds of assemblies.Therefore this reaction tower also is known as and stablizes the flow velocity reaction tower.
When (according to double-head arrow 5 directions) reduction or raising insert 2, the gas flow rate in the fluidising chamber can increase or reduce.So when the air velocity that enters reaction tower changed, by reducing or improving insert, the gas flow rate of an almost stable can obtain in annular space.
Fluidising chamber's 4 its cross sections that are the reaction tower annular space that can be designed to be furnished with can dwindle or enlarge (seeing Fig. 1 or Fig. 2).
The present invention makes the solution of previously known costliness seem unnecessary.And this invention can set up stable running environment, and common this running environment only may obtain just under stable gas flow rate under the very wide situation of load range.Stablize annular space reactor by using, the influence to upstream or down-stream system is minimized.Annular space fluidized bed reactor, comply with geometry sheath body of the present invention and insert because of it, make the operation optimization of fluid bed become possibility---especially when the air velocity through fluid bed reacting tower changes---and can avoid strong negative effect thus upstream or down-stream system.
Another problem of fluid bed reacting tower known to everybody is: in not with stabilizing gas flow velocity operation " recirculating fluidized bed " and static fluid bed, aggregation can sink in fluidising chamber or fall, and most cases is along wall.When aggregation arrived constriction zone, they can be broken up by very high-speed gas, can cause sizable pressure peak like this, particularly within the load range of maximum airflow＜70%-80%.This pressure summit causes sizable interference to power plant's operation, thereby hinders the normal operation of power plant.
Address this problem, be second purpose of the present invention.
In order to address this problem, the inventor provides an agglomerate separator (see figure 4), it can be designed to an annular space opening 6 or be designed to the opening of a large amount of stagger arrangement, is arranged on the circumference of fluid bed reacting tower fluidising chamber, or is designed to an outlet of reaction tower center.This opening can be positioned at the conical big end below fluidising chamber's column part, just in the junction of big end of taper shape and cylindrical part; Also can be positioned at the cylindrical portion of traditional fluid bed reacting tower; Can also be nozzle bottom Anywhere or annular space fluidized bed outer wall or inner cone Anywhere.
Make the optimized agglomerate separator of fluid bed reacting tower, aggregation can be discharged away from fluidising chamber by the exhaust outlet of opening on the circumference or nozzle bottom.Particularly at the fluidized bed processes of operation under the different load, the present invention can create a more stable running environment, reduces the influence to connected system considerably.
The function of agglomerate separator is to separate recirculation aggregation and agglomerated thing from fluidising chamber 4.These solid matters can be sent into fluid bed once more by controlled or uncontrolled dispenser 8 then.As shown in Figure 4, the agglomerate separator of band shape space opening 6, here, solid matter is sent to the groove 7 that floats, and by such as being evenly distributed on several pipelines on the circumference etc., in a controlled manner, groove is sent to fluid bed reacting tower from floating.
Use this agglomerate separator, necessary expenditure before can reducing.And agglomerate separator has been created more stable running environment under the very wide situation of load range, and common this running environment only just might obtain in less load range (throughput).To the impact of reaction tower upstream or down-stream system, will minimize by the use of agglomerate separator.
Another problem of fluid bed reacting tower known to everybody is: exhanst gas outlet.In traditional reactor head design, contain the solid and gas body and be discharged into the top from the center or be discharged into the side by a direction.Because in this head zone, gas has a nuclear stream higher than other zone of reaction tower usually, and so-called " roller shape " flows and can occur, and causes the solids backflow along the reaction tower wall.If use the principle of central outlet towards the top, so " roller shape " to flow be uniformly, but may have a solid aggregate, their can sink along wall as aggregation.If the horizontal outlet of a side can partly be avoided this aggregate so, do not have so significantly that " roller shape " forms, but air-flow heterogeneity still has more obvious local aggregation and forms.
Avoid above-mentioned influence then to be the 3rd purpose of the present invention.
The invention enables the gas of load product can be earlier radially, discharging downwards then, promptly via annular arrangement opening (these openings preferably are evenly distributed on the circumference of reaction tower) or via wide-open annular space opening 11 discharging (see figure 3)s.Thus, arrive the solid of the reactor head that nuclear stream is arranged, will evenly be discharged to the path by minor axis in all directions.In this way, the size of the formation of aggregation and aggregation all is reduced.The fluidized bed processes of in the load (throughput) that changes, moving particularly.The present invention can create more stable running environment, reduces considerably on the reaction tower or the impact of down-stream system.
Description of drawings
The invention will be further described below in conjunction with the accompanying drawing example.
Fig. 1 mainly designs 1 structural principle schematic diagram for the fluidising chamber of annular space of the present invention.
Fig. 2 mainly designs 2 structural principle schematic diagrames for the fluidising chamber of annular space of the present invention.
Fig. 3 is an annular space gas vent schematic perspective view of the present invention.
Fig. 4 is a band agglomerate separator schematic perspective view of the present invention.
Fig. 5 is according to reaction tower simple flow chart of the present invention, a subsidiary downstream solids matter separator and solids recirculation passage.
The specific embodiment
According to Fig. 1 or Fig. 2, the fluidising chamber 4 of reaction tower 1 comprises a taper shape or parabola shaped sheath body 3, and it is the insert 2 of taper shape or parabolic shape equally that this sheath body accommodates one.By this design, having formed function between sheath body 3 and insert 2 is the annulus of fluidising chamber 4, and annulus produces gas velocity, and this speed both can remain unchanged, also can be that maintenance reduces or the maintenance increase, this depends on the geometry of two assemblies.So may also be referred to as, this reaction tower stablizes the flow velocity reaction tower.
By an adjusting device (not showing in detail), the direction of pressing double-head arrow 5 reduces or raising insert 2, and the geometry of annulus is changed, thereby the gas velocity in the fluidising chamber can increase or reduce.So, when the air velocity in sending into reaction tower changes,, can in annulus, obtain the gas flow rates of almost stable by reducing or improving insert 2.Annulus can be realized (seeing Fig. 1 or 2) by increasing or reducing fluidising chamber's cross section mode from bottom to top.
According to the present invention, reaction tower has an agglomerate separator (Fig. 4), it is designed to an annulus opening 6, or is designed to a large amount of stagger arrangement openings of arranging on the circumference of fluid bed reacting tower fluidising chamber, also is designed to be positioned at an outlet at reaction tower center.Agglomerate separator 6 openings can be positioned at the conical big end of fluidising chamber, just in big end of taper shape and cylindrical part junction, also can be positioned at the cylindrical part of traditional fluid bed reacting tower, can also be located at nozzle bottom Anywhere or annular space reaction tower exterior wall or inner cone Anywhere.Agglomerate separator can be guaranteed aggregation before falling nozzle bottom, was shifted by side direction on 7 li most of ground of unsteady groove.The remainder of aggregation, the opening of arrival nozzle bottom is removed from nozzle bottom by tapping equipment, and this tapping equipment does not show in detail.
The function of agglomerate separator is to separate from fluidising chamber 4 and the recirculation aggregation and the agglomerated thing that come.These solid matters can be sent into fluid bed once more by controlled or uncontrolled dispenser 8 then.
As shown in Figure 4, the agglomerate separator 6 that has the annulus opening.Here, solid matter is sent to the groove 7 that floats, and in a controlled manner, by such as the several pipelines 8 that are evenly distributed on the circumference, is sent to fluid bed reacting tower again from unsteady groove 7.
By this method, can reach more stable running environment in big load range, common this environment only might be realized in less load range (throughput).Use agglomerate separator that the impact to reaction tower upstream or down-stream system will be minimized.
As shown in Figure 3, a reaction tower that has annular arrangement exit opening 11, these openings preferably are evenly distributed on the circumference of reaction tower 1, and like this, the gas of load product is radial discharge, discharging 9 downwards if necessary time the then.So arriving the solid that the reactor head that core flows is arranged will be by shortest path, especially radially evenly discharged to all directions.In this way, the formation of aggregation be reduced with and size be reduced.Particularly to the fluid mapper process of operation in the load (throughput) that changes, the present invention can create stable operation environment more, and certain degree ground reduces the impact to reaction tower up-stream system or down-stream system.
The annulus outlet can also be assembled gas channeling cone 10 (see figure 2)s, and it can improve the discharging of gas and solid mixture more.
The gas feed of fluid bed reacting tower of the present invention it be: at least one nozzle or annular space nozzle/nozzles.
As Fig. 5, fluid bed reacting tower of the present invention is connected with a downstream solid matter separator 12, and it links to each other by slideway with a container or unsteady groove 13 or is linked to be a unit 14, and the solid that is separated just is collected in the separator.And container or unsteady groove 13 also have passage 15 to link to each other with reaction tower 1, and the solid matter that is collected is from being transported back reaction tower 1 and/or discharging here.
Fluid bed reacting tower of the present invention is characterized in that: described downstream solids matter separator 12 is for controlled, and when air-flow hour, the pressure reduction of separator is just low, and when air-flow was big, separator pressure reduction was just high.
Fluid bed reacting tower of the present invention can be used for:
A: purify smelting furnace or incinerate the flue gas of factory;
B: the gas mixture that purifies any kind of;
C: burning fuel or rubbish in the fluid bed;
D: Catalytic processes flow process, absorbing process flow process and/or absorption technique flow process;
E: the conversion that produces by the contained material chemical reaction of fluid bed.
Claims (10)
1, fluid bed reacting tower (1), it is characterized in that: the fluidising chamber (4) of described fluid bed reacting tower (1) is equipped with available its and adjusts the insert (2) in fluidising chamber (4) cross section, and under that change or stable throughput, can adjust gas flow rate, that is: fluidising chamber (4) comprises that one is the sheath body (3) of taper shape or parabolical to the longitudinal axis, it accommodates one also is the insert (2) of taper shape or parabolical concerning the longitudinal axis, so between the outer surface of the inner surface of sheath body (3) and insert (2), just formed an annular space that constitutes fluidising chamber (4); And fluid bed reacting tower (1) is equipped with adjusting device, can axially adjust position between sheath body (3) and the insert (2) to change the area in annular space cross section.
2, fluid bed reacting tower according to claim 1 (1) is characterized in that: an outlet is arranged directly over the bottom nozzle of described fluidising chamber (4), and by this outlet, solid can become the centrality discharging from fluidising chamber (4) lining.
3, fluid bed reacting tower according to claim 1 (1) is characterized in that: an outlet is arranged directly over the bottom nozzle of described fluidising chamber (4), and by this outlet, aggregation can become the centrality discharging from fluidising chamber (4) lining.
4, fluid bed reacting tower according to claim 1 (1), it is characterized in that: described fluid bed reacting tower (1) connects a downstream solids matter separator (12), it links to each other by slideway with a container (13) or a synthetic unit (14), the solid matter that is separated just is collected in the solid matter separator (12), and container (13) also has passage (15) to link to each other with fluid bed reacting tower (1), and the solid matter that is collected is from being transported back fluid bed reacting tower (1) and/or discharging here.
5, fluid bed reacting tower according to claim 1 (1) is characterized in that: the gas vent of described fluid bed reacting tower (1) has a tapered insert (10).
6, fluid bed reacting tower according to claim 1 (1) is characterized in that: described fluid bed reacting tower (1) is used for:
A: purify smelting furnace or incinerate the flue gas of factory;
B: the gas mixture that purifies any kind of;
C: the conversion that produces by the contained material chemical reaction of fluid bed;
D: absorbing process flow process and/or absorption technique flow process.
7, fluid bed reacting tower according to claim 4 (1) is characterized in that: described container (13) is the groove that floats.
8, according to claim 2 or 3 described fluid bed reacting towers (1), it is characterized in that: the gas feed of described fluid bed reacting tower (1) it be: at least one nozzle.
9, according to claim 2 or 3 described fluid bed reacting towers (1), it is characterized in that: the gas feed of described fluid bed reacting tower (1) it be: annular space nozzle/nozzles.
10, fluid bed reacting tower according to claim 6 (1) is characterized in that: described by being converted into that the contained material chemical reaction of fluid bed produces: burning fuel or rubbish in the fluid bed, Catalytic processes flow process.
Priority Applications (10)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100757099A CN100528323C (en) | 2005-06-03 | 2005-06-03 | Fluid bed reacting tower |
| BRPI0611328-1A BRPI0611328A2 (en) | 2005-06-03 | 2006-06-02 | fluidized bed reactor |
| PCT/CN2006/001197 WO2007009334A1 (en) | 2005-06-03 | 2006-06-02 | FLUlDIZED BED REACTOR |
| RU2008100026/21A RU2403966C2 (en) | 2005-06-03 | 2006-06-02 | Reactor with pseudoliquid layer |
| NZ58897606A NZ588976A (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
| NZ564804A NZ564804A (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
| CA2610826A CA2610826C (en) | 2005-06-03 | 2006-06-02 | Fluldized bed reactor having a variable cross section |
| CNA200680019515XA CN101189061A (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
| AU2006272299A AU2006272299B2 (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
| AU2011200770A AU2011200770A1 (en) | 2005-06-03 | 2011-02-23 | Fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100757099A CN100528323C (en) | 2005-06-03 | 2005-06-03 | Fluid bed reacting tower |
Related Child Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910170677A Division CN101683603A (en) | 2005-06-03 | 2005-06-03 | Fluidized bed reaction tower |
| CN200910170678A Division CN101708449A (en) | 2005-06-03 | 2005-06-03 | Fluidized bed reaction tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1712121A CN1712121A (en) | 2005-12-28 |
| CN100528323C true CN100528323C (en) | 2009-08-19 |
Family
ID=35718023
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100757099A Expired - Fee Related CN100528323C (en) | 2005-06-03 | 2005-06-03 | Fluid bed reacting tower |
| CNA200680019515XA Pending CN101189061A (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA200680019515XA Pending CN101189061A (en) | 2005-06-03 | 2006-06-02 | Fluidized bed reactor |
Country Status (7)
| Country | Link |
|---|---|
| CN (2) | CN100528323C (en) |
| AU (2) | AU2006272299B2 (en) |
| BR (1) | BRPI0611328A2 (en) |
| CA (1) | CA2610826C (en) |
| NZ (2) | NZ588976A (en) |
| RU (1) | RU2403966C2 (en) |
| WO (1) | WO2007009334A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120179097A1 (en) * | 2011-01-06 | 2012-07-12 | Cully Edward H | Methods and apparatus for an adjustable stiffness catheter |
| RU2650154C1 (en) | 2016-12-16 | 2018-04-09 | Общество с ограниченной ответственностью "Биологические Источники Энергии" (ООО "БиоИстЭн") | Device with a fluidized spouted bed of annular form and the method of its work |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2092365U (en) * | 1991-03-27 | 1992-01-08 | 中国科学院化工冶金研究所 | Reactor of combined rapid fludized bed |
| CN2215346Y (en) * | 1994-12-23 | 1995-12-20 | 中国科学院兰州化学物理研究所 | Fluidized-bed reactor |
| DE19945033A1 (en) * | 1999-09-20 | 2001-03-22 | Juergen Karl | Apparatus for inserting solid and pasty materials into the fixed or fluidized bed of a stationary fluidized bed reactor comprises a vertical or a weakly slanted down pipe which protrudes into the reactor |
-
2005
- 2005-06-03 CN CNB2005100757099A patent/CN100528323C/en not_active Expired - Fee Related
-
2006
- 2006-06-02 CN CNA200680019515XA patent/CN101189061A/en active Pending
- 2006-06-02 CA CA2610826A patent/CA2610826C/en not_active Expired - Fee Related
- 2006-06-02 NZ NZ58897606A patent/NZ588976A/en not_active IP Right Cessation
- 2006-06-02 WO PCT/CN2006/001197 patent/WO2007009334A1/en active Application Filing
- 2006-06-02 NZ NZ564804A patent/NZ564804A/en not_active IP Right Cessation
- 2006-06-02 BR BRPI0611328-1A patent/BRPI0611328A2/en not_active IP Right Cessation
- 2006-06-02 AU AU2006272299A patent/AU2006272299B2/en not_active Ceased
- 2006-06-02 RU RU2008100026/21A patent/RU2403966C2/en not_active IP Right Cessation
-
2011
- 2011-02-23 AU AU2011200770A patent/AU2011200770A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| NZ588976A (en) | 2011-03-31 |
| WO2007009334A1 (en) | 2007-01-25 |
| AU2006272299B2 (en) | 2010-11-25 |
| CA2610826A1 (en) | 2007-01-25 |
| NZ564804A (en) | 2010-12-24 |
| CA2610826C (en) | 2013-07-30 |
| RU2403966C2 (en) | 2010-11-20 |
| AU2011200770A1 (en) | 2011-03-17 |
| CN1712121A (en) | 2005-12-28 |
| AU2006272299A1 (en) | 2007-01-25 |
| BRPI0611328A2 (en) | 2011-02-22 |
| CN101189061A (en) | 2008-05-28 |
| RU2008100026A (en) | 2009-07-20 |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090819 Termination date: 20160603 |