WO2005119154A1 - Thick slurry heating system - Google Patents
Thick slurry heating system Download PDFInfo
- Publication number
- WO2005119154A1 WO2005119154A1 PCT/AU2005/000781 AU2005000781W WO2005119154A1 WO 2005119154 A1 WO2005119154 A1 WO 2005119154A1 AU 2005000781 W AU2005000781 W AU 2005000781W WO 2005119154 A1 WO2005119154 A1 WO 2005119154A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- slurry
- heating system
- slurry heating
- inner tubes
- units
- Prior art date
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0098—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for viscous or semi-liquid materials, e.g. for processing sludge
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2280/00—Mounting arrangements; Arrangements for facilitating assembling or disassembling of heat exchanger parts
- F28F2280/02—Removable elements
Definitions
- This invention relates to a heating system used in processing of dense slurries and similar types of viscous fluids.
- this invention relates to a slurry heating system suitable for heating dense slurries handled in the Bayer digestion process, in which aluminium hydroxide is extracted from bauxite.
- bauxite is usually wet milled with a caustic soda solution, usually referred to as spent liquor.
- the resulting bauxite slurry (referred to as thick bauxite slurry) must be heated prior to further dilution with hot spent liquor, after which it is conveyed to the digestion plants.
- indirect heating the increase in the slurry temperature is achieved by heat transfer equipment.
- direct heating steam or vapour is injected directly into the slurry.
- the latter form of heating is often employed because the equipment required is extremely simple and reliable and avoids a number of serious problems associated with the more complex conventional heat transfer equipment utilised in previous attempts at indirect heating.
- the major disadvantage of direct heating is that it adds the condensate created by the injected vapour to the liquor stream and thereby dilutes the process liquor stream.
- the process liquor stream is a recirculating flow that must be maintained at a certain concentration. Any water added to the process will steadily dilute the process liquor stream and is therefore removed by forced evaporation in other parts of the Bayer process, before it is returned to the digestion plant. Forced evaporation is an expensive process and there are significant advantages in elimination of direct injection in favour of suitable and reliable heat exchange equipment.
- There are several problems associated with the heating of thick bauxite slurry The slurry is essentially viscous. It has a shear stress at zero flow and exhibits marked non-Newtonian behaviour.
- Shell and tube heat exchangers of conventional design have been tried, but in regard to thick slurry heating they experience a number of significant problems.
- the flow path offered by conventional 25 or 38 mm diameter heat exchanger tubes is insufficient to guarantee blockage free operation. Viscous fluids in general are difficult to heat using shell and tube heaters.
- Shell and tube heaters normally operate in the turbulent flow regime where heat transfer coefficients are considerably greater than those attainable in the laminar flow regime. High viscosities and high shear values position the flow in the laminar regime (low Reynolds number). In the laminar regime there is a reduction or absence of turbulence, which results in poor mixing between the outer layers and the core of the flow.
- High-density bauxite slurry is also termed a 'power-law' fluid. This means that the velocity distribution across the tube diameter does not adhere to the same exponential functions that rule the velocity distribution in pure fluids. This causes slurry flow to be less turbulent than the pure fluids in laminar flow, resulting in even less exchange of heat between the fluid temperature attained at the tube wall and the core of the flow area.
- Bauxite slurry is also a 'shear-thinning' fluid. This means that in fluid elements subject to high shear rates, such as along the tube wall, the 'apparent viscosity' may reduce significantly. At extreme solid densities this shear thinning nature of thick bauxite slurry may cause plug flow. In plug flow, the velocity profile across the tube is essentially flat, with all fluid elements being transported at the same velocity. The only relative movement then occurs at a high shear lubricating laminar sub-layer along the tube wall. At this extreme flow regime there is effectively no mixing and indirect slurry heating is for all practical purposes impossible.
- the lower limit is determined by preventing Reynolds numbers that are too low.
- the upper limit is determined by preventing excessive tube wear.
- the preferred velocity is about 2 m/s, which, in the range of sizes likely to be utilised in tubular heating equipment, is independent of tube size. There is therefore no degree of freedom to significantly vary velocities for the particular tube size that has been employed. Given the velocity, smaller tubes will require a higher driving force in order to maintain flow. This higher pressure must be added to the back-pressure that must be maintained on the heater to prevent boiling of the slurry at the laminar sub-layer in the tubes. This adds significantly to both capital and operating (power) costs for pumps, pumping systems, the heat exchange equipment itself as well as any downstream equipment.
- a slurry heating system comprising a plurality of tube heat exchanger units, each of said units comprising a plurality of inner tubes arranged in parallel for single-pass operation, contained within an outer tube, each said unit having an internal wall located proximal to each opposed end of said inner tubes to fluidly isolate a heating volume from a slurry containing volume; said heating volume being located between said walls, said outer tube and said inner tube, and said slurry containing volume being located within said inner tubes and beyond either end of said inner tubes bound by said walls; each said unit having_a removable cover at least at one end to allow physical access to open ends of said inner tubes for cleaning purposes, said plurality of units being arranged in series with adjacent units in the series being connected by an interconnecting pipe or other interconnecting system that provides some turbulence in slurry flow between adjacent said units.
- This arrangement provides for the slurry to be remixed after passing through each unit.
- the remixing provides an element of turbulent flow, which compensates for uneven heating brought about due to laminar flow within the inner tubes in each unit. This effect will also be observed where remixing occurs in multi-pass units.
- said interconnecting pipe intersects said outer tube between at least one said wall and adjacent said removable cover.
- the volume between at least one said wall and adjacent said removable cover is minimised, to avoid low flow rate areas and attendant settling out of slurry.
- the heat source can be any fluid medium, but most preferably is either steam or hot condensate.
- said plurality of inner tubes are arranged for single-pass operation for parallel flow of slurry.
- the cross-sectional area of the interconnecting pipe is less than the combined cross-sectional area of the inner tubes in each unit.
- the cross-sectional area of the interconnecting pipe is less than 0.8 times the combined cross-sectional area of the inner tubes in each unit.
- the cross-sectional area of the interconnecting pipe is from about 0.5 to 0.75 times the combined cross-sectional area of the inner tubes in each unit.
- the interconnecting pipe has a nominal bore diameter of from 200mm to 300mm.
- the outer tube is circular in cross-section, and has a nominal bore diameter of from 400mm to 750mm.
- said plurality of inner tubes comprises from 10 to 60 individual inner tubes.
- said plurality of inner tubes comprises from 30 to 60 individual inner tubes.
- each end of each of said units is provided with a said removable end cover.
- said removable end cover comprises a quick-opening blind.
- said slurry heating system has from three to twelve said units arranged in series.
- said slurry heating system has from three to ten said units arranged in series.
- said slurry heating system has from three to seven said units arranged in series.
- said slurry heating system has from four to six said units arranged in series.
- said slurry heating system has five said units arranged in series.
- a plurality of said slurry heating systems can be arranged in parallel (so as to form an array).
- the number of slurry heating systems arranged in parallel depends on the total plant production requirement.
- said slurry heating system has a restrictor or pressure controller to maintain a higher pressure of said slurry within said slurry heating system. This arrangement will prevent boiling of said slurry, to prevent scale formation within said inner tubes.
- said restrictor comprises a valve
- Inner tubes should be as few and as large as possible, compatible with the requirements of maximum permissible inner tube velocities and the required heat transfer area.
- Figure 1 is a plan view of a single slurry heating system showing a series of tube heat exchanger units according to the embodiment
- Figure 2 is an end elevation of the series shown in figure 1
- Figure 3 is a side elevation of the series shown in figures 1 and 2
- Figure 4 is a cross section through one of the tube heat exchanger units.
- the embodiment of the invention provides a thick bauxite slurry heating system for use in heating slurry for processing in the Bayer process.
- Each heating system as illustrated in the drawing figures is designed for a throughput of at least 200 t/h, typically 500 to 700 t/h, and up to 1000 t/h of slurry containing approximately 40% to 50% solids by weight. These are the approximate quantities of thick slurry required for digestion plants with capacity equivalent to 350 000 tpa (typically 700 000 tpa to 1 000 000 tpa) and 1 400 000 tpa of alumina respectively when extracted from bauxite containing approximately 50% available alumina.
- Each heating system consists of tube heat exchanger units 11 , 12, 13, 14, and 15, combined into a series by interconnecting pipes in the form of flanged pipe connections 21 , 22, 23, 24 arranged either horizontally or at an inclination equal to the hydraulic gradient for the same slurry flow under gravity.
- Each tube heat exchanger unit 11 , 12, 13, 14, and 15 is supported on a common structural support 25.
- Each tube heat exchanger unit 11 , 12, 13, 14, and 15 is single pass, comprising 34 inner tubes 30 of 50mm nominal bore (ID), enclosed in a 600mm nominal bore (ID) outer tube 32.
- the inner tubes 30 are held in place by and sealed into a wall in the form of a 38mm thick steel sheet 35 located near each end of each outer tube 32, and at opposed ends of the inner tubes 30.
- the inner tubes 30 are located in a triangular configuration relative to each other, and are spaced apart by a minimum of about 10mm. These sheets 35 effectively create slurry chambers 41 to 50 (inclusive) that distribute the slurry into and receive slurry from the individual inner tubes 30.
- the volume outside of the inner tubes 30 and inside the outer tube 32, bound by the walls formed by the steel sheets 35 defines a heating volume, which will be discussed later.
- the inner tubes 30 are approximately 6 m long.
- the interconnecting pipes forming the flanged pipe connections 21 , 22, 23, 24 have a nominal diameter of 250mm.
- the area formed by the diameter of the pipes forming the flanged pipe connections 21 , 22, 23, 24 is about 0.75 times the sum of the area formed by the diameter of the inner tubes 30. This change in area gives rise to a relative difference in velocity of the slurry in the interconnecting pipes forming the flanged pipe connections 21, 22, 23, 24 compared with the velocity in the inner tubes 30. This assists in creating conditions of turbulent flow, and significantly increases heat transfer efficiency in the next pass.
- Each outer tube 32 is furnished with a removable end cover in the form of a quick opening blind 60 at each end. This provides access into the slurry chambers 41 to 50 (inclusive) and into the insides of the inner tubes 30, allowing any build-up inside the inner tubes to be cleaned, to maintain the heat transfer efficiency of the unit.
- the five tube heat exchanger units 11, 12, 13, 14, and 15 can be made from standard piping materials.
- the outer tubes 32 and inner tubes 30 are manufactured from standard pipe, which has the advantage of being a standard off-the-shelf item, reducing the cost of fabrication of the slurry heater.
- the series of tube heat exchanger units 11, 12, 13, 14, and 15 has a slurry inlet 70 where slurry enters, and a slurry outlet 80 where heated slurry exits the series.
- an array of a plurality of heating systems in parallel each consisting of the series of tube heat exchanger units 11 , 12, 13, 14, and 15 can be provided.
- the number of heating systems required depends on total plant production.
- an array comprising five parallel streams fed by five feed pumps, four of which (streams and pumps) are in use while one stream and pump is on standby and available if any stream comes off-line for maintenance etc.
- backpressure control for each stream is provided in the form of a valve 90, operation of which is controlled by a pressure sensor (not shown).
- the valve is controlled to ensure that the pressure within the heater pipes is above the equilibrium vapour pressure of the maximum temperature that can be reached on the inner surface of the heater pipes.
- the theoretical limit of this minimum required back-pressure is the equilibrium vapour pressure at the temperature of the heating medium.
- the design heat transfer coefficient, based on maximum scale conditions, is 300 W/m 2 °C to 500 W/m 2 °C, or 260 kcal/m 2 h°C to 430 kcal/m 2 h°C.
- the pressure in the slurry is controlled dependent on local temperatures generated in the slurry at the inner wall of the inner tube, to a level equal to or just greater than the vapour pressure of the heating medium. This precaution is taken because the limited turbulence in the inner tubes will cause the temperature of the slurry at the inner tube walls to be noticeably higher than for fully turbulent flow.
- the outer tubes 32 each have a 150mm nominal bore heating fluid injection inlet 92 and a 50mm nominal bore condensate outlet 94 connecting respectively to a 250mm nominal bore heating fluid header 100 and 50mm nominal bore condensate drains 110.
- the condensate from the drains 110 is collected in a receiver vessel and returned to other plant operations.
- the heating fluid injection inlet 92 can receive live steam or hot condensate, depending on the required temperature.
- the heating fluid injection inlet 92 and a condensate outlet 94 communicate with the heating volume as defined above, to heat slurry within the inner tubes 30.
- the intent of the arrangement of the five tube heat exchanger units 11 , 12, 13, 14, and 15 is to eliminate complex channel sections, while still allowing the fluid to be mixed at relatively small length to diameter ratio (L/D) intervals. This mixing is desirable owing to the near laminar flow conditions through the inner tubes 30, which may result in an uneven temperature distribution.
- the use of relatively large diameter inner tubes 30 in the tube heat exchanger units 11 , 12, 13, 14, and 15 minimises the pressure drop along the series of units, and also avoids inner tube blockage.
- the five tube heat exchanger units 11 , 12, 13, 14, and 15, with their small size and quick opening blinds 60 allow easy heater cleaning, without the need for removing heavy covers or channel sections. Cleaning can be accomplished by water hose at normal plant water pressure, although high-pressure water jet cleaning is not precluded.
- the slurry needs to be heated with a reasonably large difference between the temperature of the slurry to be heated and the temperature of the heating fluid (approach temperature).
- the resulting temperature difference between the inner and outer surfaces of the inner tubes 30 wall when transferred to the semi-laminar flow of the outer layers of slurry adjacent to the inner surface of the inner tubes 30, will cause a measurable degree of turbulence due to convection.
- This convection together with the limited turbulence due to flow, will enhance the mixing of the hot and cold regions of slurry across the inner tubes 30 section.
- the lack of complete turbulence may cause the temperature in the outer layers of the slurry flow to be considerably higher than the mean temperature. Together with the low vapour pressure of the product being heated, the outer layers of slurry can therefore easily reach boiling point. This would lead to evaporation of the liquor content and to baking of the solids onto the inner surface of the inner tubes 30. This would cause rapid heater pipe-side fouling and would prevent effective heat transfer. Use of the backpressure control to raise the pressure of the slurry assists in preventing this problem from occurring.
- the invention has a number of advantages over hitherto known methods for heating bauxite slurry.
- the invention achieves process benefits of indirect heating, avoiding unwanted dilution that causes lower caustic concentrations in slurry leaving digestion and hence consequent constraints on digester productivity.
- the introduction of turbulent zones avoids need for large heat exchange areas, usually resulting from inherently low slurry film heat transfer coefficients in high bauxite slurry viscosities with inherent low Reynolds numbers.
- a benefit of smaller heat transfer apparatus is reduced capital cost and in addition, lower operating cost due to reduced de-scaling requirements.
- the invention achieves high heat fluxes without risk of slurry boiling in proximity to the inner tube walls (and resulting scale generation).
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2005250509A AU2005250509B2 (en) | 2004-06-01 | 2005-06-01 | Thick slurry heating system |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2004902884 | 2004-06-01 | ||
AU2004902884A AU2004902884A0 (en) | 2004-06-01 | Thick Slurry Heating System |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2005119154A1 true WO2005119154A1 (en) | 2005-12-15 |
Family
ID=35463001
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/AU2005/000781 WO2005119154A1 (en) | 2004-06-01 | 2005-06-01 | Thick slurry heating system |
Country Status (1)
Country | Link |
---|---|
WO (1) | WO2005119154A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2006092005A1 (en) * | 2005-03-02 | 2006-09-08 | Alcoa Of Australia Limited | Heat exchange apparatus |
AU2006201746B2 (en) * | 1994-06-07 | 2011-05-19 | Hatch Pty Ltd | Improved Multi-Cell Heating System |
EP2565572A1 (en) * | 2011-09-02 | 2013-03-06 | Aurotec GmbH | Heat exchange conduit system |
CN106197088A (en) * | 2016-08-19 | 2016-12-07 | 张家港市德胜染整有限责任公司 | A kind of waste-heat recovery device of dyeing waste-water |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59204692A (en) * | 1983-05-09 | 1984-11-20 | Babcock Hitachi Kk | Slurry heater |
JPH0428916A (en) * | 1990-05-24 | 1992-01-31 | Ube Ind Ltd | Slurry heater |
JPH08313177A (en) * | 1995-05-15 | 1996-11-29 | Nippon Pipe Syst Kk | Multi-tube type heat exchanger |
-
2005
- 2005-06-01 WO PCT/AU2005/000781 patent/WO2005119154A1/en active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59204692A (en) * | 1983-05-09 | 1984-11-20 | Babcock Hitachi Kk | Slurry heater |
JPH0428916A (en) * | 1990-05-24 | 1992-01-31 | Ube Ind Ltd | Slurry heater |
JPH08313177A (en) * | 1995-05-15 | 1996-11-29 | Nippon Pipe Syst Kk | Multi-tube type heat exchanger |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU2006201746B2 (en) * | 1994-06-07 | 2011-05-19 | Hatch Pty Ltd | Improved Multi-Cell Heating System |
WO2006092005A1 (en) * | 2005-03-02 | 2006-09-08 | Alcoa Of Australia Limited | Heat exchange apparatus |
EP2565572A1 (en) * | 2011-09-02 | 2013-03-06 | Aurotec GmbH | Heat exchange conduit system |
WO2013030402A2 (en) | 2011-09-02 | 2013-03-07 | Aurotec Gmbh | Heat exchanger pipe system |
WO2013030402A3 (en) * | 2011-09-02 | 2013-04-25 | Aurotec Gmbh | Heat exchanger pipe system |
CN103988040A (en) * | 2011-09-02 | 2014-08-13 | 奥若泰克股份有限公司 | Heat exchanger pipe system |
TWI586931B (en) * | 2011-09-02 | 2017-06-11 | Aurotec Gmbh | Heat exchanger pipe system |
US10557668B2 (en) | 2011-09-02 | 2020-02-11 | Aurotec Gmbh | Pipe system including internal heat exchangers |
CN106197088A (en) * | 2016-08-19 | 2016-12-07 | 张家港市德胜染整有限责任公司 | A kind of waste-heat recovery device of dyeing waste-water |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US8607850B2 (en) | Method for processing a mineral ore slurry | |
US4584932A (en) | Apparatus for heat-treating a liquid product | |
US6626235B1 (en) | Multi-tube heat exchanger with annular spaces | |
WO2005119154A1 (en) | Thick slurry heating system | |
AU2013205314B2 (en) | Thick Slurry Heating System | |
AU2005250509B2 (en) | Thick slurry heating system | |
RU2237676C2 (en) | Apparatus and method for preliminary heating of polymer solution | |
KR100245547B1 (en) | Heating and/or cooling of vessels | |
AU2006201746B2 (en) | Improved Multi-Cell Heating System | |
EP0706415B1 (en) | Multi-cell heating system | |
EP0586747A1 (en) | Heat exchanger system with turbulator for particle-in-liquid dispersion | |
CN104142073B (en) | Carbonated drink plate-type heat-exchange unit | |
WO2003021177A1 (en) | Piping system and method of making the same and associated method of heat transfer | |
CN218723357U (en) | Water comprehensive utilization device in middle of production process | |
EP2877799A1 (en) | An improved tubular heat exchanger | |
EP0212011B1 (en) | Multistage evaporation boiling equipment | |
AU2014231761A1 (en) | Shell and tube heat exchanger arrangement | |
RU2371228C2 (en) | Heating method of scale-forming solutions at evaporation and heat-exchanger for its implementation | |
AU676920B2 (en) | Multi-cell heating system | |
US20240018416A1 (en) | Hydrothermal liquefaction system with heat exchanger network | |
EP2766110B1 (en) | Process for the production of a polymer | |
WO2007049974A1 (en) | Fluid cooling means and method | |
CN111285421A (en) | Methanol-to-olefin sewage stripping tower system | |
Klaren et al. | Achievements and Potential of Self-Cleaning Heat Exchangers Using Untreated Natural Seawater as a Coolant | |
WO2016172758A1 (en) | Processing plant arrangement |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KM KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NG NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SM SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): BW GH GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
DPEN | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed from 20040101) | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2005250509 Country of ref document: AU |
|
WWE | Wipo information: entry into national phase |
Ref document number: 7222/DELNP/2006 Country of ref document: IN |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWW | Wipo information: withdrawn in national office |
Ref document number: DE |
|
ENP | Entry into the national phase |
Ref document number: 2005250509 Country of ref document: AU Date of ref document: 20050601 Kind code of ref document: A |
|
WWP | Wipo information: published in national office |
Ref document number: 2005250509 Country of ref document: AU |
|
122 | Ep: pct application non-entry in european phase |