Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
  • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
  • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
  • B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
  • B04C5/18—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations with auxiliary fluid assisting discharge
• • 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
  • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
• • 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
  • B01J8/26—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 two or more fluidised beds, e.g. reactor and regeneration installations
  • B01J8/28—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 two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
• • 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
  • B01J8/386—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 internally, i.e. the particles rotate within the vessel
• • 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
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
  • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
  • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
  • B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
  • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

• the invention is directed to a cyclone separator provided with an inlet for receiving gas and solid particles, a gas outlet at its upper end and a lower tubular part.
• the invention is especially directed to such a cyclone separator as part of a fluid catalytic cracking (FCC) reactor wherein the cyclone separator is fluidly connected to the downstream part of an elongated reactor riser and wherein the gas is cracked hydrocarbon vapours and the solids are cracking catalyst particles .
• FCC fluid catalytic cracking
• the reactor riser is fluidly connected to one or more primary cyclones, which are in turn connected to one or more secondary cyclones each.
• the cleaned gas obtained in the secondary cyclone is discharged at the upper end of the reactor vessel.
• the primary and secondary cyclones discharge the separated FCC catalyst particles to below into a dense fluidized bed via their respective diplegs.
• As fluidization gas steam is added in order to strip adsorbed and/or entrained hydrocarbons, which are present in the catalyst flow.
• stripped catalyst particles are discharged from the vessel and transported to a separate regenerator vessel.
• coke is removed by means of combustion from the catalyst in order to provide a regenerated catalyst, which can be reused in the reactor riser.
• a disadvantage of the above-described process is that the stripping efficiency of existing units is often too low.
• the aim of the present invention is to provide a cyclone separator which use results in an improved stripping efficiency.
• Cyclone separator provided with an inlet for receiving gas and solid particles, a gas outlet at its upper end and a lower tubular part, wherein the lower tubular part is provided with a closed lower end, through which closed lower end a substantially vertical particle withdrawal conduit extends from a position below the closed lower end to a position in the tubular part and below the inlet for receiving gas and solid particles, said conduit being provided with openings to withdraw solid particles from the cyclone separator and wherein said conduit has a smaller cross-sectional area than the lower tubular part, thereby defining a space between conduit and inner wall of the lower tubular part, wherein in the lower part of said space main means to add a primary fluidizing medium are present.
• the cyclone according to the invention can enhance the overall stripping efficiency when used in a fluid catalytic cracking unit and when the fluidizing medium added to the lower end of the cyclone is a stripping medium, for example steam.
• a next advantage is that many existing FCC reactors provided with cyclone separators can easily be modified into the reactor according to the invention.
• a further advantage is that the operation of the cyclone provided with the solids discharge conduit and its fluidised bed is less dependent of the pressure outside the cyclone separator.
• the separation efficiency of, for example, the prior art FCC cyclone, not having this specific lower tubular end is influenced by the pressure fluctuations in the FCC reactor vessel.
• the separation efficiency of a separation system comprising said cyclone and secondary separation means, for example a secondary cyclone is not significantly negatively affected when compared to a separation system comprising a state of the art primary and secondary cyclone.
• a dense fluidised bed will be present in the, preferably annular, space between the catalyst withdrawal conduit and the inner wall of the tubular part.
• the bed is kept in a fluidization mode by means of primary fluidization gas supplied to the lower end of the dense fluidised bed. Solids may be withdrawn from this fluidization zone via the openings present in the particle withdrawal conduit.
• one or more openings are present in the upper end of the catalyst withdrawal conduit.
• the upper end of the particle withdrawal conduit is open. The upper most positioned openings in the conduit define the maximum fluidised bed level.
• one or more openings are also present in the lower half of the particle withdrawal conduit through which solids can be discharged from the cyclone.
• the fluidised bed in the lower tubular part of the cyclone separator also functions as a stripping zone, as for example in a FCC configuration.
• the opening at the upper end of the withdrawal conduit will then only serve as withdrawal opening in case of blockage of the secondary openings by for example coke or debris. In this manner more counter-current contact between stripping medium and catalyst takes place in the fluidised bed zone, which is advantageous for the stripping efficiency. More preferably a row of such openings at the same elevation are present in the lower half of the conduit.
• Even more preferably two or more of such rows are present above each other, wherein, in use, most solid particles will flow through the lower openings while through the upper openings gas is vented and pressure is balanced.
• the same effect of the two rows can be achieved by making use of rectangular designed openings, wherein the elongated side of the opening extends upwards.
• Other possible shapes of the openings are, for example, circular, keyhole shaped, oval shaped or straight-sides holes with circular ends. These openings are suitably at the same elevation or above the position of the means to add the primary fluidizing medium, such to ensure that the solid particles are sufficiently fluidised to flow easily through the openings.
• a preferred opening to withdraw solid particles from the lower tubular part of the cyclone is one or more substantially horizontal conduits fluidly connecting the lower tubular part and the particle withdrawal conduit, wherein said substantially horizontal conduit is provided with means to add a secondary fluidizing medium.
• This substantially horizontal conduit is positioned below the position of the means to add the primary fluidizing medium of the separation cyclone as described above.
• solid particles will not or at a very small rate flow through these substantially horizontal conduits.
• the flow of solid particles will increase significantly. If for example FCC catalyst particles are the solid particles • the flow rate can be increased to more than 10 times by adding the secondary fluidizing medium to the connecting conduit.
• a well-defined and controlled bed level is advantageous because all solid particles will be sufficiently contacted with the fluidizing medium before being withdrawn from the fluidised bed.
• the fluidizing medium is a stripping gas a more efficient stripping of FCC catalyst particles is thus achieved.
• the number of such connecting conduits can be from one to forty or more, but preferably from four to sixteen.
• the means to supply stripping gas suitably comprises at least one gas injection ring.
• This gas injection ring may be connected to a stripping gas supply conduit which is either connected to the stripping supply means of the main stripping bed at the lower end of the reactor vessel, if present, or which transfers the reactor vessel wall near the cyclone itself.
• Preferred stripping medium is steam.
• the cyclone in a FCC configuration is preferably designed to ensure a minimum residence time of the FCC catalyst particles in the dense fluidised bed.
• said minimum residence time of the catalyst is 5 seconds, more preferably this residence time is greater than 10 seconds, most preferably this residence time is more than 30 seconds.
• the residence time will be less than 60 seconds.
• a horizontal plate may suitably be present just above said opening. More preferably a vortex stabiliser is used to terminate the vortex before it reaches the open end of the withdrawal conduit.
• the vortex stabiliser may comprise of a vortex stabiliser plate arranged perpendicular to the central vertical axis of the cyclone and a vortex finder rod arranged parallel to said axis and extending in the direction of the gas outlet of the vertical cyclone. The position of the vortex stabiliser will be between the upper end of the catalyst withdrawal conduit and the cyclone inlet for gas and solids.
• the cyclone separator according to the present invention is suitably used in a FCC process.
• the invention is especially directed to such a cyclone separator as part of a fluid catalytic cracking (FCC) reactor wherein the cyclone separator is fluidly connected to the downstream part of an elongated reactor riser and wherein the gas is cracked hydrocarbon vapours and the solids are cracking catalyst particles.
• the downstream end of the catalyst withdrawal conduit will then discharge catalyst particles to the lower end of the reactor.
• the reactor vessel may be suitably provided with a dense phase fluidised bed of catalyst at the lower end of the reactor vessel, provided with means to supply stripping medium as fluidization gas as for example described in the aforementioned US-A-5039397.
• Stripping vessels may also be part of the FCC unit comprising the reactor according to the invention.
• the invention can find application in new FCC reactors or by modification of existing FCC reactors.
• Existing FCC reactors which may be modified to a reactor according the present invention, will suitably comprise a reactor vessel comprising cyclone separation means fluidly connected to the downstream end of a reactor riser.
• Examples of such FCC reactors are illustrated in Figures 1-16, 1-17, 1-19, 1-21 and 1-22 as published in "Fluid Catalytic Cracking Technology and Operation" by Joseph W. Wilson, PennWell Publishing Company, Tulsa Oklahoma (US) , 1997, pages 31-39.
• the illustrated reactors describe both embodiments wherein the upper end of the reactor riser is placed within the reactor vessel or placed outside the reactor vessel.
• the location of the upper end of the reactor riser is not essential.
• the cyclone separator which is provided with the pre-stripping zone, is a so-called rough-cut cyclone or primary cyclone, in which the first separation is performed between catalyst and cracked vapour.
• Suitable 1 to 4 primary cyclones are fluidly connected to one reactor riser.
• the reactor vessel may be provided with further separation stages, for example secondary cyclones, to further separate catalyst fines from the cracked vapour.
• One primary cyclone may be fluidly connected to suitably 1 to 4 secondary cyclones.
• the design of the primary cyclone can vary.
• the cyclone may for example be a horizontal cyclone as described in EP-A-332277 or a conventional vertical cyclone.
• an existing primary cyclone may suitably be modified as described hereafter.
• An FCC reactor provided with cyclones having an upper tubular body, a converging sector connected at its lower side to a dipleg can be modified by replacing the converging part and part of the dipleg by a tubular part with a closed bottom as described above.
• the tubular part may have the same diameter as the diameter of the upper tubular body of the existing cyclone.
• the catalyst withdrawal conduit can be obtained by modification of the existing dipleg.
• the lower end of the catalyst withdrawal conduit may be submerged in the dense fluidized bed of catalyst of the stripping zone or terminate above said bed level. If the conduit terminates above the fluidized bed level it is preferably provided with a valve, for example as described in co-pending PCT application PCT/EP00/06591. If the conduit terminates below the fluidised bed level a horizontal plate is preferably present below the opening.
• the flow of catalyst in such a primary cyclone according to the present invention is suitably between
• Figure 1 illustrates the prior art FCC reactor vessel.
• Figure 2 illustrates a detail of a FCC reactor vessel according to the present invention.
• Figure 3 shows a preferred embodiment of the invention.
• Figure 4 illustrates a FCC process unit wherein no reactor vessel is used.
• Figure 5 illustrates the connecting conduits for control of the bed level in the tubular part.
• Figure 1 shows the upper part of a fluid catalytic cracking reactor (1) consisting of the upper part of an elongated reactor riser (2) and reactor vessel (3) .
• the reactor vessel (3) is provided with a catalyst outlet at its lower end (not shown), a cracked vapour outlet (4) at its upper end and a primary vertical cyclone separator (5) .
• the cyclone separator (5) is provided with an inlet (6) for receiving gas and catalyst from the outlet (7) of the reactor riser (2) .
• the cyclone further consists of an upper tubular part (8) , a converging part (9) and a dipleg (10) .
• the primary cyclone (5) is further provided with a roof (11) through which a gas outlet conduit (12) protrudes.
• Gas outlet conduit (12) is provided with an opening (13) for receiving stripping gas and stripped hydrocarbons, which flow from the lower situated fluidised dense stripping bed (14) .
• the conduit (12) is fluidly connected to ' the gas inlet of secondary cyclone (15) .
• Secondary cyclone (15) is provided with a dipleg (16) and a gas outlet (17), which is in fluid communication with the gas outlet (4) .
• Figure 2 shows the reactor of Figure 1 with a modified primary cyclone (18) provided with a lower tubular part (19) .
• the lower tubular part (19) is provided with a closed lower end (20) .
• an open-ended vertical catalyst withdrawal conduit (21) extends from a position (22) below the closed lower end (20) into the tubular part (19) up to a position (23) below the inlet (6) for receiving gas and catalyst.
• Said conduit (21) has a smaller cross-sectional area than the tubular part (19) , thereby defining an annular space (24) between conduit (21) and inner wall of the tubular part (19) .
• In the lower end of this annular space (24) means (25) to add a stripping medium are present.
• the gas ring (25) receives . stripping medium via conduit (26) .
• the catalyst withdrawal conduit (21) is further provided with a plurality of vertical slots (27) and an opening (28) at its upper position (23) .
• a vortex finder consisting of a vortex stabiliser plate (29) and a vortex stabiliser finder rod (30) .
• Figure 3 shows the reactor of Figure 2 except that the primary cyclone (31) is provided with an elevated roof (32) and a gas outlet conduit (33), which protrudes the roof to a position above the inlet (6) for receiving gas and catalyst.
• Vertical cyclones as in Figure 3 have shown to achieve high separation efficiency.
• Such cyclones are characterised in that they have an elevated roof (32) with respect to the position of the inlet (6) for receiving gas and catalyst. More preferably the elevated roof (32) is arranged at a vertical distance (dl) above the centre (34) of the tangentially arranged inlet (6) opening and wherein the ratio of this distance (dl) and the diameter (d2) of the upper tubular part (8) of the cyclone is between 0.2 and 3 and most preferably between 0.5 and 2.
• the gas outlet conduit (33) may protrude the elevated roof (32) from above, wherein the protrusion may range from no protrusion to about the vertical level of the inlet (6) for receiving gas and catalyst.
• FIG. 4 is an example of how such an embodiment.
• Figure 4 shows an external reactor riser (35) in fluid communication via tangential inlet (36) to the cyclone according to the present invention (37) .
• This cyclone (37) is provided with a gas outlet (38) and a lower tubular part (39) .
• a catalyst withdrawal conduit (40) is positioned having an open upper end (41) and a row of rectangular openings (42) .
• annular space (45) is present between the wall (43) of lower tubular part (39) and the upper part (44) of the catalyst withdrawal conduit (40) is present.
• a gas ring (46) is present for introducing steam, which keeps per-stripping zone (47) in a fluidised state.
• a vortex finder (48) is placed above conduit (40).
• the catalyst discharge conduit (40) has a downstream end, which terminates in a main stripping zone (49) consisting off a fluidised bed (50) contained in a stripping vessel (51) .
• a plate (52) is present to avoid fluidization gas from easily entering the conduit (40) .
• Stripping vessel (51) is further provided with means (52) , for example a gas ring, to supply stripping gas, a catalyst discharge conduit (53) through which catalyst is discharged to the regenerator (not shown) and a gas outlet conduit (54) .
• means (52) for example a gas ring
• catalyst discharge conduit (53) through which catalyst is discharged to the regenerator (not shown)
• gas outlet conduit (54) Through gas outlet conduit (54) stripping gas and stripped hydrocarbons leave the stripping vessel (51) .
• This conduit (54) may be in fluid communication with the gas outlet (38) of the cyclone separator (37) or with the downstream end of reactor riser (35) .
• the gas outlet (38) is fluidly connected to one or more secondary cyclones (55) (of which only one is shown) .
• the dipleg (56) of the secondary cyclone (55) is in fluid communication with stripping vessel (51) .
• Figure 5 shows the tubular part (57) of the cyclone separator according to the invention. Also shown is the upper part of the particle withdrawal conduit (58) provided with an open upper end (59) .
• Two connecting conduits (60) are shown for withdrawal of solid particles from fluidised bed (61) .
• the open-ended conduits (60) are positioned such that the particle inlet (66) is positioned below the main means, for example steam ring (62), for adding the primary fluidised medium.
• the conduits (60) are further provided an outlet (67), which outlet fluidly connects conduit (60) with particle withdrawal conduit (58) .
• Conduit (60) is further provided with a conduit (63) for adding a secondary fluidizing medium.
• the flow of the secondary fluidizing medium to conduit (63) can be controlled independently of the flow to steam ring (62) .
• the bed level (64) of fluidised bed (61) can be measured with pressure measurement points (65).
• a solids withdrawal means for withdrawing solids from a fluidised bed through a solids withdrawal conduit as above, wherein below the means to add primary fluidizing medium separate means are present to add a secondary fluidizing medium, in order to control the flow of solids through openings present in the solids withdrawal conduit, can find application in any fluidised bed and more preferably any fluidised bed comprising FCC catalyst particles.
• the embodiment of Figure 5 is an example of such a particle withdrawal means.
• the invention is therefore also directed to a solids withdrawal means suited to withdraw solid particles in a controlled manner from a fluidised bed of said solid particles.
• the solids withdrawal means comprises a substantially vertical withdrawal conduit with an open upper end protruding the fluidised bed from below.
• the withdrawal conduit is provided with one or more substantially horizontal conduits fluidly connecting the fluidised bed and the particle withdrawal conduit, wherein said substantially horizontal conduit is provided with means to add a secondary fluidizing medium.
• This substantially horizontal conduit is positioned below the position of the main means to add the primary fluidizing medium to the fluidised bed.
• the above fluid catalytic cracking units comprising the cyclone according to the present invention can be suitably employed to catalytically crack a hydrocarbon feedstock boiling above 370 °C to fuels boiling below 370 °C.
• Catalysts and operating conditions as well as suitable feedstocks and preferred products may be as, for example, described in General Textbook Fluid Catalytic Cracking, Technology and Operation, Joseph W. Wilson, PennWell Publishing Company, 1997.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Cyclones (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Catalysts (AREA)
• Signal Processing For Digital Recording And Reproducing (AREA)
• Memory System Of A Hierarchy Structure (AREA)
• Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)

Applications Claiming Priority (3)

Publications (1)

Family

ID=23093889

Family Applications (2)

Family Applications Before (1)

Country Status (10)

Families Citing this family (6)

Family Cites Families (5)

• 2002
  • 2002-04-11 EP EP02730157A patent/EP1379607B1/en not_active Expired - Lifetime
  • 2002-04-11 CA CA002444613A patent/CA2444613A1/en not_active Abandoned
  • 2002-04-11 AU AU2002310844A patent/AU2002310844B2/en not_active Ceased
  • 2002-04-11 RU RU2003133727/15A patent/RU2298577C2/ru not_active IP Right Cessation
  • 2002-04-11 EP EP02735255A patent/EP1379608A2/en not_active Withdrawn
  • 2002-04-11 WO PCT/EP2002/004144 patent/WO2002085527A2/en active Application Filing
  • 2002-04-11 MX MXPA03009473A patent/MXPA03009473A/es active IP Right Grant
  • 2002-04-11 BR BR0208964-5A patent/BR0208964A/pt not_active IP Right Cessation
  • 2002-04-11 WO PCT/EP2002/004142 patent/WO2002086019A2/en active Application Filing
  • 2002-04-11 AU AU2002302533A patent/AU2002302533B2/en not_active Ceased
  • 2002-04-11 MX MXPA03009472A patent/MXPA03009472A/es active IP Right Grant
  • 2002-04-11 DE DE60231800T patent/DE60231800D1/de not_active Expired - Fee Related
  • 2002-04-11 RU RU2003133729/15A patent/RU2294954C2/ru not_active IP Right Cessation
  • 2002-04-11 CA CA002444620A patent/CA2444620A1/en not_active Abandoned
  • 2002-04-11 BR BR0208963-7A patent/BR0208963A/pt not_active IP Right Cessation
  • 2002-04-11 AT AT02730157T patent/ATE427346T1/de not_active IP Right Cessation
  • 2002-04-11 JP JP2002583096A patent/JP2004534112A/ja not_active Ceased
  • 2002-04-11 JP JP2002583537A patent/JP2004533505A/ja not_active Ceased

Non-Patent Citations (1)

Also Published As

Similar Documents

Legal Events