Patent Grant
8152998
1. Field of the Disclosure
This disclosure relates to an apparatus and method for filtering liquids containing suspended solids. Specifically, this disclosure relates to an improved vertical filtration unit.
2. Description of Related Art
The removal of suspended solids from liquids, especially water, has been a longstanding requirement for many uses of such liquids. For example, water, which is free of suspended solids, is greatly preferred for uses, such as drinking, industrial processing, and swimming pools. Vertical filters, which utilize filter media, such as sand and garnet, have been used to separate suspended solids from water.
Vertical filters operate by introducing the liquid containing suspended solids onto the top portion of a bed of filter media. As the liquid passes through the filter media under the force of gravity, the suspended solids adhere to the filter media and/or to solids accumulated on the filer media, allowing liquid essentially free of suspended solids to flow through one or more screen cartridges prior to accumulating in an effluent chamber and then exit from the filtration unit.
The above-described method, although effective at removing suspended solids from liquids, has several shortcomings. The filter media eventually becomes saturated with suspended solids and no longer effectively removes suspended solids from the incoming liquid. When this condition occurs, the vertical filtration unit must cease operation so that the captured suspended solids can be removed from the filter media. This removal is accomplished through an operation referred to as “backwashing,” in which clean liquid is introduced, under pressure, to the bottom of the filter media bed and passes through the filter media in the reverse direction from the filtration process. The reverse flow of the liquid removes the filtered solids from the filter media and exits the vertical filter. This operation is typically continued until the exiting backwash water is essentially free of suspended solids, indicating that the filter media is clean. Backwashing can be very time consuming and generates large volumes of wastewater. Additionally, filtered solids are never completely removed from the filter media during backwashing, which eventually results in the filter media needing to be replaced. Filtration devices utilizing the above method are disclosed in U.S. Pat. No. 650,611.
The problem of backwashing filter media has been addressed, to some extent, through the development of continuous or moving bed filtration systems. While these continuous filtration systems operate to remove suspended solids as outlined above, they have the added benefit of continuously removing filtered suspended solids from the filter media. Examples of continuous filtration systems and various improvements thereon are disclosed and explained in U.S. Pat. Nos. 4,060,484; 4,891,142; 5,582,722; 5,730,886; 6,319,413; 6,517,712; 6,641,737; 6,790,351 all of which are herein incorporated by reference. See also the following articles: “Deep Moving Bed Downflow Sand Filter—An Optimum Granular Media Filter for Wastewater Treatment” American Filtration Society, Volume 10, 1996; and “The Application of Dual Media Concept to Upflow Filtration”, Water Treatment, Volume 4, No. 2, April 1989.
The above-described continuous systems for the filtration of liquids and the removal of suspended solid granules are typically not as effective or efficient as industry desires. One problem that remains is the corrosion of metallic screens in the screen cartridges, for example when brines are processed in a vertical granular media filter such as described above. While various plastic screens have tried, they have met with limited success, primarily due to insufficient strength of plastic screens, and the added cost of engineering special screens for specific applications. Therefore, there remains an unmet need to provide reliable, maintenance-free, continuous, self-cleaning, vertical filtration units for the removal of suspended solids from liquids that may be corrosive to metallic components, such as metallic screens in screen cartridges.
In one aspect, the present disclosure comprises a continuous, self-cleaning liquid filtering apparatus comprising:
In certain embodiments the granular filtration material moves downward, and the apparatus of this disclosure may be characterized as screenless downflow moving bed filters. In certain apparatus the liquid filtering apparatus the filtration material is stratified so that the unfiltered liquid first contacts coarse grained (larger average granule size) filtration material and then finer grained (smaller average granule size) filtration material, and then the finest grained filtration material. In certain apparatus, the finest filtration material is selected from the group consisting of sand, anthracite, ceramic beads and granular activated carbon, and the finer grained filtration material is one or more species of garnet. In yet other apparatus, the species of garnet may be selected from the group consisting of minerals within the general formula:
X3Y2(SiO4)3
In certain embodiments, the stratification of granular filter media is such that the finer grained filtration material is positioned between the coarse grained filtration material and outside surfaces of the vertically spaced apart upper and lower inverted cones. The coarse grained filtration material comprises sand of gradually diminishing granule size, starting from coarsest sand at an initial fluid contact layer having granule size not less than 0.5 mm, the sand grains progressively becoming smaller to a granule size of not less than 0.3 mm and not more than 3.0 mm. The finer grained filtration material may comprise one or more species of garnet of gradually diminishing granule size, starting from coarsest garnet having granule size not less than 0.15 mm, the garnet grains progressively becoming smaller to a granule size of not less than 0.1 mm and not more than 1.0 mm.
In certain embodiments, the deflector is connected to the inner surface of the vessel and slanted or inclined downward from a position near the inner surface of the vessel and extending toward but not touching the lower periphery of the lower inverted cone. In yet other embodiments, the deflector is connected to the lower periphery of the lower inverted cone and slanted or inclined upward from a position near the inner surface of the vessel and extending toward but not touching the inner surface of the vessel. The deflector may have a deflector angle “α” ranging from about 45 to about 55 degrees, or from about 48 to about 54 degrees, or from about 50 to about 54 degrees, and in certain embodiments about 52 degrees (as measured in reference to horizontal, as illustrated herein). In embodiments where the deflector is connected to the inner surface of the vessel and slanted downward from a position near the inner surface of the vessel and extending toward but not touching the lower periphery of the lower inverted cone, an upper terminus of the deflector may be positioned a distance “g1” about 0.5 to about 2 inches away from the inside surface of the vessel, or from about 1 to about 2 inches, or from about 1 to about 1.5 inches away from the inside surface of the vessel. In these embodiments, a lower terminus of the deflector may be positioned horizontally away from the peripheral edge of the lower inverted cone by a distance “g2” ranging from about 0.5 to about 1.5 inches, or from about 0.8 to about 1.2 inches. Also, the lower terminus of the deflector may be separated from the plane of the lower inverted cone by a distance “g3” ranging from about 2 to about 3 inches, or from about 2.3 to about 2.6 inches. The distances g1, g2, and g3 are carefully selected to ensure the stratification of the filter material. The slanted or inclined deflector is primarily positioned in a region or regions of the filter vessel where the coarser granular filtration media is downwardly moving, which are generally near the inside vessel surface.
In certain embodiments, the upper and lower inverted cones may have their peripheral edges positioned away from the inside surface of the vessel distances defines by “d” and “d2”, respectively, the upper inverted cone peripheral edge located closer to the inside surface of the vessel than is the peripheral edge of the lower inverted cone, so that the ratio d/d2 ranges from about 0.6 to about 0.95, or from about 0.7 to about 0.9, or from about 0.8 to about 0.9. In certain embodiments the upper inverted cone may have a cone angle “β” (relative to vertical) ranging from about 35 to about 45 degrees, or from about 36 to about 40 degrees. In certain embodiments the lower inverted cone may have a cone angle “γ” (relative to vertical) ranging from about 25 to about 35 degrees, or from about 28 to about 32 degrees. It is important that β>γ to ensure proper stratification of the filter material, in conjunction with the various distances and gaps referred to herein.
In certain embodiments the washbox comprises a filter media shield hood attached to an upper portion of the washbox, above the expulsion end of the airlifting tube, a washbox skirt below the filter media shield hood, a washbox isolator at the bottom of the washbox skirt, and at least one inlet tube at a bottom portion of the washbox skirt. The washbox may further comprise a target plate below the filter media shield hood and above the washbox skirt. The filter media shield hood may be an airlift return cap. The washbox may further comprise a porous separation cone below the filter media shield, a dirtied liquid reject collection tray below the separation cone, and a second reject outlet pipe communicating the dirtied liquid reject collection tray with the reject box. The reject outlet pipe may include at least one valve, and the effluent collector may include at least one valve. The latter valve may be a telescoping valve.
In certain embodiments the reject box comprises a weir volume space defined by a bottom side, a riser side and a weir plate, an outlet side comprising an outlet, and a vertical pipe communicating with the weir volume space by way of a riser outlet. The height of the weir plate may be adjusted to vary the volume of the weir volume space, and the weir plate may comprise a V-shaped notch along a top side of the weir plate.
In certain embodiments, the effluent collector is positioned above the upper inverted cone, and the airlifting tube is disposed in a generally centered position within the central pipe by way of one or more internal guide vanes.
In certain embodiments, the vessel is an existing basin with no installed piping, and the liquid filtering apparatus is retrofitted to the existing basin, and no holes are cored into the existing basin.
In certain embodiments, the depth of the filtration material above the upper inverted cone is at least 40 inches (102 cm).
In certain embodiments, the apparatus further comprises a sand cone attached to the central pipe below the lower inverted cone and terminating above the intake end of the airlifting tube, the sand cone having a sand cone space defined by a bottom of the filter vessel, an inner surface of the sand cone, a sand cone bottom plate, and the outer surface of the central pipe. In certain apparatus, the sand cone has an outer peripheral edge that is positioned a distance d1 from the inside surface of the vessel, where d1 ranges from about 1 to about 3 inches, or from about 1.5 to about 3 inches, or from about 2 to about 3 inches, and in certain embodiments about 2.5 inches. In certain embodiments the sand cone may have a cone angle “ρ” (relative to vertical) ranging from about 35 to about 45 degrees, or from about 36 to about 40 degrees.
In certain embodiments, the liquid filtering apparatus further comprises silt tubes connecting a bottom portion of the lower inverted cone and the sand cone space. In certain embodiments, the liquid filtering apparatus comprises a sand cone flush tube extending from the sand cone space to an area above the effluent collector. In certain embodiments, the liquid filtering apparatus comprises a back flush pipe extending from the effluent collector at a point between the effluent chamber and the valve to a point above the washbox skirt. The effluent collector may be connected to an effluent header. The apparatus may comprise a pipe extending from the outlet of the reject box to a reject manifold.
Methods of filtering liquid are also presented in this disclosure. One method includes the steps of:
Liquid filter assemblies are also considered a part of this disclosure, wherein two or more of the liquid filtering apparatus described above are included. Apparatus and methods of this disclosure will become more apparent upon review of the brief description of the drawings, the detailed description of the disclosure, and the claims that follow.
The manner in which the objectives of this disclosure and other desirable characteristics can be obtained is explained in the following detailed description and drawings included herein in which:
It is to be noted, however, that the appended drawings are not to scale and illustrate only typical embodiments of this disclosure, and are therefore not to be considered limiting of its scope, for other equally effective embodiments may become apparent after reading this disclosure.
In the following description and accompanying drawings, like reference numbers, as used in the various figures, refer to like features or elements. Terms, such as upper, lower, inner, and outer, refer to the orientation of a given element as shown in the drawings.
Various numerical ranges are disclosed herein. Because these ranges are continuous, they include every value between the minimum and maximum values. Unless expressly indicated otherwise, the various numerical ranges specified in this application are approximations.
The novel screenless continuous cleaning granular media filters and methods described herein employ, in certain embodiments, two filter media: a coarse granular media and a fine granular media, for example sand as the coarse granular media and garnet as the fine granular media. In these embodiments, the garnet grain employed is much smaller than the sand grains in the filter bed. The mixed media will be stratified in the filter bed based on filter media grain size, with the larger grains being generally located near the outside of the bed (near the vessel wall), and the finer grains being located closer to the central region of the bed. The filtration apparatus comprises a baffle system that enhances this stratification, and the filtration methods are generally force the influent, dirty fluids to flow through coarse sand first, followed by fine sand, and then to finest garnet. The finest garnet is located in filter polishing zone. This ensures the filter will produce excellent quality filter effluent. Another key feature is the absence of effluent screens. This feature eliminates the potential of screen fouling, and may reduce the overall capital and/or operating cost of the filters described herein.
Referring now to the drawing figures,
The upper conical configuration 54 of filter media bed 3 occurs naturally from the operation of filtration apparatus embodiments described herein. As the filter media drops from washbox 18 onto the top of conical pile 54, the granules classify themselves. The larger filter media granules tend to roll down the slope of the cone. The smaller granules, however, tend to descend vertically through the interior of the cone portion. This action results in the preferred, natural conical configuration of the pile.
Embodiment 100 further includes an effluent riser pipe or conduit 56, a central effluent riser pipe or conduit 58, and an airlifting tube 60. Operation of these features is known in the art as well, and reference is made to assignee's previously incorporated by reference U.S. Pat. No. 6,790,351. Embodiment 100 includes a baffle assembly 62 that includes an upper inverted cone 63 and a lower inverted cone 65. Upper inverted cone 63 is supported by supports 64, while lower inverted cone 65 is supported by supports 66. Also included is a sand cone 67 and compressed air inlet 68, as well as a target plate 70. As filtration material grains and the dirt and floc adhered thereto travel up airlifting tube 60 they strike target plate 70, helping to loosen the dirt from the grains of filtration material. Influent jets 72 may be employed to effect a countercurrent flow of clean influent fluid against the falling dirty grains, further cleansing the grains before they drop down on the conical top surface 54 of filter bed 3.
As illustrated generally in
In certain embodiments, and as illustrated in embodiment 100 of
The filtration process begins with the entry of the unfiltered liquid into vessel 2 through influent liquid connection 4. The unfiltered liquid descends, due to gravity, through the conical filter media bed 3, toward the bottom of the filter. The unfiltered liquid may be any liquid but will typically be water or wastewater. The liquid intake connection 4 is located in a sidewall of vessel 2 at a point above media bed 3, but not so high as to be above the liquid level, which would cause splashing and air entrainment. Liquid intake connection 4 may be positioned horizontally and tangent to the tank wall to impart a circular motion to the unfiltered liquid. This avoids stagnant zones and keeps floating material from sticking to inside surfaces of vessel 2.
The unfiltered liquid tends to flow through the coarser outer layer rather than through the finer inner layer. Liquids typically follow the path of least resistance. The path of least resistance in this case is through the coarse granule size filter media because the space between granules is large compared to the finer filter media. Thus, the initial filtration of unfiltered liquid is accomplished by the coarse granule size filter media.
The partially filtered liquid is further filtered as it next flows through the interior layer of finer granule size filter media. Contrary to previously known filter apparatus of this type, the liquid then flows directly to effluent chamber 44 through risers 56, 58, and conduits 40, 42 and to effluent collector 44, which collects the filtered liquid. There are no screens or screen cartridges in the filters according to the present disclosure.
In the presently disclosed filter apparatus, central pipe 58 extends along an outside surface of airlifting tube 60 from a position just below the washbox 18 to a position just above the intake end of airlifting tube 60. An effluent riser pipe 56 extends along an outside surface of central pipe 58 from a position just below washbox 18 to a position above its intake end.
The filtered effluent liquid leaves the filtration unit through effluent collector 44 to external exit riser pipe 38. An effluent valve can be used to control or stop the flow of liquid through effluent box 36. The exit riser pipe 38 discharges to an area external from the filter unit. The rate of flow through effluent collector 44 may be controlled by a telescoping valve on exit riser pipe 38, as is taught is assignee's previous U.S. Pat. No. 6,790,351. Any suitable telescoping valve may be used. Suitable telescoping valves include, but are not limited to, those disclosed in U.S. Pat. No. 6,364,179 to Sullivan and U.S. Pat. No. 6,035,892 to Kennedy, both of which are herein incorporated by reference.
The solids captured by the filter media bed 3 are drawn downward with the downflow moving filter media bed 3 into an intake end area 68 of airlift tube 60. The continuous transport of dirtied filter media from the bottom of the filter to washbox 18 is carried out by airlifting tube 60. The performance of the filter unit depends, in great part, on the performance of the airlift. Airlifts themselves are well known in the fields of wastewater treatment and well hydraulics. A conventional airlift pump consists essentially of a vertical tube having its lower end submerged in a liquid or slurry to be pumped. The upper end of the tube discharges the pump material. In the case of the present disclosure, the upwardly transported mixture of dirtied filter media and filtered liquid empties into the washbox 18. The height to which the mixture can be airlifted depends on the efficiency of the airlift system.
The actual pumping or lifting action is achieved by the introduction of air into the lower part of the airlifting tube 68 which also contains a mixture of filtered liquid and dirtied filter media. Any suitable airlifting means may be used in the airlifting tube 60 of the present disclosure. Suitable airlift means include, but are not limited to, those disclosed in U.S. Pat. No. 6,319,413 to Xia et al., U.S. Pat. No. 5,730,886 to Wachinski et al., and U.S. Pat. No. 5,582,722 to Wachinski et al., all of which are herein incorporated by reference. Intake end 68 may have a bell-shaped bottom 69 to increase the pumping rate of the airlift. Thus, more filtered water, filter media, and dirt can be pumped to the top of the filtration unit without increasing the air supply requirement.
Any suitable washbox design may be used in filter apparatus of the present disclosure. One useful embodiment, described with reference to FIG. 3 of the '351 patent, is a one-stage washbox. The higher density filter media settles into the washbox skirt area 76. In this area, the unfiltered liquid flows up from the bottom of the washbox skirt 76 via inlet tubes 72.
In an alternative embodiment, washbox 18 may be a two-stage cleaning washbox apparatus as depicted in FIG. 2 of the '351 patent. The two-stage cleaning washbox includes a filter media shield hood which deflects the filtered liquid and dirtied filter media downwardly onto a separation cone. This downward deflection efficiently washes dirt granules and solids from the filter media, along with the filtered liquid. The solids concentrated liquid from the airlift drops on an inclined porous surface of the separation cone and passes through the surface of separation cone into a dirtied liquid reject collecting tray. The dewatered, partially cleaned, filter media moves down along the surface of the separation cone and falls into a washbox filter media liquid separation area and eventually into the washbox skirt and is washed clean of filtered granules as described in the above-mentioned one-stage washbox by unfiltered liquid, now wash liquid, entering into washbox skirt.
In other embodiments of the present disclosure, the present liquid filtering apparatus may be used for “in-ground” installations, typically in new or existing concrete basins. This embodiment avoids the difficulty of piping the effluent out of the basin at a low level. This embodiment avoids designs that require the effluent to be removed via a pipe that exits through a side wall of the vessel. Such a design is particularly inconvenient in a poured concrete tank, especially if the concrete is an existing installation being converted to a vertical downflow moving bed sand filter. As illustrated in embodiment 300 of
The specifics of operating reject box 26 is fully discussed in assignee's '351 patent and only summarized here. The wash liquid discharges out of washbox housing via reject outlet pipe 30 to a reject box 26. A valve 32 on reject outlet pipe 30 may be used to adjust the flow rate of the wash liquid into reject box 26. This may be used to conserve washing liquid that will have to be recycled through the filter plant. Reject outlet pipe 30 fluidly connects with a reject line inlet (not illustrated), which allows wash liquid to enter reject box 26. Reject box 26 has a weir volume space defined by a bottom, a riser side, and a weir plate. Reject box 26 also includes an outlet side. The height of weir plate may be adjusted to vary the volume of weir volume space. The weir plate may include a V-shaped notch along a top side, acting to regulate and gauge the flow of wash liquid out of the weir volume space. The flow of wash liquid is the reject flow rate. Once wash liquid passes over the weir plate it exits reject box 26 by way of outlet conduit 28 and is carried away.
Liquid, typically water or waste water, may be filtered using the present liquid filtering apparatus. In order to filter liquid, a bed of filtration material, usually sand, comprising granules of different sizes, including large granules and fine granules, is provided within a vessel. The bed typically has a general conical configuration. An unfiltered liquid, typically water or wastewater, is introduced above the bed and is filtered through the bed in a generally downward direction. The filtered liquid passes into an effluent chamber, as described above without the use of cartridge screens, to form a collection of filtered liquid. The collection of filtered liquid is removed from the effluent chamber by way of an effluent collector, the flow through which is controlled by a ball valve or telescoping valve as discussed above.
More specifically, the novel filter apparatus works as follows, using sand and garnet as an example only, it being realized and understood that other combinations of coarse and fine-grained granules may be employed equally as well:
The present disclosure has been described with reference to certain embodiments. Obvious modifications and alterations will occur to others upon reading and understanding the preceding detailed description. It is intended that the disclosure be construed as including all such modifications and alterations insofar as they come within the scope of appended claims or the equivalents thereof.
| Number | Name | Date | Kind |
|---|---|---|---|
| 329185 | Matthiessen | Oct 1885 | A |
| 335586 | Howes | Feb 1886 | A |
| 395070 | Moore | Dec 1888 | A |
| 579039 | Brashear | Mar 1897 | A |
| 650611 | Reeves | May 1900 | A |
| 800113 | Kassian | Sep 1905 | A |
| 1007929 | Deacon et al. | Nov 1911 | A |
| 1099396 | Rothwell | Jun 1914 | A |
| 1130382 | Deacon et al. | Mar 1915 | A |
| 1179658 | Rothwell | Apr 1916 | A |
| 1565233 | Berntsen | Dec 1925 | A |
| 1608661 | Nordell | Nov 1926 | A |
| 1861295 | Bramwell | May 1932 | A |
| 1903612 | Dotterweich | Apr 1933 | A |
| 2057887 | Elliott et al. | Oct 1936 | A |
| 2073388 | Elliott et al. | Mar 1937 | A |
| 2348854 | Schrelber | May 1944 | A |
| 2355564 | Sebald | Aug 1944 | A |
| 2468838 | Rey | May 1949 | A |
| 2590148 | Berg | Mar 1952 | A |
| 2683109 | Norris | Jul 1954 | A |
| 2735803 | Leffer | Feb 1956 | A |
| 2742381 | Donald et al. | Apr 1956 | A |
| 2768221 | Findlay | Oct 1956 | A |
| 2863829 | Henke et al. | Dec 1958 | A |
| 3003641 | Laughlin | Oct 1961 | A |
| 3019079 | Donohue | Jan 1962 | A |
| 3150063 | Comte | Sep 1964 | A |
| 3480542 | Wilhelm et al. | Nov 1969 | A |
| 3537582 | Laszlo | Nov 1970 | A |
| 3550774 | Gene et al. | Dec 1970 | A |
| 3556299 | Zievers et al. | Jan 1971 | A |
| 3563385 | Bykov | Feb 1971 | A |
| 3594991 | Berz et al. | Jul 1971 | A |
| 3598235 | Demeter | Aug 1971 | A |
| 3667604 | Lagoutte | Jun 1972 | A |
| 3679581 | Kunz | Jul 1972 | A |
| 3767048 | Prengemann | Oct 1973 | A |
| 3798159 | Kisbocskoi et al. | Mar 1974 | A |
| 3814247 | Hirs | Jun 1974 | A |
| 3853752 | Tymoszczuk | Dec 1974 | A |
| 3855120 | Garbo | Dec 1974 | A |
| 3878096 | Somogyi | Apr 1975 | A |
| 3929640 | Dohnert | Dec 1975 | A |
| 3953333 | Hirs | Apr 1976 | A |
| 3968034 | Tymoszczuk | Jul 1976 | A |
| 3987148 | Squires | Oct 1976 | A |
| 3998739 | Morimoto et al. | Dec 1976 | A |
| 4000066 | Squires | Dec 1976 | A |
| 4005016 | Haese et al. | Jan 1977 | A |
| 4008159 | Besik | Feb 1977 | A |
| 4052300 | Mosso | Oct 1977 | A |
| 4060484 | Austin et al. | Nov 1977 | A |
| 4126546 | Hjelmner et al. | Nov 1978 | A |
| 4133759 | Ikeda et al. | Jan 1979 | A |
| 4140497 | Zenz | Feb 1979 | A |
| 4197201 | Hjelmner et al. | Apr 1980 | A |
| 4197205 | Hirs | Apr 1980 | A |
| 4202770 | Gappa et al. | May 1980 | A |
| 4238335 | Grimsley | Dec 1980 | A |
| 4240910 | Stratmann et al. | Dec 1980 | A |
| 4240911 | Demeter et al. | Dec 1980 | A |
| 4246102 | Hjelmner et al. | Jan 1981 | A |
| 4246119 | Alldredge | Jan 1981 | A |
| 4265767 | Gappa et al. | May 1981 | A |
| 4276178 | Gappa et al. | Jun 1981 | A |
| 4330401 | Boze et al. | May 1982 | A |
| 4340485 | Ikeda et al. | Jul 1982 | A |
| 4374029 | Jaisinghani | Feb 1983 | A |
| 4399034 | Moller | Aug 1983 | A |
| 4441998 | Ueda | Apr 1984 | A |
| 4482457 | Jacquet | Nov 1984 | A |
| 4482458 | Rovel et al. | Nov 1984 | A |
| 4496464 | Hensley | Jan 1985 | A |
| 4592837 | Ludwig et al. | Jun 1986 | A |
| 4626359 | Bennett et al. | Dec 1986 | A |
| 4692248 | Stannard et al. | Sep 1987 | A |
| 4707252 | Durot et al. | Nov 1987 | A |
| 4720347 | Berne | Jan 1988 | A |
| 4787987 | Hensley | Nov 1988 | A |
| 4826609 | Hensley | May 1989 | A |
| 4842744 | Schade | Jun 1989 | A |
| 4851122 | Stanley | Jul 1989 | A |
| 4861472 | Weis | Aug 1989 | A |
| 4869815 | Bernard et al. | Sep 1989 | A |
| 4871459 | Titoff | Oct 1989 | A |
| 4891142 | Hering, Jr. | Jan 1990 | A |
| 4900434 | Schade | Feb 1990 | A |
| 4931183 | Klein et al. | Jun 1990 | A |
| 4966698 | Hensley | Oct 1990 | A |
| 5019278 | Jacquet | May 1991 | A |
| 5032276 | Mackrle et al. | Jul 1991 | A |
| 5112504 | Johnson | May 1992 | A |
| 5154824 | Anderson | Oct 1992 | A |
| 5171443 | Bratten | Dec 1992 | A |
| 5173194 | Hering, Jr. | Dec 1992 | A |
| 5198105 | Kauling et al. | Mar 1993 | A |
| 5207905 | O'Brien et al. | May 1993 | A |
| 5217609 | Holdeman | Jun 1993 | A |
| 5252230 | Dunkers | Oct 1993 | A |
| 5277829 | Ward | Jan 1994 | A |
| 5350505 | Tang | Sep 1994 | A |
| 5372712 | Petit | Dec 1994 | A |
| 5407574 | Hensley | Apr 1995 | A |
| 5433862 | Batson | Jul 1995 | A |
| 5441634 | Edwards | Aug 1995 | A |
| 5449453 | Tang | Sep 1995 | A |
| 5454959 | Stevens | Oct 1995 | A |
| 5458788 | Tang | Oct 1995 | A |
| 5462654 | Hering, Jr. | Oct 1995 | A |
| 5472610 | Jonsson | Dec 1995 | A |
| 5474585 | Geibel et al. | Dec 1995 | A |
| 5514284 | Uban et al. | May 1996 | A |
| 5520804 | Ward | May 1996 | A |
| 5543037 | Hering, Jr. | Aug 1996 | A |
| 5549827 | Batson | Aug 1996 | A |
| 5565098 | Vellinga | Oct 1996 | A |
| 5573663 | Junius et al. | Nov 1996 | A |
| 5573671 | Klein | Nov 1996 | A |
| 5582722 | Wachinski et al. | Dec 1996 | A |
| 5630936 | Oyzboyd | May 1997 | A |
| 5635080 | Hensley | Jun 1997 | A |
| 5653181 | Yang et al. | Aug 1997 | A |
| 5681472 | Jonsson et al. | Oct 1997 | A |
| 5695712 | Kumar et al. | Dec 1997 | A |
| 5698106 | Larsson et al. | Dec 1997 | A |
| 5707523 | Temple | Jan 1998 | A |
| 5730886 | Wachinski et al. | Mar 1998 | A |
| 5746913 | Chang et al. | May 1998 | A |
| 5755959 | Jonsson et al. | May 1998 | A |
| 5766488 | Uban et al. | Jun 1998 | A |
| 5843308 | Suozzo et al. | Dec 1998 | A |
| 5895567 | Van Der Herberg | Apr 1999 | A |
| 5945005 | Junius et al. | Aug 1999 | A |
| 5976365 | Petit | Nov 1999 | A |
| 5993650 | Kim | Nov 1999 | A |
| 6035892 | Kennedy | Mar 2000 | A |
| 6048459 | Khudenko | Apr 2000 | A |
| 6063720 | Kumar et al. | May 2000 | A |
| 6074549 | Cochrane et al. | Jun 2000 | A |
| 6077426 | Grabowski | Jun 2000 | A |
| 6077446 | Steiner et al. | Jun 2000 | A |
| 6103109 | Noyes et al. | Aug 2000 | A |
| 6143186 | Van Unen | Nov 2000 | A |
| 6159365 | Kigel et al. | Dec 2000 | A |
| 6171498 | Fassbender et al. | Jan 2001 | B1 |
| 6319396 | Heagey | Nov 2001 | B1 |
| 6319413 | Xia et al. | Nov 2001 | B1 |
| 6326191 | VanToever | Dec 2001 | B2 |
| 6328892 | Jones | Dec 2001 | B1 |
| 6334956 | Hanemaaijer | Jan 2002 | B1 |
| 6361701 | Schade | Mar 2002 | B1 |
| 6364179 | Sullivan | Apr 2002 | B1 |
| 6365044 | Crane | Apr 2002 | B1 |
| 6387283 | Lind | May 2002 | B1 |
| 6413427 | Tipton et al. | Jul 2002 | B2 |
| 6426005 | Larsson | Jul 2002 | B1 |
| 6471857 | Kaibara | Oct 2002 | B1 |
| 6517712 | Xia et al. | Feb 2003 | B2 |
| 6527948 | Haridas et al. | Mar 2003 | B2 |
| 6531058 | Josse et al. | Mar 2003 | B1 |
| 6617155 | Van Toever | Sep 2003 | B1 |
| 6630071 | Buisman et al. | Oct 2003 | B1 |
| 6641737 | Xia et al. | Nov 2003 | B2 |
| 6716344 | Bassi et al. | Apr 2004 | B1 |
| 6733662 | Pollock | May 2004 | B2 |
| 6780312 | Saito | Aug 2004 | B2 |
| 6790351 | Xia et al. | Sep 2004 | B2 |
| 6874644 | Wagener et al. | Apr 2005 | B1 |
| 6881350 | Wilson | Apr 2005 | B2 |
| 6966987 | Morgan et al. | Nov 2005 | B1 |
| 7018530 | Pollock | Mar 2006 | B2 |
| 7147781 | Gordic | Dec 2006 | B2 |
| 7160452 | Saito | Jan 2007 | B2 |
| 7368059 | Drake | May 2008 | B2 |
| 7381336 | Stedman | Jun 2008 | B2 |
| 7399416 | Moller et al. | Jul 2008 | B2 |
| 7445721 | Moller | Nov 2008 | B2 |
| 7553418 | Khudenko et al. | Jun 2009 | B2 |
| 7666302 | Jenkins | Feb 2010 | B2 |
| 7713423 | Moller et al. | May 2010 | B2 |
| 7713426 | Newcombe | May 2010 | B2 |
| 7744764 | Moller et al. | Jun 2010 | B2 |
| 7862715 | Drake | Jan 2011 | B2 |
| 7897040 | Newcombe et al. | Mar 2011 | B2 |
| 7972509 | Newcombe et al. | Jul 2011 | B2 |
| 8012359 | Parkinson | Sep 2011 | B2 |
| 8070963 | Bomze | Dec 2011 | B2 |
| 8071055 | Newcombe | Dec 2011 | B2 |
| 20020023885 | Lind | Feb 2002 | A1 |
| 20020036164 | Xia et al. | Mar 2002 | A1 |
| 20020162795 | Pollock | Nov 2002 | A1 |
| 20030066792 | Xia et al. | Apr 2003 | A1 |
| 20040050762 | Xia et al. | Mar 2004 | A1 |
| 20040074836 | Long | Apr 2004 | A1 |
| 20040104183 | Wilson | Jun 2004 | A1 |
| 20040144728 | Moller et al. | Jul 2004 | A1 |
| 20050077247 | Stedman | Apr 2005 | A1 |
| 20050115880 | Pollock | Jun 2005 | A1 |
| 20050173348 | Drake | Aug 2005 | A1 |
| 20060000785 | Moller | Jan 2006 | A1 |
| 20060261010 | Drake | Nov 2006 | A1 |
| 20070187329 | Moller et al. | Aug 2007 | A1 |
| 20080099413 | Tolley et al. | May 2008 | A1 |
| 20080257807 | Parkinson | Oct 2008 | A1 |
| 20080277349 | Moller et al. | Nov 2008 | A1 |
| 20080302726 | Moller et al. | Dec 2008 | A1 |
| 20090071909 | Newcombe et al. | Mar 2009 | A1 |
| 20090101568 | Donaque et al. | Apr 2009 | A1 |
| 20090178980 | Newcombe | Jul 2009 | A1 |
| 20100133196 | Khudenko | Jun 2010 | A1 |
| 20110024369 | Reekers | Feb 2011 | A1 |
| 20110100888 | Newcombe et al. | May 2011 | A1 |
| 20110100925 | Newcombe et al. | May 2011 | A1 |
| 20110147321 | Oz | Jun 2011 | A1 |
| 20110240562 | Bomze | Oct 2011 | A1 |
| 20110290734 | Xia et al. | Dec 2011 | A1 |
| Number | Date | Country | |
|---|---|---|---|
| 20110290734 A1 | Dec 2011 | US |
