Submerged combustion melters having an extended treatment zone and methods of producing molten glass

Information

  • Patent Grant
  • 10392285
  • Patent Number
    10,392,285
  • Date Filed
    Tuesday, November 22, 2016
    8 years ago
  • Date Issued
    Tuesday, August 27, 2019
    5 years ago
Abstract
A submerged combustion melter includes a floor, a roof, and a sidewall structure connecting the floor and roof defining an internal space. A first portion of the internal space defines a melting zone, and a second portion defines a fining zone immediately downstream of the melting zone. One or more combustion burners in either the floor, roof, the sidewall structure, or any combination of these, are configured to emit the combustion gases from a position under a level of, and positioned to transfer heat to and produce, a turbulent molten mass of glass containing bubbles in the melting zone. The fining zone is devoid of combustion burners or other apparatus or components that would increase turbulence above that in the melting zone. The melter may include a treating zone that stabilizes or destabilizes bubbles and/or foam. Processes of using the melters are a feature of the disclosure.
Description
BACKGROUND INFORMATION

Technical Field


The present disclosure relates generally to the field of combustion furnaces and methods of use to produce glass, and more specifically to submerged combustion melters and methods for producing foamed glass, hollow or entrained-gas fiber, or non-foamed glass using the submerged combustion melters.


Background Art


A submerged combustion melter (SCM) may be employed to melt glass batch materials to produce molten glass by passing oxygen, oxygen-enriched mixtures, or air along with a liquid, gaseous fuel, or particulate fuel in the glass batch, directly into a molten pool of glass usually through burners submerged in a glass melt pool. The introduction of high flow rates of oxidant and fuel into the molten glass, and the expansion of the gases cause rapid melting of the glass batch and much turbulence, and possibly foaming.


Often it is a primary goal to melt batch or other feed materials in an SCM as quickly and with as small a footprint SCM as possible. Although this is still desired for the most part, one drawback to this strategy in known SCMs is the lack of, or total absence of melter footprint or size outside of the submerged combustion melting zone that might provide some time downstream of the melting zone for treatment of the turbulent, foamy molten glass before it enters downstream equipment. Furthermore, there typically is a lack of, or no melter footprint before the melting zone of an SCM. These failings may severely limit the flexibility of operation of an SCM.


Fining or removal of foam prior to downstream processing may be desired in some instances, while in other instances increased or changed foaming may be desired, for example, when producing hollow fiber or producing products including entrained bubbles. Reduced foaming may be desired in the first case, as the foam may stabilize in a top layer when the molten mass is routed through conventional conditioning and/or distribution channels/systems downstream of the SCM. The foam layer may impede the ability to apply heat to the glass using combustion burners to achieve or maintain temperature and compositional homogeneity of the molten glass, and may also impede the rate at which further bubbles in the melt rise and thus affect expulsion of the bubbles and mass flow rate of the melt in the channels. In extreme cases, the foam generated may interfere with the traditional energy application methods employed, which may cause systems to require shutdown, maintenance and may result in a process upset. Attempts to reduce the foam through process adjustments have not met with complete success in reducing foam to an acceptable amount. On the other hand, in cases where foaming may be desired, control of bubble size, composition, and the like may be hindered in smaller footprint SCMs.


It would be an advance in the glass manufacturing art if submerged combustion melters and processes of their use could address the above restrictions on flexibility of operation.


SUMMARY

In accordance with the present disclosure, submerged combustion melters and processes are described which reduce or overcome one or more of the above problems.


A first aspect of the disclosure is a submerged combustion melter comprising:


a floor, a roof, and a sidewall structure connecting the floor and roof defining an internal space, a first portion of the internal space comprising a melting zone, and a second portion of the internal space defining a fining zone immediately downstream of the melting zone;


one or more combustion burners in either the floor, the roof, the sidewall structure, or any two or more of these, producing combustion gases and configured to emit the combustion gases from a position under a level of, and positioned to transfer heat to and produce, a turbulent molten mass of glass containing bubbles in the melting zone;


the submerged combustion melter comprising a geometry whereby the level of the molten glass is substantially equivalent in the melting zone and the fining zone, and the fining zone is devoid of combustion burners or other apparatus or components that would increase turbulence above that in the melting zone.


A second aspect of the disclosure is a submerged combustion melter comprising:


a floor, a roof, and a sidewall structure connecting the floor and roof defining an internal space, a first portion of the space comprising a melting zone, and a second portion of the space comprising a fining zone immediately downstream of the melting zone, a third portion of the space comprising a treating zone downstream of the melting zone and upstream of the fining zone, and a fourth portion of the space comprising a feed zone upstream of the melting zone, wherein the feed zone, the treating zone, and the fining zone are all devoid of submerged combustion burners other apparatus to increase turbulence above that in the melting zone;


one or more combustion burners in either the floor, the roof, the sidewall structure, or any two or more of these, producing combustion gases and configured to emit the combustion gases from a position under a level of, and positioned to transfer heat to and produce, a turbulent molten mass of glass containing bubbles in the melting zone;


one or more non-burner apparatus configured to inject a composition into the molten glass in the treating zone; and


the submerged combustion melter comprising a geometry whereby the level of the molten glass is substantially equivalent in the feed zone, the melting zone, the treating zone, and the fining zone, and optionally comprising an exhaust stack positioned in the roof of the fining section.


A third aspect of the disclosure is a process comprising:


charging a feed composition into a submerged combustion melter comprising a geometry, at least a portion of the feed composition comprising a vitrifiable material;


heating the feed composition with one or more submerged combustion burners, thereby melting at least a portion of the vitrifiable material in a melting zone of the submerged combustion melter to form a turbulent molten mass of glass and bubbles in the melting zone;


allowing the turbulent molten mass of glass and bubbles to flow into a fining zone in the submerged combustion melter immediately downstream of the melting zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a fined molten mass of glass; and


maintaining a level of molten glass in the fining zone substantially equal to a level of the molten glass in the melting zone.


A fourth aspect of the disclosure is a process comprising:


charging a feed composition into a submerged combustion melter comprising a feed zone, at least a portion of the feed composition comprising a vitrifiable material;


heating the feed composition with one or more submerged combustion burners in a melting zone downstream of the feed zone, thereby melting at least a portion of the vitrifiable material in the melting zone of the submerged combustion melter to form a turbulent molten mass of glass and bubbles in the melting zone;


allowing the turbulent molten mass of glass and bubbles to flow from the melting zone into a treating zone in the submerged combustion melter immediately downstream of the melting zone, and feeding a treating composition into the molten glass in the treating zone, the treating zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a treated molten mass of glass;


allowing the treated molten mass of glass to flow from the treating zone into a fining zone in the submerged combustion melter immediately downstream of the treating zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a treated, fined molten mass of glass;


maintaining a level of molten glass in the feed zone, the treating zone, and the fining zone substantially equal to a level of the molten glass in the melting zone; and


exhausting the submerged combustion melter employing an exhaust stack positioned in the roof of the fining section.


Submerged combustion melters and processes 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.





BRIEF DESCRIPTION OF THE DRAWINGS

The manner in which the objectives of the disclosure and other desirable characteristics can be obtained is explained in the following description and attached drawings in which:



FIGS. 1-6 are schematic side elevation views, partially in cross-section with some portions cut away, of six system embodiments in accordance with this disclosure; and



FIGS. 7 and 8 are logic diagrams of two process embodiments of the present disclosure.





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 the disclosure may admit to other equally effective embodiments.


DETAILED DESCRIPTION

In the following description, numerous details are set forth to provide an understanding of the disclosed systems and methods. However, it will be understood by those skilled in the art that the systems and methods covered by the claims may be practiced without these details and that numerous variations or modifications from the specifically described embodiments may be possible and are deemed within the claims. All U.S. published patent applications and U.S. patents referenced herein are hereby explicitly incorporated herein by reference. In the event definitions of terms in the referenced patents and applications conflict with how those terms are defined in the present application, the definitions for those terms that are provided in the present application shall be deemed controlling.


As explained briefly in the Background, one drawback to present submerged combustion melters is the lack of, or total absence of melter footprint or size outside of the submerged combustion melting zone that might provide some time downstream of the melting zone for treatment of the turbulent, foamy molten glass before it enters downstream equipment. Furthermore, there typically is a lack of, or no melter footprint before the melting zone of an SCM. These failings may severely limit the flexibility of operation of an SCM. Removal of foam prior to downstream processing may be desired in some instances, while in other instances increased or changed foaming may be desired, for example, when producing hollow fiber or producing products including entrained bubbles.


Applicants have discovered certain SCMs and processes that may reduce or eliminate such shortcomings.


Various terms are used throughout this disclosure. “Submerged” as used herein means that combustion gases emanate from combustion burners under the level of the molten glass; the burners may be floor-mounted, wall-mounted, or in melter embodiments comprising more than one submerged combustion burner, any combination thereof (for example, two floor mounted burners and one wall mounted burner). “SC” as used herein means “submerged combustion” unless otherwise specifically noted, and “SCM” means submerged combustion melter unless otherwise specifically noted.


The term “fining” as used herein means stabilizing or destabilizing foam, as well as the traditional concept of fining which refers to the removal of few bubbles from within the molten glass. A “fining zone” of an SCM may involve simply holding a molten mass of glass for a time at a certain temperature, or may include time at temperature plus action of a treatment composition introduced in a treatment zone of an SCM prior to a fining zone. The term “treating” means contacting a molten mass of glass with one or more compositions, or mixtures of compositions, in a “treating zone” of an SCM. Treating compositions may be organic, inorganic, of combinations or mixtures thereof, and may be gaseous (bubbles), liquid, solid, or combination or mixture thereof. The term “composition” includes one or more gases, one or more liquids or solids that may evolve a gas or become gaseous under the high temperature conditions associated with submerged combustion melting, one or more particulate solids, and combinations of thereof. The term “treating” means the treating composition is not simply present in the head space above the molten glass and foamy layer floating on top thereof, but is present in such a manner so that the composition has a greater chance of interacting with the “SC” bubbles of the foam and/or changing the SC bubble atmosphere and/or the SC bubble film.


The terms “foam” and “foamy” include froths, spume, suds, heads, fluffs, fizzes, lathers, effervesces, layer and the like. The term “bubble” means a thin, shaped, gas-filled film of molten glass. The shape may be spherical, hemispherical, rectangular, polyhedral, ovoid, and the like. The gas or “bubble atmosphere” in the gas-filled SC bubbles may comprise oxygen or other oxidants, nitrogen, combustion products (including but not limited to, carbon dioxide, carbon monoxide, NORx, SOx, H2S, and water), reaction products of glass-forming ingredients (for example, but not limited to, sand (primarily SiO2), clay, limestone (primarily CaCO3), burnt dolomitic lime, borax and boric acid, and the like. Bubbles may include solids particles, for example soot particles, either in the film, the gas inside the film, or both.


As used herein the term “combustion gases” means substantially gaseous mixtures of combusted fuel, any excess oxidant, and combustion products, such as oxides of carbon (such as carbon monoxide, carbon dioxide), oxides of nitrogen, oxides of sulfur, and water. Combustion products may include liquids and solids, for example soot and unburned liquid fuels.


“Oxidant” as used herein includes air and gases having the same molar concentration of oxygen as air, oxygen-enriched air (air having oxygen concentration greater than 21 mole percent), and “pure” oxygen, such as industrial grade oxygen, food grade oxygen, and cryogenic oxygen. Oxygen-enriched air may have 50 mole percent or more oxygen, and in certain embodiments may be 90 mole percent or more oxygen.


The term “fuel”, according to this disclosure, means a combustible composition comprising a major portion of, for example, methane, natural gas, liquefied natural gas, propane, hydrogen, steam-reformed natural gas, atomized hydrocarbon oil, combustible powders and other flowable solids (for example coal powders, carbon black, soot, and the like), and the like. Fuels useful in the disclosure may comprise minor amounts of non-fuels therein, including oxidants, for purposes such as premixing the fuel with the oxidant, or atomizing liquid or particulate fuels. As used herein the term “fuel” includes gaseous fuels, liquid fuels, flowable solids, such as powdered carbon or particulate material, waste materials, slurries, and mixtures or other combinations thereof.


The sources of oxidant and fuel may be one or more conduits, pipelines, storage facility, cylinders, or, in embodiments where the oxidant is air, ambient air. Oxygen-enriched oxidants may be supplied from a pipeline, cylinder, storage facility, cryogenic air separation unit, membrane permeation separator, or adsorption unit such as a vacuum swing adsorption unit.


The term “flow channel” means a channel or conduit defined by a flow channel floor, a flow channel roof, and a flow channel wall structure connecting the floor and roof, and may have any operable cross-sectional shape (for example, but not limited to, rectangular, oval, circular, trapezoidal, hexagonal, and the like) and any flow path shape (for example, but not limited to, straight, zigzag, curved, and combinations thereof). In certain systems and processes the flow channel may be selected from the group consisting of a conditioning channel, a distribution channel, and a forehearth.


Conduits used in burners and devices for delivery of a treating composition useful in SCMs and processes of the present disclosure may be comprised of metal, ceramic, ceramic-lined metal, or combination thereof. Suitable metals include stainless steels, for example, but not limited to, 306 and 316 steel, as well as titanium alloys, aluminum alloys, and the like. Suitable materials for the glass-contact refractory, which may be present in SC melters and flow channels, and refractory burner blocks (if used), include fused zirconia (ZrO2), fused cast AZS (alumina-zirconia-silica), rebonded AZS, or fused cast alumina (Al2O3). The melter, flow channel, treating composition delivery device, and burner geometry, and type of glass to be produced may dictate the choice of a particular material, among other parameters.


The terms “cooled” and “coolant” may include use of any heat transfer fluid and may be any gaseous, liquid, or some combination of gaseous and liquid composition that functions or is capable of being modified to function as a heat transfer fluid. Gaseous heat transfer fluids may be selected from air, including ambient air and treated air (for example, air treated to remove moisture), inorganic gases, such as nitrogen, argon, and helium, organic gases such as fluoro-, chloro- and chlorofluorocarbons, including perfluorinated versions, such as tetrafluoromethane, and hexafluoroethane, and tetrafluoroethylene, and the like, and mixtures of inert gases with small portions of non-inert gases, such as hydrogen. Heat transfer liquids may be selected from liquids that may be organic, inorganic, or some combination thereof, for example, salt solutions, glycol solutions, oils and the like. Other possible heat transfer fluids include steam (if cooler than the expected glass melt temperature), carbon dioxide, or mixtures thereof with nitrogen. Heat transfer fluids may be compositions comprising both gas and liquid phases, such as the higher chlorofluorocarbons.


Certain burners and treating composition delivery devices useful in SCMs and processes of this disclosure may be fluid-cooled, and may include first and second (or more) concentric conduits. In the case of burners, the first conduit may be fluidly connected at one end to a source of fuel, the second conduit may be fluidly connected to a source of oxidant, and a third substantially concentric conduit may connect to a source of cooling fluid. Treating composition delivery devices may be, for example, and not limited to those disclosed in Applicant's U.S. Pat. No. 9,032,760.


Certain SCMs of this disclosure may comprise one or more non-submerged burners. Suitable non-submerged combustion burners may comprise a fuel inlet conduit having an exit nozzle, the conduit and nozzle inserted into a cavity of a ceramic burner block, the ceramic burner block in turn inserted into either the SCM roof or the SCM wall structure, or both the SCM roof and SCM wall structure. Downstream flow channels may also comprise one or more non-submerged burners.


In certain systems, one or more burners in the SCM and/or the flow channel(s) may be adjustable with respect to direction of flow of the combustion products. Adjustment may be via automatic, semi-automatic, or manual control. Certain system embodiments may comprise a burner mount that mounts the burner in the wall structure, roof, or floor of the SCM and/or flow channel comprising a refractory, or refractory-lined ball joint. Other burner mounts may comprise rails mounted in slots in the wall or roof. In yet other embodiments the burners may be mounted outside of the melter or channel, on supports that allow adjustment of the combustion products flow direction. Useable supports include those comprising ball joints, cradles, rails, and the like.


Certain SCMs and/or flow channels may employ one or more high momentum burners, for example, to impinge on portions of a foam layer. High momentum burners useful in apparatus, systems, and methods of this disclosure include those disclosed in Applicant's U.S. Pat. No. 9,021,838. As used herein the phrase “high momentum” combustion burners means burners configured to have a fuel velocity ranging from about 150 ft./second to about 1000 ft./second (about 46 meters/second to about 305 meters/second) and an oxidant velocity ranging from about 150 ft./second to about 1000 ft./second (about 46 meters/second to about 305 meters/second). As used herein the phrase “low momentum” combustion burners means burners configured to have a fuel velocity ranging from about 6 ft./second to about 40 ft./second (about 2 meters/second to about 12 meters/second) and an oxidant velocity ranging from about 6 ft./second to about 40 ft./second (about 2 meters/second to about 12 meters/second).


Certain system and process embodiments of this disclosure may include submerged combustion melters comprising fluid-cooled panels such as disclosed in Applicant's U.S. Pat. No. 8,769,992. In certain system and process embodiments, the submerged combustion melter may include one or more adjustable flame submerged combustion burners comprising one or more oxy-fuel combustion burners, such as described in Applicant's U.S. Pat. No. 8,875,544. In certain systems and processes, the submerged combustion melter may comprise a melter exit structure designed to minimize impact of mechanical energy, such as described in Applicant's U.S. Pat. No. 9,145,319. In certain systems and processes, the flow channel may comprise a series of sections, and may comprise one or more skimmers and/or impingement (high momentum) burners, such as described in Applicant's U.S. Pat. Nos. 9,021,838 and 8,707,739. Certain systems and processes of the present disclosure may utilize measurement and control schemes such as described in Applicant's U.S. Pat. No. 9,096,453, and/or feed batch densification systems and methods as described in Applicant's U.S. Pat. No. 9,643,869. Certain SCMs and processes of the present disclosure may utilize devices for delivery of treating compositions such as disclosed in Applicant's U.S. Pat. No. 8,973,405.


Certain SCMs and process embodiments of this disclosure may be controlled by one or more controllers. For example, burner combustion (flame) temperature may be controlled by monitoring one or more parameters selected from velocity of the fuel, velocity of the primary oxidant, mass and/or volume flow rate of the fuel, mass and/or volume flow rate of the primary oxidant, energy content of the fuel, temperature of the fuel as it enters the burner, temperature of the primary oxidant as it enters the burner, temperature of the effluent, pressure of the primary oxidant entering the burner, humidity of the oxidant, burner geometry, combustion ratio, and combinations thereof. Certain SCMs and processes of this disclosure may also measure and/or monitor feed rate of batch or other feed materials, such as glass batch, cullet, mat or wound roving and treatment compositions, mass of feed, and use these measurements for control purposes. Exemplary systems and methods of the disclosure may comprise a combustion controller which receives one or more input parameters selected from velocity of the fuel, velocity of oxidant, mass and/or volume flow rate of the fuel, mass and/or volume flow rate of oxidant, energy content of the fuel, temperature of the fuel as it enters the burner, temperature of the oxidant as it enters the burner, pressure of the oxidant entering the burner, humidity of the oxidant, burner geometry, oxidation ratio, temperature of the burner combustion products, temperature of melt, composition of bubbles and/or foam, and combinations thereof, and may employ a control algorithm to control combustion temperature, treatment composition flow rate or composition, based on one or more of these input parameters.


Specific non-limiting SCM and process embodiments in accordance with the present disclosure will now be presented in conjunction with FIGS. 1-8. The same numerals are used for the same or similar features in the various figures. In the views illustrated in FIGS. 1-6, it will be understood in each case that the figures are schematic in nature, and certain conventional features are not illustrated in order to illustrate more clearly the key features of each embodiment.



FIG. 1 is a schematic side elevation view, partially in cross-section with some portions cut away, of an SCM embodiment 100 in accordance with this disclosure. Illustrated schematically is a melter 1 fluidly and mechanically connected to a flow channel 26 downstream of melter 1. SCM 1 includes a floor 2, a roof or ceiling 4, a side wall structure 6, an exhaust stack 8, and one or more apertures 10 in floor 2 for corresponding one or more SC burners 12. It will be understood that one or more burners 12 may be mounted in sidewall structure 6. Roof-mounted burners (not illustrated) may also be included, for example for start-up. One or more burners 12 may be oxy/fuel burners. SC burners 12 produce a turbulent melt 14 and melt surface 15, turbulent melt 14 comprising bubbles 16 having a bubble atmosphere. In general the atmosphere of the bubbles is about the same from bubble to bubble, but that is not necessarily so. One or more inlet ports 18 and batch feeders 20 maybe provided. Other feeds are possible, such as glass mat waste, wound roving, waste materials, and the like, such as disclosed in Applicant's U.S. Pat. No. 8,650,914.


Still referring to FIG. 1, floor 2, roof 4, and wall structure 6 define an internal space 21 comprising a first portion 23 and a second portion 25. First portion 23 of internal space 21, along with SC burners 12, a portion 2A of floor 2, and a portion 4A of roof 4 comprise a melting zone 22 of the SCM, while second portion 25 of internal space 21, along with a portion 2B of floor 2 and a portion 4B of ceiling 4 comprise a fining zone 24. SCM embodiment 100, with burners upstream of fining zone 24, and floor portion 2B angled upwards at an angle “α”, assist in reducing or eliminating foam 17 and some of bubbles 16 prior to the molten mass of glass entering downstream flow channel 26. A skimmer 30 having a distal end 31 extending to a point just above the level of molten mass of glass may be provided, further assisting reduction or elimination of foam 17, producing a fined molten mass of glass 28 for further processing. Angle α may range from 0 to about 45 degrees. Larger angles may allow less volume of glass to be process (lower throughput), but a wider fining section may compensate for that. Smaller angles may conversely allow higher throughput, but less fining action.


Referring now to FIG. 2, another SCM embodiment 200 is illustrated schematically. SCM embodiment 200 differs from embodiment 100 illustrated schematically in FIG. 1 by not having a skimmer. The geometry of SCM embodiment 200 may be useful for producing foamy molten glass 29, and thus foamed glass products, or products such as hollow fiber or fiber having regions devoid of glass. In embodiment 200, angle α may range from 0 to about 45 degrees. Larger angles may allow less volume of glass to be process (lower throughput), but a wider fining section may compensate for that. Smaller angles may conversely allow higher throughput of foamy glass in this embodiment.


SCM embodiments 100 and 200 of course could be combined in a single SCM by providing a retractable skimmer 30. This would require a prime mover (not illustrated) that could move skimmer 30 up and down as desired through an aperture between roof 4B and the roof of flow channel 26. Examples of useable prime movers include pneumatic, hydraulic, and electrical devices.



FIG. 3 illustrates schematically another SCM embodiment 300 in accordance with the present disclosure. Embodiment 300 differs from embodiment 100 by the inclusion of a third portion 27 of internal space 21 defined by floor portion 2C, roof portion 4C, and one or more treating composition delivery devices 32, to form a treatment zone 34 downstream of melting zone 22 and upstream of fining zone 24. Treatment composition delivery device 32 may be one or more bubblers, conduits, or other devices configured to direct one or more treating compositions into contact with the molten mass of glass 14. Turbulence in treatment zone 34 may be adjusted, for example by pressure of the treating composition, but is generally less than the turbulence in melting zone 22, and generally more than turbulence in fining zone 24. This contacting produces a treated molten mass of glass 36, which then is passed through fining zone 25 to produce a treated, fined molten mass of glass 38.


In processes of the present disclosure comprising feeding a treating composition into the molten mass of glass and bubbles in a treating zone 34 downstream of melting zone 22 and upstream of fining zone 24, the process may comprise decreasing stability of bubbles 16 using the treating composition, or increasing or substantially maintaining stability of bubbles 16 using the treating composition. In process embodiments where the treating composition decreases stability of bubbles 16, the treating composition may be organic, inorganic, reactive, inert, or partially reactive with gases and other materials in bubbles 16, and/or bubble glass films. In certain embodiments where the treating composition generally decreases stability of SC bubbles 16 (either alone or on combination with a downstream process such as high moisture or helium in flow channel 26, provided there is a driving force from a partial pressure standpoint to push water or helium into bubbles 16), the treating composition may be selected from the group consisting of hydrogen, nitrogen, helium, steam, argon and other noble gases, oxides of nitrogen, oxides of carbon, and oxides of sulfur (for example as described in Applicant's U.S. Pat. No. 8,991,215, and mixtures and combinations thereof. Organic compounds may be used as treatment compositions to decrease stability of bubbles 16, although they would likely not survive the temperatures used in molten glass processing. While not wanting to be held to any particular theory, we believe the addition of an organic compound at glass melting temperatures would decompose to provide carbon, oxygen and nitrogen and their associated gases, and thus they may be reasonable materials to add. Although the specific effects may be difficult to describe, it is reasonable to predict that their decomposition products would have the effect to de-stabilize bubbles, depending on partial pressures of those compounds in the bubbles compared with their partial pressure in the downstream flow channel atmosphere. Certain nano-materials, for example but not limited to nanosilicon particles, nanoclays, carbon nanotubes, carbon spherical morphologies such as buckminsterfullerene (C60, C70, and the like), and diamond may act to impart one or more high-stress locations in a bubble film, forming one or more inclusions, and therefore reduce bubble stability. These solids compounds could be bubbled into the molten mass of glass and bubbles 16 in the form of slurries or other flowable composition. In process embodiments where the treating composition increases or substantially maintains stability of bubbles 16, the treating composition may be organic, inorganic, reactive, inert, or partially reactive with gases and other materials in bubbles 16, and/or bubble glass films. In certain embodiments where the treating composition generally increases or substantially maintains stability of bubbles 16, the treating composition may be selected from the group consisting of dry air, nitrogen-enriched dry air, and dry mixtures of oxygen and nitrogen having concentrations similar to air, for example as described in Applicant's U.S. Pat. No. 8,991,215. Certain of the above-mentioned nano-materials (such as nanoclays), in specified quantities, may increase stability of foams. Finally, it has been found that certain treatment compositions may function to both increase and decrease stability of bubbles 16, depending on the quantity added. For example, sodium sulfate may act as both a stabilizing and a de-stabilizing agent depending on the quantity added. At low levels (about 1 wt. percent or lower, as a percentage of an aqueous treating composition) this compound may act as a surfactant and may improve stability of the bubbles. However at higher levels (about 5 wt. percent or above) the reduction in surface tension may overcome the stabilizing action of the surfactant and cause bubble collapse.


Treating compositions may increase or decrease bubble stability when used separately or in conjunction with one or more downstream processes. For example, adding nitrogen as a treating composition to the molten mass of glass and bubbles 16 may tend to make bubbles 16 less stable when there is the presence of a high moisture atmosphere downstream of melter 1 in downstream flow channel 26. A high moisture atmosphere may exist in downstream flow channel 26 for example when one or more low momentum oxy/fuel combustion burners are used to heat downstream flow channel 26, or when one or more high momentum burners (whether oxy/fuel or not) are used as impingement burners in downstream flow channel 26 to impinge on foam, or when gas lancing is used to impinge an inert or reactive, non-combustion gas on foam in downstream flow channel 26. Use of one or more low momentum burners to produce a moisture-rich atmosphere in downstream flow channel 26, and use of inert or reactive, non-combustion gas lancing into downstream flow channel 26 are both described in Applicant's U.S. Pat. Nos. 9,492,831 and 9,096,452. The use of one or more high momentum impingement burners (whether oxy/fuel or not) in a downstream flow channel is described in Applicant's U.S. Pat. No. 8,707,739.


Measuring effectiveness of the treating composition may generally be made by taking samples of the molten mass of glass and counting bubbles and there size in the molten mass, or a solidified or partially solidified sample thereof, using the naked eye. Another naked eye measurement may simply be comparing an acceptable glass to a treated glass sample, and making a naked eye comparison. More sophisticated methods and equipment may certainly be used, such as image analysis using computers to measure size, size distribution and quantity of bubbles (or other parameters) within a high resolution photograph or micrograph of the material to be analyzed. For example, companies such as Glass Service market processes and equipment for such measurements. The glass melting process, as well as phenomena within the melt, may be continuously observed, recorded and evaluated using an HTO (high temperature observation) furnace equipped with a special silica observation crucible. This equipment may be further coupled with image analysis equipment to provide easy manipulation of recorded data. In a “melt test”, the objective is to evaluate the fining characteristics of differing batch compositions. The area of the recorded images occupied by inhomogeneities (bubbles), bubble size distribution, bubble number, as well as bubble growth rates vs. melting time, may be evaluated to provide comparison between individual batches. The records of the melting course may be provided in the form of video files, which may be replayed on a personal computer, handheld computer, or other viewer. Bubble growth rate measurements may be based on direct observation and recording of bubble sizes depending on time. It is possible to keep bubbles suspended in the melt for hours by the developed “shuttle” method. The temperature dependence of bubble growth rate as a function of the stationary concentration of the refining gases may be used as input data to a computer program known under the trade designation TRACE in a glass furnace model to calculate fining studies. In embodiments where it is desired to decrease stability or remove bubbles, a reduction of 5 percent, or 10 percent, or 20 percent, or 30 percent may be acceptable. In other embodiments, nothing short of complete or substantially complete bubble removal will suffice, in other words 90 percent, or 95 percent, or 99 percent, or even 99.9 percent reduction in bubbles. Similarly, in embodiments where it is desired to stabilize bubbles 16, then a measure of effectiveness may be to visually compare an acceptable sample with a treated sample, either by human or machine-aided device.



FIG. 4 illustrates schematically a side elevation view, partially in cross-section with some portions cut away, of an SCM embodiment 400 in accordance with this disclosure. Embodiment 400 expands on and differs from embodiment 300 in that embodiment 400 includes a fourth portion 33 of internal space 21, defined by a portion 2D of floor 2 and a portion 4D of roof 4. Floor portion 2D and roof portion 4D may be set at an angle “β”, which may range from about 20 degrees to about 90 degrees. The configuration of SCM 400 and others of similar geometry, allows formation of a relatively calm feed zone 40 upstream of melting zone 22, whereby batch feed or other feed materials 44 may be made to float upon relatively calm molten glass 42. This configuration also has the added benefit of allowing the exhaust stack 8 to be placed further downstream, for example in the position illustrated schematically in FIG. 4. This configuration may decrease or substantially eliminate carryover of batch materials before they have a chance to melt in melting zone 22.



FIG. 5 illustrates schematically a side elevation view, partially in cross-section with some portions cut away, of an SCM embodiment 500 in accordance with this disclosure. Embodiment 500 may be termed a “bottom exit” or “dropped throat” SCM. In embodiment 500, melter 1 comprises an extension defined by a floor portion 2E and a roof portion 4E, an optional step 50 and an exit or throat 52 positioned substantially near floor portion 2E to allow molten glass undergoing fining 28A comprising mostly molten glass with few or no bubbles to exit the melter as fined molten glass 28. Fining zone 24 may have a length substantially equal to, less than, or greater than a length of melting zone 22, depending on the degree of fining desired. A longer fining zone 24 will generally produce better fining results, but with the disadvantage of cost of construction. However, flow channel 26 may be able to be shortened. Optionally, stack 8 may be moved to fining zone 24 as noted above in reference to embodiment 400, to decrease batch loss up stack 8. Turbulence in fining zone 24 is less than the turbulence in melting zone 22. In certain embodiments turbulence in fining zone 24 may be 10 percent less than in melting zone 22, or 20 percent less, or 30 percent less, or 40 percent less, or 50 percent less than turbulence in melting zone 22. In certain embodiment it may even be more than 50 percent less than the turbulence in melting zone 22.



FIG. 6 illustrates schematically another SCM embodiment 600, which is similar to embodiment 100 illustrated schematically in FIG. 1, except that exhaust stack 8 is positioned over fining zone 24. In embodiment 600 as illustrated, exhaust stack 8 is positioned quite close to skimmer 30, but this is not necessarily so in all embodiments. The primary function of positioning exhaust stack 8 in fining zone 24 is to reduce the likelihood of entrainment of fine batch particles in the exhaust, effectively bypassing melting zone 23. Basically, we have found that moving the exhaust stack away from the batch feed is a positive move and doing so with a fining extension as well as a batch extension (as illustrated schematically in FIG. 5) are independently positive in their effect.


Devices capable if delivering a treatment composition may or may not be insertable and removable into the SCM. Embodiments of suitable devices are disclosed in Applicant's U.S. Pat. No. 8,973,405. The devices disclosed in that application are essentially conduits having one or more apertures for emitting a treating composition. In one embodiment the conduit includes two left-extending conduits and three right-extending conduits, each having holes or apertures for emitting composition. Other embodiments include only a single elongated slot for emitting composition, while other embodiments may include a plurality of smaller length slots. Yet other embodiments may include a serpentine conduit with a plurality of apertures or orifices for emitting composition. Still other embodiments may include two or more elongated slots positioned on opposite sides of the main conduit. Each of these embodiments, and others, may have advantages in certain situations.



FIGS. 7 and 8 are logic diagrams of two process embodiments 700 and 800 of the present disclosure. Process embodiment 700 includes charging a feed composition into a submerged combustion melter comprising a geometry, at least a portion of the feed composition comprising a vitrifiable material (box 702). The process further comprises heating the feed composition with one or more submerged combustion burners, thereby melting at least a portion of the vitrifiable material in a melting zone of the submerged combustion melter to form a turbulent molten mass of glass and bubbles in the melting zone, box 704. The process further includes allowing the turbulent molten mass of glass and bubbles to flow into a fining zone in the submerged combustion melter immediately downstream of the melting zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a fined molten mass of glass, box 706. The process further includes maintaining a level of molten glass in the fining zone substantially equal to a level of the molten glass in the melting zone, box 708.


Process embodiment 800 includes charging a feed composition into a submerged combustion melter comprising a feed zone, at least a portion of the feed composition comprising a vitrifiable material (box 802). The process further comprises heating the feed composition with one or more submerged combustion burners in a melting zone downstream of the feed zone, thereby melting at least a portion of the vitrifiable material in the melting zone of the submerged combustion melter to form a turbulent molten mass of glass and bubbles in the melting zone, box 804. The process further includes allowing the turbulent molten mass of glass and bubbles to flow from the melting zone into a treating zone in the submerged combustion melter immediately downstream of the melting zone, and feeding a treating composition into the molten glass in the treating zone, the treating zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a treated molten mass of glass (box 806). Process embodiment 800 further comprises allowing the treated molten mass of glass to flow from the treating zone into a fining zone in the submerged combustion melter immediately downstream of the treating zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a treated, fined molten mass of glass (box 808). The process further includes maintaining a level of molten glass in the feed zone, the treating zone, and the fining zone substantially equal to a level of the molten glass in the melting zone, box 810. The process further includes exhausting the submerged combustion melter employing an exhaust stack positioned in the roof of the fining section, box 812.


Flow channel 26 may include one or more bushings (not illustrated) for example when producing glass fiber (not illustrated). Flow channels useful for use in conjunction with SCMs and processes of the present disclosure may comprise a roof, floor and sidewall structure comprised of an outer metal shell, non-glass-contact brick or other refractory wall, and glass-contact refractory for those portions expected to be in contact with molten glass. Flow channels may include several sections arranged in series, each section having a roof, floor, and sidewall structure connecting its roof and floor, and defining a flow channel for conditioning molten glass flowing there through. The sections may be divided by a series of skimmers, each extending generally substantially vertically downward a portion of a distance between the roof and floor of the channel, with a final skimmer positioned between a last channel section and a forehearth. The number of sections and the number of skimmers may each be more or less than two. The flow channel may be rectangular as illustrated in the various figures, or may be a shape such as a generally U-shaped or V-shaped channel or trough of refractory material supported by a metallic superstructure.


The flow rate of the fined molten glass, or the treated, fined molten glass will depend on many factors, including the geometry and size of the SCM, skimmer depth into the molten glass, temperature of the melt, viscosity of the melts, and like parameters, but in general the flow rate of molten glass may range from about 0.5 lb./min to about 5000 lbs./min or more (about 0.23 kg/min to about 2300 kg/min or more), or from about 10 lbs./min to about 500 lbs./min (from about 4.5 kg/min to about 227 kg/min), or from about 100 lbs./min to 300 lbs./min (from about 45 kg/min to about 136 kg/min).


In embodiments where foam is not desired, the SCM and/or flow channel(s) may include one or more high momentum combustion burners (such as in Applicant's U.S. Pat. No. 9,021,838) positioned above the melt in the roof to burst at least some foam retained behind a skimmer, or remaining floating on top of a molten mass of glass flowing in the SCM or flow channel. High momentum burners may act to heat and/or directly impinge on bubbles. Flow channels may also include one or more low momentum combustion burners in the roof of each section to transfer heat to the molten mass of glass without substantial interference from the foamed material. As noted elsewhere herein, low momentum burners, also referred to as non-impingement burners, may alternately or in addition be positioned in section sidewall structures, or both in section roofs and section sidewall structures.


High momentum burners useful in apparatus, systems, and methods of this disclosure include those disclosed Applicant's U.S. Pat. No. 9,021,838, which include an oxidant conduit and an inner concentric fuel conduit. Oxidant and fuel supplies for these burners may quick connect/disconnect features, allowing a hose of other source of fuel to be quickly attached to and detached from the conduits. For example, high momentum burner embodiments may comprise a nominal ¼-inch stainless steel Schedule 40 pipe for the fuel conduit and a nominal ¾-inch stainless steel Schedule 40 pipe for the oxidant conduit. Nominal ¼-inch Schedule 40 pipe has an external diameter of 0.54 inch (1.37 cm) and an internal diameter of 0.36 inch (0.91 cm), while nominal ¾-inch Schedule 40 pipe has an external diameter of 1.05 inch (2.67 cm) and internal diameter of 0.82 inch (2.08 cm). The selection of conduit schedule dictates the annular distance between the OD of the inner fuel conduit and the internal diameter (ID) of the oxidant conduit. These dimensions are merely examples, as any arrangement that produces the desired momentum and/or heat will be suitable, and within the skills of the skilled artisan in possession of this disclosure. High momentum burners may be fluid-cooled by employing a third concentric conduit creating an annular region between the oxidant conduit and third conduit.


For high momentum burners burning natural gas, the burners may have a fuel firing rate ranging from about 10 to about 1000 scfh (from about 280 L/hr. to about 28,000 L/hr.); an oxygen firing rate ranging from about 15 to about 2500 scfh (from about 420 L/hr. to about 71,000 L/hr; a combustion ratio ranging from about 1.5 to about 2.5; nozzle velocity ratio (ratio of velocity of fuel to oxygen at the fuel nozzle tip) ranging from about 0.5 to about 2.5; fuel gas velocity ranging from about 150 to about 1000 ft./sec (from about 46 m/sec to about 300 m/sec); and oxygen velocity ranging from about 150 to about 1000 ft./sec (from about 46 m/sec to about 300 m/sec). Of course these numbers depend on the heating value of the fuel, amount of oxygen in the “oxygen” stream, temperatures and pressures of the fuel and oxidant, and the like, among other parameters. In one typical operation, the high momentum burner would have a combustion ratio of 2.05:1; a velocity ratio of 1; firing rate of natural gas of 500 scfh (14,000 L·hr.) and 1075 scfh (30,400 L/hr.) oxygen; natural gas and oxygen velocities each of 270 ft./sec (80 m/sec); natural gas pressure of 1 psig (6.9 KPa); and oxygen pressure of 0.6 psig (4.1 KPa), pressures measured at the entrance to the combustion chamber.


Low momentum burners useful in apparatus, systems, and methods of this disclosure may include some of the features of those disclosed in Applicant's U.S. Pat. No. 9,021,838. For low momentum burners using natural gas as fuel, the burners may have a fuel firing rate ranging from about 0.4 to about 40 scfh (from about 11 L/hr. to about 1,120 L/hr.); an oxygen firing rate ranging from about 0.6 to about 100 scfh (from about 17 L/hr. to about 2,840 L/hr.); a combustion ratio ranging from about 1.5 to about 2.5; nozzle velocity ratio (ratio of velocity of fuel to oxygen at the fuel nozzle tip) ranging from about 0.5 to about 2.5; a fuel velocity ranging from about 6 ft./second to about 40 ft./second (about 2 meters/second to about 12 meters/second) and an oxidant velocity ranging from about 6 ft./second to about 40 ft./second (about 2 meters/second to about 12 meters/second).


Submerged combustion burners useful in the SC melter apparatus described herein include those described in U.S. Pat. Nos. 4,539,034; 3,170,781; 3,237,929; 3,260,587; 3,606,825; 3,627,504; 3,738,792; 3,764,287; and 7,273,583, and Applicant's U.S. Pat. No. 8,875,544. The total quantities of fuel and oxidant used by the SC burners in systems of the present disclosure may be such that the flow of oxygen may range from about 0.9 to about 1.2 of the theoretical stoichiometric flow of oxygen necessary to obtain the complete combustion of the fuel flow. Another expression of this statement is that the combustion ratio may range from about 0.9 to about 1.2. In certain embodiments, the equivalent fuel content of the feed material must be taken into account. For example, organic binders in glass fiber mat scrap materials will increase the oxidant requirement above that required strictly for fuel being combusted. In consideration of these embodiments, the combustion ratio may be increased above 1.2, for example to 1.5, or to 2, or 2.5, or even higher, depending on the organic content of the feed materials.


The velocity of the fuel gas in the various SC burners depends on the burner geometry used, but generally is at least about 15 m/s. The upper limit of fuel velocity depends primarily on the desired mixing of the melt in the melter apparatus, melter geometry, and the geometry of the burner; if the fuel velocity is too low, the flame temperature may be too low, providing inadequate melting, which is not desired, and if the fuel flow is too high, flame might impinge on the melter floor, roof or wall, and/or heat will be wasted, which is also not desired.


In certain embodiments the SC burners may be floor-mounted burners. In certain embodiments, the SC burners may be positioned in rows substantially perpendicular to the longitudinal axis (in the melt flow direction) of melter 10. In certain embodiments, the SC burners may be positioned to emit combustion products into molten glass in a melting zone in a fashion so that the gases penetrate the melt generally perpendicularly to the floor. In other embodiments, one or more burners may emit combustion products into the melt at an angle to the floor of the melter, as taught in Applicant's U.S. Pat. No. 8,769,992.


Those of skill in this art will readily understand the need for, and be able to construct suitable fuel supply conduits and oxidant supply conduits, as well as respective flow control valves, threaded fittings, quick connect/disconnect fittings, hose fittings, and the like.


High momentum burners and low momentum burners may be mounted to the sidewall structure and/or roof of the flow channel sections using adjustable mounts, such as a ceramic-lined ball turrets, as explained in the afore-mentioned U.S. Pat. No. 9,021,838.


Aside from the features newly described herein, SCMs described herein may be any of the currently known submerged combustion melter designs, or may be one of those described in Applicant's U.S. Pat. No. 8,769,992. SCMs may take any number of forms, including those described in Applicant's '992 patent, which describes sidewalls forming an expanding melting zone formed by a first trapezoidal region, and a narrowing melting zone formed by a second trapezoidal region, wherein a common base between the trapezoid defines the location of the maximum width of the melter. Optionally, fluid-cooled panels may comprise some or all of the sidewall structure.


Submerged combustion melters may be fed a variety of feed materials by one or more roll stands, which in turn supports one or more rolls of glass mat, as described in Applicant's U.S. Pat. No. 8,650,914, incorporated herein by reference. In certain embodiments powered nip rolls may include cutting knives or other cutting components to cut or chop the mat (or roving, in those embodiments processing roving) into smaller length pieces prior to entering melter 602. Also provided in certain embodiments may be a glass batch feeder. Glass batch feeders are well-known in this art and require no further explanation.


The initial raw material may include any material suitable for forming molten glass such as, for example, limestone, glass, sand, soda ash, feldspar and mixtures thereof. A glass composition for producing glass fibers known as “E-glass” typically includes 52-56% SiO2, 12-16% Al2O3, 0-0.8% Fe2O3, 16-25% CaO, 0-6% MgO, 0-10% B2O3, 0-2% Na2O+K2O, 0-1.5% TiO2 and 0-1% F2. Other glass compositions may be used, such as those described in Applicant's published U.S. Applications 2007/0220922 and 2008/0276652. The initial raw material to provide these glass compositions can be calculated in known manner from the desired concentrations of glass components, molar masses of glass components, chemical formulas of batch components, and the molar masses of the batch components. Typical E-glass batches include those reproduced in Table 1, borrowed from the 2007/0220922 published application. Notice that during glass melting, carbon dioxide (from lime) and water (borax) evaporate. The initial raw material can be provided in any form such as, for example, relatively small particles.









TABLE 1







A typical E-glass batch


BATCH COMPOSITION (BY WEIGHT)
























Ca





Quartz








Silicate &



Ca

and
Ca



Limestone
Quick-
Ca
Volcanic
Volcanic
Quartz-
Quartz-
Limestone
Silicate
Quartz-
Clay
Silicate/


Raw material
(Baseline)
lime
Silicate
Glass
Glass
free #1
free #2
Slag
Slag
free #3
Free
Feldspar






















Quartz (flint)
31.3% 
35.9% 
15.2% 
22.6%
8.5%
0%
0%
22.3%  
5.7%
  0%
0%
19.9%  


Kaolin Clay
28.1% 
32.3% 
32.0% 
23.0%
28.2% 
26.4%  
0%
22.7%  
26.0% 
26.0% 
0%
0%


BD Lime
3.4%
4.3%
3.9%
 3.3%
3.8%
3.7%  
4.3%  
2.8%  
3.1%
3.1%
4.3%  
4.4%  


Borax
4.7%
5.2%
5.2%
  0%
1.5%
0%
0%
0%
  0%
  0%
1.1%  
1.1%  


Boric Acid
3.2%
3.9%
3.6%
 7.3%
6.9%
8.2%  
8.6%  
7.3%  
8.2%
8.2%
7.7%  
7.8%  


Salt Cake
0.2%
0.2%
0.2%
 0.2%
0.2%
0.2%  
0.2%  
0.2%  
0.2%
0.2%
0.2%  
0.2%  


Limestone
29.1% 
  0%
  0%
28.7%
  0%
0%
0%
27.9%  
  0%
  0%
0%
0%


Quicklime
  0%
18.3% 
  0%
  0%
  0%
0%
0%
0%
  0%
  0%
0%
0%


Calcium
  0%
  0%
39.9% 
  0%
39.1% 
39.0%  
27.6%  
0%
37.9% 
37.9% 
26.5%  
26.6%  


Silicate














Volcanic Glass
  0%
  0%
  0%
14.9%
11.8% 
17.0%  
4.2%  
14.7%  
16.8% 
16.8% 
0%
0%


Diatomaceous





5.5%  
17.4%  
0%
  0%
5.7%
20.0%  
0%


Earth (DE)














Plagioclase





0%
38.3%  
0%
  0%
  0%
40.1%  
40.1%  


Feldspar














Slag





0%
0%
2.0%  
2.0%
2.0%
0%
0%


Total
 100% 
 100% 
 100% 
 100%
 100% 
100% 
100% 
100% 
 100% 
 100% 
100% 
100% 


Volume of
1668  
0
0
1647 
0
0  
0  
1624   
0
0
0  
0  


  CO2@














1400 C.









SCMs in accordance with the present disclosure may also comprise one or more wall-mounted submerged combustion burners, and/or one or more roof-mounted burners. Roof-mounted burners may be useful to pre-heat the melting zone, and serve as ignition sources for one or more submerged combustion burners. Melters having only wall-mounted, submerged-combustion burners are also considered within the present disclosure. Roof-mounted burners may be oxy-fuel burners, but as they are typically only used in certain situations, are more likely to be air/fuel burners. Most often they would be shut-off after pre-heating the melter and/or after starting one or more submerged combustion burners. In certain embodiments, if there is a possibility of carryover of particles to the exhaust, one or more roof-mounted burners could be used to form a curtain to prevent particulate carryover. In certain embodiments, one or more submerged combustion burners may be oxy/fuel burners (where “oxy” means oxygen, or oxygen-enriched air, as described earlier), but this is not necessarily so in all embodiments; some or all of the submerged combustion burners may be air/fuel burners. Furthermore, heating may be supplemented by electrical heating in certain melter embodiments, in melting zones, feed zones, treating zones, and/or fining zones. In certain embodiments the oxy-fuel burners may comprise one or more submerged combustion burners each having co-axial fuel and oxidant tubes forming an annular space there between, wherein the outer tube extends beyond the end of the inner tube, as taught in U.S. Pat. No. 7,273,583. Burners may be flush-mounted with the melter floor in certain embodiments. In other embodiments, such as disclosed in the '583 patent, a portion of one or more of the burners may extend slightly into the melt above the melter floor.


In certain embodiments, melter sidewalls may have a free-flowing form, devoid of angles. In certain other embodiments, sidewalls may be configured so that an intermediate location may comprise an intermediate region of melters having constant width, extending from a first trapezoidal region to the beginning of a narrowing melting region. Other embodiments of suitable melters are described in the above-mentioned U.S. Pat. No. 8,769,992.


As mentioned herein, SCMs may include refractory fluid-cooled panels. Liquid-cooled panels may be used, having one or more conduits or tubing therein, supplied with liquid through one conduit, with another conduit discharging warmed liquid, routing heat transferred from inside the melter to the liquid away from the melter. Liquid-cooled panels may also include a thin refractory liner, which minimizes heat losses from the melter, but allows formation of a thin frozen glass shell to form on the surfaces and prevent any refractory wear and associated glass contamination. Other useful cooled panels include air-cooled panels, comprising a conduit that has a first, small diameter section, and a large diameter section. Warmed air transverses the conduits such that the conduit having the larger diameter accommodates expansion of the air as it is warmed. Air-cooled panels are described more fully in U.S. Pat. No. 6,244,197. In certain embodiments, the refractory fluid cooled-panels are cooled by a heat transfer fluid selected from the group consisting of gaseous, liquid, or combinations of gaseous and liquid compositions that functions or is capable of being modified to function as a heat transfer fluid. Gaseous heat transfer fluids may be selected from air, including ambient air and treated air (for air treated to remove moisture), inert inorganic gases, such as nitrogen, argon, and helium, inert organic gases such as fluoro-, chloro- and chlorofluorocarbons, including perfluorinated versions, such as tetrafluoromethane, and hexafluoroethane, and tetrafluoroethylene, and the like, and mixtures of inert gases with small portions of non-inert gases, such as hydrogen. Heat transfer liquids may be selected from inert liquids that may be organic, inorganic, or some combination thereof, for example, salt solutions, glycol solutions, oils and the like. Other possible heat transfer fluids include steam (if cooler than the oxygen manifold temperature), carbon dioxide, or mixtures thereof with nitrogen. Heat transfer fluids may be compositions comprising both gas and liquid phases, such as the higher chlorofluorocarbons.


Certain embodiments may comprise a process control scheme for the submerged combustion melter and burners. For example, as explained in the '970 application, a master process controller may be configured to provide any number of control logics, including feedback control, feed-forward control, cascade control, and the like. The disclosure is not limited to a single master process controller, as any combination of controllers could be used. The term “control”, used as a transitive verb, means to verify or regulate by comparing with a standard or desired value. Control may be closed loop, feedback, feed-forward, cascade, model predictive, adaptive, heuristic and combinations thereof. The term “controller” means a device at least capable of accepting input from sensors and meters in real time or near-real time, and sending commands directly to burner control elements, and/or to local devices associated with burner control elements and glass mat feeding devices able to accept commands. A controller may also be capable of accepting input from human operators; accessing databases, such as relational databases; sending data to and accessing data in databases, data warehouses or data marts; and sending information to and accepting input from a display device readable by a human. A controller may also interface with or have integrated therewith one or more software application modules, and may supervise interaction between databases and one or more software application modules. The controller may utilize Model Predictive Control (MPC) or other advanced multivariable control methods used in multiple input/multiple output (MIMO) systems. The methods of Applicant's U.S. Pat. No. 8,973,400, using the vibrations and oscillations of the melter itself, may prove useful predictive control inputs.


Both the melter and flow channel floors and sidewall structures may include a glass-contact refractory lining, as discussed herein. The glass-contact lining may be 1 centimeter, 2 centimeters, 3 centimeters or more in thickness, however, greater thickness may entail more expense without resultant greater benefit. The refractory lining may be one or multiple layers. Glass-contact refractory used in melters and channels described herein may be cast concretes such as disclosed in U.S. Pat. No. 4,323,718. Two cast concrete layers are described in the '718 patent, the first being a hydraulically setting insulating composition (for example, that known under the trade designation CASTABLE BLOC-MIX-G, a product of Fleischmann Company, Frankfurt/Main, Federal Republic of Germany). This composition may be poured in a form of a wall section of desired thickness, for example a layer 5 cm thick, or 10 cm, or greater. This material is allowed to set, followed by a second layer of a hydraulically setting refractory casting composition (such as that known under the trade designation RAPID BLOCK RG 158, a product of Fleischmann company, Frankfurt/Main, Federal Republic of Germany) may be applied thereonto. Other suitable materials for the refractory cooled panels, melter and channel refractory liners, and refractory block burners (if used) are fused zirconia (ZrO2), fused cast AZS (alumina-zirconia-silica), rebonded AZS, or fused cast alumina (Al2O3). The choice of a particular material is dictated among other parameters by the melter geometry and type of glass to be produced. The refractory or refractory-lined channels or troughs described in accordance with the present disclosure may be constructed using refractory cooled panels.


Those having ordinary skill in this art will appreciate that there are many possible variations of the melter, flow channels, burners, and adjustment mechanisms to adjust composition emission into the molten glass and foaming, and will be able to devise alternatives and improvements to those described herein that are nevertheless considered to be within the claims.

Claims
  • 1. A submerged combustion melter comprising: a floor, a roof, and a sidewall structure connecting the floor and roof defining an internal space, a first portion of the internal space comprising a melting zone, a second portion of the internal space defining a fining zone downstream of the melting zone, and a third portion of the internal space comprising a treating zone downstream of the melting zone and upstream of the fining zone, the treating zone comprising one or more apparatus configured to inject a treating composition into a molten mass of glass containing bubbles in the treating zone, the treating zone and the fining zone devoid of submerged combustion burners and other apparatus that would increase turbulence above that in the melting zone;one or more combustion burners in either the floor, the roof, the sidewall structure, or any two or more of these, producing combustion gases and configured to emit the combustion gases from a position under a level of, and positioned to transfer heat to and produce, a turbulent molten mass of glass containing bubbles in the melting zone;a skimmer having distal end adapted to extend to a point just above a level of molten mass of glass exiting the fining zone to hold back a portion of foam floating on the molten mass of glass flowing out of the fining zone;the submerged combustion melter comprising a geometry whereby the level of the molten glass is substantially equivalent in the melting zone, the treatment zone, and the fining zone, wherein the floor in the melting zone is substantially horizontal and the floor in the fining zone is angled upward at an angle α with respect to the substantially horizontal floor in the melting zone so that the floor in the fining zone is angled upward relative to horizontal beginning at an entrance to the fining zone and extending to an exit of the fining zone and rises uniformly from the depth of the substantially horizontal floor in the melting zone to a final depth that is at least 10 percent less than the depth of the substantially horizontal floor in the melting zone.
  • 2. A submerged combustion melter comprising: a floor, a roof, and a sidewall structure connecting the floor and roof defining an internal space, a first portion of the internal space comprising a melting zone, and a second portion of the internal space comprising a fining zone downstream of the melting zone, a third portion of the internal space comprising a treating zone downstream of the melting zone and upstream of the fining zone, the treating zone comprising one or more non-burner apparatus configured to inject a treating composition into a molten mass of glass containing bubbles in the treating zone, and a fourth portion of the internal space comprising a feed zone upstream of the melting zone, wherein the feed zone, the treating zone, and the fining zone are all devoid of submerged combustion burners and other apparatus that would increase turbulence above that in the melting zone;one or more combustion burners in either the floor, the roof, the sidewall structure, or any two or more of these, producing combustion gases and configured to emit the combustion gases from a position under a level of, and positioned to transfer heat to and produce, a turbulent molten mass of glass containing bubbles in the melting zone;a skimmer having distal end adapted to extend to a point just above a level of molten mass of glass exiting the fining zone to hold back a portion of foam floating on the molten mass of glass flowing out of the fining zone; andthe submerged combustion melter comprising a geometry whereby the level of the molten glass is substantially equivalent in the feed zone, the melting zone, the treating zone, and the fining zone, wherein the floor in the melting zone is substantially horizontal, the floor in the feed zone is angled at an angle β with respect to the substantially horizontal floor in the melting zone so that the floor in the feed zone falls uniformly from an initial depth that is at least 10 percent less than a depth of the substantially horizontal floor in the melting zone, and the floor in the fining zone is angled at an angle α with respect to the substantially horizontal floor in the melting zone so that the floor in the fining zone is angled upward relative to horizontal beginning at an entrance to the fining zone and extending to an exit of the fining zone and rises uniformly from the depth of the substantially horizontal floor in the melting zone to a final depth that is at least 10 percent less than the depth of the substantially horizontal floor in the melting zone, and α and β are the same or different.
  • 3. A process comprising: charging a feed composition into a submerged combustion melter comprising a geometry, at least a portion of the feed composition comprising a vitrifiable material;heating the feed composition with one or more submerged combustion burners, thereby melting at least a portion of the vitrifiable material in a melting zone of the submerged combustion melter to form a turbulent molten mass of glass and bubbles in the melting zone;allowing the turbulent molten mass of glass and bubbles to flow from the melting zone into a treating zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a less turbulent molten mass of glass containing bubbles in the treating zone, the treating zone immediately downstream of the melting zone, while injecting a treating composition into the less turbulent molten mass of glass containing bubbles in the treating zone using one or more non-burner apparatus, thus forming a treated molten mass of glass having foam on an upper surface thereof;allowing the treated molten mass of glass and bubbles to flow into a fining zone in the submerged combustion melter immediately downstream of the treating zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone and the treating zone, thus forming a fined molten mass of glass having foam on an upper surface thereof;skimming at least a portion of the foam on the upper surface of the fined molten mass of glass as it leaves the fining zone; andmaintaining a level of molten glass in the treating zone and the fining zone substantially equal to a level of the molten glass in the melting zone, the melter geometry comprises a floor in the melting zone being substantially horizontal and a floor in the fining zone is angled upward at an angle α with respect to the substantially horizontal floor in the melting zone so that the floor in the fining zone is angled upward relative to horizontal beginning at an entrance to the fining zone and extending to an exit of the fining zone and rises uniformly from the depth of the substantially horizontal floor in the melting zone to a final depth that is at least 10 percent less than the depth of the substantially horizontal floor in the melting zone.
  • 4. The process of claim 3 comprising flowing the fined molten mass of glass from the fining zone into a flow channel fluidly and mechanically connected to the melter downstream of the fining zone.
  • 5. The process of claim 3 wherein the skimming of at least a portion of the foam on the upper surface of the fined molten mass of glass as it exits the fining zone comprises using a skimmer having a distal end, the distal end extending into the molten glass a depth sufficient to hold back a portion of the fined molten mass of glass flowing out of the submerged combustion melter through an exit that is lower than the distal end of the skimmer.
  • 6. The process of claim 3 comprising decreasing stability of the bubbles using the treating composition.
  • 7. The process of claim 6 wherein the treating composition is selected from the group consisting of nitrogen, argon, dry air, nitrogen-enriched dry air, and combinations thereof.
  • 8. The process of claim 3 comprising increasing stability of the bubbles using the treating composition.
  • 9. The process of claim 8 wherein the treatment composition is selected from the group consisting of oxides of sulfur, oxides of nitrogen, and combinations thereof.
  • 10. The process of claim 3 wherein the charging of a feed composition into a submerged combustion melter comprising a geometry comprises feeding a feed zone upstream of the melting zone, the feed zone devoid of submerged combustion burners.
  • 11. The process of claim 3 comprising exhausting the submerged combustion melter employing an exhaust stack positioned in the roof of the fining zone.
  • 12. A process comprising: charging a feed composition into a feed zone of a submerged combustion melter, at least a portion of the feed composition comprising a vitrifiable material;heating the feed composition with one or more submerged combustion burners, thereby melting at least a portion of the vitrifiable material in a melting zone of the submerged combustion melter immediately downstream of the feed zone to form a turbulent molten mass of glass and bubbles in the melting zone;allowing the turbulent molten mass of glass and bubbles to flow from the melting zone into a treating zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone, thus forming a less turbulent molten mass of glass containing bubbles in the treating zone, the treating zone immediately downstream of the melting zone, while injecting a treating composition into the less turbulent molten mass of glass containing bubbles in the treating zone using one or more non-burner apparatus, thus forming a treated molten mass of glass containing bubbles having foam on an upper surface thereof;allowing the treated molten mass of glass containing bubbles having foam on the upper surface thereof to flow into a fining zone in the submerged combustion melter immediately downstream of the treating zone, the fining zone devoid of submerged combustion burners and other apparatus or components that would increase turbulence above that in the melting zone and the treating zone, thus forming a fined molten mass of glass having foam on an upper surface thereof;skimming at least a portion of the foam on the upper surface of the fined molten mass of glass as it leaves the fining zone; andmaintaining a level of molten glass in the feed zone, the treating zone, and the fining zone substantially equal to a level of the molten glass in the melting zone, wherein a floor in the melting zone is substantially horizontal, a floor in the feed zone is angled at an angle β with respect to the floor in the melting zone so that the floor in the feed zone falls uniformly from an initial depth that is at least 10 percent less than a depth of the substantially horizontal floor in the melting zone, and a floor in the fining zone is angled at an angle α with respect to the substantially horizontal floor in the melting zone so that the floor in the fining zone is angled upward relative to horizontal beginning at an entrance to the fining zone and extending to an exit of the fining zone and rises uniformly from the depth of the substantially horizontal floor in the melting zone to a final depth that is at least 10 percent less than the depth of the substantially horizontal floor in the melting zone, and α and β are the same or different.
  • 13. The process of claim 12 comprising flowing the fined molten glass from the fining zone into a flow channel fluidly and mechanically connected to the melter downstream of the fining zone.
  • 14. The process of claim 12 wherein the skimming of the fined molten mass of glass as it exits the fining zone comprises using a skimmer having a distal end, the distal end extending into the molten glass a depth sufficient to hold back a portion of the fined molten glass flowing out of the submerged combustion melter through an exit that is lower than the distal end of the skimmer.
CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a Division of U.S. application Ser. No. 13/633,979 filed Oct. 3, 2012, now U.S. Pat. No. 9,533,905, issued Jan. 3, 2017, and this application may be related to the following United States Patents assigned to the Applicant of the present application which are all incorporated by reference herein: U.S. Pat. Nos. 8,769,992, 8,997,525, 8,875,544, 8,707,740, 9,021,838, 9,145,319, 8,707,739, 9,096,453 and 9,032,760.

US Referenced Citations (445)
Number Name Date Kind
1579353 Good Apr 1926 A
1636151 Schofield Jul 1927 A
1679295 Dodge Jul 1928 A
1706857 Mathe Mar 1929 A
1716433 Ellis Jun 1929 A
1675474 McKinley Sep 1932 A
1883023 Slick Oct 1932 A
1937321 Howard Nov 1933 A
1944855 Wadman Jan 1934 A
1989103 McKelvey et al. Jan 1935 A
2042560 Stewart Jun 1936 A
2064546 Kutchka Dec 1936 A
2174533 See et al. Oct 1939 A
2118479 McCaskey Jan 1940 A
2269459 Kleist Jan 1942 A
2432942 See et al. Dec 1947 A
2455907 Slayter Jan 1948 A
2597858 Howard May 1952 A
2658094 Nonken Nov 1953 A
2677003 Arbeit et al. Apr 1954 A
2679749 Poole Jun 1954 A
2691689 Arbeit et al. Oct 1954 A
2718096 Henry et al. Sep 1955 A
2773545 Petersen Dec 1956 A
2781756 Kobe Feb 1957 A
2867972 Holderreed et al. Jan 1959 A
2878644 Fenn Mar 1959 A
2690166 Heinze Jun 1959 A
2902029 Hill Sep 1959 A
2981250 Stewart Apr 1961 A
3020165 Davis Feb 1962 A
3056283 Tiede Oct 1962 A
3073683 Switzer et al. Jan 1963 A
3084392 Labino Apr 1963 A
3088812 Bitterlich et al. May 1963 A
3104947 Switzer et al. Sep 1963 A
3129087 Hagy Apr 1964 A
3160578 Saxton et al. Dec 1964 A
3165452 Williams Jan 1965 A
3170781 Keefer Feb 1965 A
3174820 See et al. Mar 1965 A
3215189 Bauer Nov 1965 A
3224855 Plumat Dec 1965 A
3226220 Plumat Dec 1965 A
3237929 Piumat et al. Mar 1966 A
3239325 Roberson et al. Mar 1966 A
3241548 See et al. Mar 1966 A
3245769 Eck et al. Apr 1966 A
3248205 Dolf et al. Apr 1966 A
3248206 Apple et al. Apr 1966 A
3260587 Dolf et al. Jul 1966 A
3268313 Burgman et al. Aug 1966 A
3285834 Guerrieri et al. Nov 1966 A
3294512 Penberthy Dec 1966 A
3325298 Brown Jun 1967 A
3375095 Poole Mar 1968 A
3380463 Trethewey Apr 1968 A
3385686 Plumat et al. May 1968 A
3402025 Garrett et al. Sep 1968 A
3407805 Bougard Oct 1968 A
3407862 Mustian, Jr. Oct 1968 A
3420510 Griem Jan 1969 A
3421873 Burgman et al. Jan 1969 A
3421876 Schmidt Jan 1969 A
3432399 Schutt Mar 1969 A
3442633 Perry May 1969 A
3445214 Oremesher May 1969 A
3498779 Hathaway Mar 1970 A
3499743 Fanica et al. Mar 1970 A
3510393 Burgman et al. May 1970 A
3519412 Olink Jul 1970 A
3525674 Barnebey Aug 1970 A
3533770 Adler et al. Oct 1970 A
3547611 Williams Dec 1970 A
3563683 Hess Feb 1971 A
3573016 Rees Mar 1971 A
3592151 Webber Jul 1971 A
3592633 Shepherd Jul 1971 A
3600149 Chen et al. Aug 1971 A
3606825 Johnson Sep 1971 A
3617234 Hawkins et al. Nov 1971 A
3627504 Johnson et al. Dec 1971 A
3632335 Worner Jan 1972 A
3649235 Harris Mar 1972 A
3692017 Glachant et al. Sep 1972 A
3717139 Guillet et al. Feb 1973 A
3738792 Feng Jun 1973 A
3741656 Shapiro Jun 1973 A
3741742 Jennings Jun 1973 A
3746527 Knavish et al. Jul 1973 A
3747588 Malmin Jul 1973 A
3754879 Phaneuf Aug 1973 A
3756800 Phaneuf Sep 1973 A
3763915 Perry et al. Oct 1973 A
3764287 Brocious Oct 1973 A
3771988 Starr Nov 1973 A
3788832 Nesbitt Jan 1974 A
3818893 Kataoka et al. Jun 1974 A
3835909 Douglas et al. Sep 1974 A
3840002 Douglas et al. Oct 1974 A
3856496 Nesbitt et al. Dec 1974 A
3885945 Rees et al. May 1975 A
3907585 Francel et al. Sep 1975 A
3913560 Lazarre et al. Oct 1975 A
3929445 Zippe Dec 1975 A
3936290 Cerutti et al. Feb 1976 A
3951635 Rough Apr 1976 A
3976464 Wardlaw Aug 1976 A
4001001 Knavish et al. Jan 1977 A
4004903 Daman et al. Jan 1977 A
4028083 Patznick et al. Jun 1977 A
4083711 Jensen Apr 1978 A
4101304 Marchand Jul 1978 A
4110098 Mattmuller Aug 1978 A
4153438 Stream May 1979 A
4185982 Schwenninger Jan 1980 A
4203761 Rose May 1980 A
4205966 Horikawa Jun 1980 A
4208201 Rueck Jun 1980 A
4226564 Takahashi et al. Oct 1980 A
4238226 Sanzenbacher et al. Dec 1980 A
4249927 Fakuzaki et al. Feb 1981 A
4270740 Sanzenbacher et al. Jun 1981 A
4282023 Hammel et al. Aug 1981 A
4303435 Seighter Dec 1981 A
4309204 Brooks Jan 1982 A
4316734 Spinosa et al. Feb 1982 A
4323718 Buhring et al. Apr 1982 A
4349376 Dunn et al. Sep 1982 A
4360373 Pecoraro Nov 1982 A
4397692 Ramge et al. Aug 1983 A
4398925 Trinh et al. Aug 1983 A
4405351 Sheinkop Sep 1983 A
4406683 Demarest Sep 1983 A
4413882 Bailey et al. Nov 1983 A
4424071 Steitz et al. Jan 1984 A
4432760 Propster et al. Feb 1984 A
4455762 Saeman Jun 1984 A
4461576 King Jul 1984 A
4488537 Laurent Dec 1984 A
4508970 Ackerman Apr 1985 A
4539034 Hanneken Sep 1985 A
4542106 Sproull Sep 1985 A
4545800 Won et al. Oct 1985 A
4549896 Streicher et al. Oct 1985 A
4599100 Demarest Jul 1986 A
4622007 Gitman Nov 1986 A
4626199 Bounini Dec 1986 A
4632687 Kunkle et al. Dec 1986 A
4634461 Demarest, Jr. et al. Jan 1987 A
4657586 Masterson et al. Apr 1987 A
4718931 Boettner Jan 1988 A
4723708 Berger et al. Feb 1988 A
4735642 Jensen et al. Apr 1988 A
4738938 Kunkle et al. Apr 1988 A
4758259 Jensen Jul 1988 A
4780122 Schwenninger et al. Oct 1988 A
4794860 Welton Jan 1989 A
4798616 Knavish et al. Jan 1989 A
4812372 Kithany Mar 1989 A
4814387 Donat Mar 1989 A
4816056 Tsai et al. Mar 1989 A
4818265 Krumwiede et al. Apr 1989 A
4877436 Sheinkop Oct 1989 A
4877449 Khinkis Oct 1989 A
4878829 Anderson Nov 1989 A
4882736 Pieper Nov 1989 A
4886539 Gerutti et al. Dec 1989 A
4900337 Zortea et al. Feb 1990 A
4919700 Pecoraro et al. Apr 1990 A
4927866 Backderf et al. May 1990 A
4932035 Pieper Jun 1990 A
4953376 Merlone Sep 1990 A
4963731 King Oct 1990 A
4969942 Schwenninger et al. Nov 1990 A
4973346 Kobayashi et al. Nov 1990 A
5011086 Sonnleitner Apr 1991 A
5032230 Shepherd Jul 1991 A
5052874 Johanson Oct 1991 A
5062789 Gitman Nov 1991 A
5097802 Clawson Mar 1992 A
5168109 Backderf et al. Dec 1992 A
5169424 Grinnen et al. Dec 1992 A
5194747 Culpepper et al. Mar 1993 A
5199866 Joshi et al. Apr 1993 A
5204082 Schendel Apr 1993 A
5299929 Yap Apr 1994 A
5360171 Yap Nov 1994 A
5374595 Dumbaugh et al. Dec 1994 A
5405082 Brown et al. Apr 1995 A
5412882 Zippe et al. May 1995 A
5449286 Snyder et al. Sep 1995 A
5473885 Hunter, Jr. et al. Dec 1995 A
5483548 Coble Jan 1996 A
5490775 Joshi et al. Feb 1996 A
5522721 Drogue et al. Jun 1996 A
5545031 Joshi et al. Aug 1996 A
5575637 Slavejkov et al. Nov 1996 A
5586999 Kobayashi Dec 1996 A
5595703 Swaelens et al. Jan 1997 A
5606965 Panz et al. Mar 1997 A
5613994 Muniz et al. Mar 1997 A
5615668 Panz et al. Apr 1997 A
5636623 Panz et al. Jun 1997 A
5672827 Jursich Sep 1997 A
5713668 Lunghofer et al. Feb 1998 A
5718741 Hull et al. Feb 1998 A
5724901 Guy et al. Mar 1998 A
5736476 Warzke et al. Apr 1998 A
5743723 Iatrides et al. Apr 1998 A
5765964 Calcote et al. Jun 1998 A
5814121 Travis Sep 1998 A
5829962 Drasek et al. Nov 1998 A
5833447 Bodelin et al. Nov 1998 A
5849058 Takeshita et al. Dec 1998 A
5863195 Feldermann Jan 1999 A
5887978 Lunghofer et al. Mar 1999 A
5944507 Feldermann Aug 1999 A
5944864 Hull et al. Aug 1999 A
5954498 Joshi et al. Sep 1999 A
5975886 Phillippe Nov 1999 A
5979191 Jian Nov 1999 A
5984667 Phillippe et al. Nov 1999 A
5993203 Koppang Nov 1999 A
6029910 Joshi et al. Feb 2000 A
6036480 Hughes et al. Mar 2000 A
6039787 Edlinger Mar 2000 A
6044667 Chenoweth Apr 2000 A
6045353 VonDrasek et al. Apr 2000 A
6068468 Phillipe et al. May 2000 A
6071116 Phillipe et al. Jun 2000 A
6074197 Phillippe Jun 2000 A
6077072 Marin et al. Jun 2000 A
6085551 Pieper et al. Jul 2000 A
6109062 Richards Aug 2000 A
6113389 Joshi et al. Sep 2000 A
6116896 Joshi et al. Sep 2000 A
6120889 Turner et al. Sep 2000 A
6123542 Joshi et al. Sep 2000 A
6126438 Joshi et al. Oct 2000 A
6154481 Sorg et al. Nov 2000 A
6156285 Adams et al. Dec 2000 A
6171100 Joshi et al. Jan 2001 B1
6178777 Chenoweth Jan 2001 B1
6183848 Turner et al. Feb 2001 B1
6210151 Joshi et al. Apr 2001 B1
6210703 Novich Apr 2001 B1
6237369 LeBlanc et al. May 2001 B1
6241514 Joshi et al. Jun 2001 B1
6244197 Coble Jun 2001 B1
6244857 VonDrasek et al. Jun 2001 B1
6247315 Marin et al. Jun 2001 B1
6250136 Igreja Jun 2001 B1
6250916 Phillipe et al. Jun 2001 B1
6274164 Novich Aug 2001 B1
6276924 Joshi et al. Aug 2001 B1
6276928 Joshi et al. Aug 2001 B1
6293277 Panz et al. Sep 2001 B1
6314760 Chenoweth Nov 2001 B1
6314896 Marin et al. Nov 2001 B1
6318126 Takei et al. Nov 2001 B1
6332339 Kawaguchi et al. Dec 2001 B1
6338337 Panz et al. Jan 2002 B1
6339610 Hoyer et al. Jan 2002 B1
6344747 Lunghofer et al. Feb 2002 B1
6357264 Richards Mar 2002 B1
6386271 Kawamoto et al. May 2002 B1
6398547 Joshi et al. Jun 2002 B1
6404799 Mori et al. Jun 2002 B1
6418755 Chenoweth Jul 2002 B2
6422041 Simpson et al. Jul 2002 B1
6454562 Joshi et al. Sep 2002 B1
6460376 Jeanvoine et al. Oct 2002 B1
6470710 Takei et al. Oct 2002 B1
6536238 Kawaguchi et al. Mar 2003 B2
6536651 Ezumi et al. Mar 2003 B2
6558606 Kulkarni et al. May 2003 B1
6578779 Dion Jun 2003 B2
6660106 Babel et al. Dec 2003 B1
6694791 Johnson et al. Feb 2004 B1
6701617 Li et al. Mar 2004 B2
6701751 Arechaga et al. Mar 2004 B2
6705118 Simpson et al. Mar 2004 B2
6708527 Ibarlucea et al. Mar 2004 B1
6711942 Getman et al. Mar 2004 B2
6715319 Barrow et al. Apr 2004 B2
6722161 LeBlanc Apr 2004 B2
6736129 Sjith May 2004 B1
6739152 Jeanvoine et al. May 2004 B2
6796147 Borysowicz et al. Sep 2004 B2
6797351 Kulkarni et al. Sep 2004 B2
6854290 Hayes et al. Feb 2005 B2
6857999 Jeanvoine Feb 2005 B2
6883349 Jeanvoine Apr 2005 B1
6918256 Gutmark et al. Jul 2005 B2
7027467 Baev et al. Apr 2006 B2
7116888 Aitken et al. Oct 2006 B1
7134300 Hayes et al. Nov 2006 B2
7168395 Engdahl Jan 2007 B2
7175423 Pisano et al. Feb 2007 B1
7231788 Karetta et al. Jun 2007 B2
7273583 Rue et al. Sep 2007 B2
7330634 Aitken et al. Feb 2008 B2
7383698 Ichinose et al. Jun 2008 B2
7392668 Adams et al. Jul 2008 B2
7428827 Maugendre et al. Sep 2008 B2
7441686 Odajima et al. Oct 2008 B2
7448231 Jeanvoine et al. Nov 2008 B2
7454925 DeAngelis et al. Nov 2008 B2
7509819 Baker et al. Mar 2009 B2
7565819 Jeanvoine et al. Jul 2009 B2
7578988 Jacques et al. Aug 2009 B2
7581948 Borders et al. Sep 2009 B2
7622677 Barberree et al. Nov 2009 B2
7624595 Jeanvoine et al. Dec 2009 B2
7748592 Koga et al. Jul 2010 B2
7767606 McGinnis et al. Aug 2010 B2
7778290 Sacks et al. Aug 2010 B2
7781562 Crawford et al. Aug 2010 B2
7802452 Borders et al. Sep 2010 B2
7832365 Hannum et al. Nov 2010 B2
7845314 Smith Dec 2010 B2
7855267 Crawford et al. Dec 2010 B2
7946136 Watkinson May 2011 B2
8033254 Hannum et al. Oct 2011 B2
8279899 Kitabayashi Oct 2012 B2
8285411 Hull et al. Oct 2012 B2
8402787 Pernode et al. Mar 2013 B2
8424342 Kiefer et al. Apr 2013 B2
8487262 Damm et al. Jul 2013 B2
8650914 Charbonneau Feb 2014 B2
8707739 Huber et al. Apr 2014 B2
8707740 Huber et al. Apr 2014 B2
8769992 Huber Jul 2014 B2
8875544 Charbonneau Nov 2014 B2
8973400 Charbonneau et al. Mar 2015 B2
8973405 Charbonneau et al. Mar 2015 B2
8991215 Shock et al. Mar 2015 B2
8997525 Shock et al. Apr 2015 B2
9021838 Charbonneau et al. May 2015 B2
9032760 Charbonneau et al. May 2015 B2
9096452 Charbonneau et al. Aug 2015 B2
9096453 Charbonneau Aug 2015 B2
20010039813 Simpson et al. Nov 2001 A1
20020086077 Noller et al. Jul 2002 A1
20020124598 Borysowicz et al. Sep 2002 A1
20020134112 Barrow et al. Sep 2002 A1
20020152770 Becher et al. Oct 2002 A1
20020162358 Jeanvoine et al. Nov 2002 A1
20020166343 LeBlanc Nov 2002 A1
20030000250 Arechaga et al. Jan 2003 A1
20030015000 Hayes et al. Jan 2003 A1
20030029197 Jeanvoine et al. Feb 2003 A1
20030037571 Kobayashi et al. Feb 2003 A1
20040025569 Damm et al. Feb 2004 A1
20040099009 Linz et al. May 2004 A1
20040128098 Neuhaus et al. Jul 2004 A1
20040131988 Baker et al. Jul 2004 A1
20040168474 Jeanvoine et al. Sep 2004 A1
20040224833 Jeanvoine et al. Nov 2004 A1
20050039491 Maugendre et al. Feb 2005 A1
20050061030 Ichinose et al. Mar 2005 A1
20050083989 Leister et al. Apr 2005 A1
20050103323 Engdal May 2005 A1
20050236747 Rue et al. Oct 2005 A1
20060000239 Jeanvoine et al. Jan 2006 A1
20060101859 Takagi et al. May 2006 A1
20060122450 Kim et al. Jun 2006 A1
20060144089 Eichholz et al. Jul 2006 A1
20060162387 Schmitt et al. Jul 2006 A1
20060174655 Kobayashi et al. Aug 2006 A1
20060177785 Varagani et al. Aug 2006 A1
20060233512 Aitken et al. Oct 2006 A1
20060257097 Aitken et al. Nov 2006 A1
20060287482 Crawford et al. Dec 2006 A1
20060293494 Crawford et al. Dec 2006 A1
20060293495 Crawford et al. Dec 2006 A1
20070051136 Watkinson Mar 2007 A1
20070106054 Crawford et al. May 2007 A1
20070122332 Jacques et al. May 2007 A1
20070130994 Boratav et al. Jun 2007 A1
20070137259 Borders et al. Jun 2007 A1
20070212546 Jeanvoine et al. Sep 2007 A1
20070220922 Bauer et al. Sep 2007 A1
20070266737 Rodek et al. Nov 2007 A1
20070278404 Spanke et al. Dec 2007 A1
20080035078 Li Feb 2008 A1
20080227615 McGinnis et al. Sep 2008 A1
20080256981 Jacques et al. Oct 2008 A1
20080276652 Bauer et al. Nov 2008 A1
20080278404 Blalock et al. Nov 2008 A1
20080293857 Crawford et al. Nov 2008 A1
20080302136 Bauer et al. Dec 2008 A1
20090042709 Jeanvoine et al. Feb 2009 A1
20090044568 Lewis Feb 2009 A1
20090120133 Fraley et al. May 2009 A1
20090176639 Jacques et al. Jul 2009 A1
20090220899 Spangelo et al. Sep 2009 A1
20090235695 Pierrot et al. Sep 2009 A1
20090320525 Johnson Dec 2009 A1
20100064732 Jeanvoine et al. Mar 2010 A1
20100087574 Crawford et al. Apr 2010 A1
20100089383 Cowles Apr 2010 A1
20100120979 Crawford et al. May 2010 A1
20100139325 Watkinson Jun 2010 A1
20100143601 Hawtof et al. Jun 2010 A1
20100162757 Brodie Jul 2010 A1
20100227971 Crawford et al. Sep 2010 A1
20100236323 D'Angelico et al. Sep 2010 A1
20100242543 Ritter et al. Sep 2010 A1
20100300153 Zhang et al. Dec 2010 A1
20100304314 Rouchy et al. Dec 2010 A1
20100307196 Richardson Dec 2010 A1
20100313604 Watson et al. Dec 2010 A1
20100319404 Borders et al. Dec 2010 A1
20100326137 Rouchy et al. Dec 2010 A1
20110016922 Kitamura et al. Jan 2011 A1
20110048125 Jackson et al. Mar 2011 A1
20110054091 Crawford et al. Mar 2011 A1
20110061642 Rouchy et al. Mar 2011 A1
20110088432 Purnode et al. Apr 2011 A1
20110107670 Galley et al. May 2011 A1
20110236846 Rue et al. Sep 2011 A1
20110308280 Huber Dec 2011 A1
20120033792 Kulik et al. Feb 2012 A1
20120077135 Charbonneau Mar 2012 A1
20120104306 Kamiya et al. May 2012 A1
20120216567 Boughton et al. Aug 2012 A1
20120216568 Fisher et al. Aug 2012 A1
20120216576 Boughton et al. Aug 2012 A1
20130072371 Jansen et al. Mar 2013 A1
20130086944 Shock et al. Apr 2013 A1
20130086949 Charbonneau Apr 2013 A1
20130086950 Huber et al. Apr 2013 A1
20130086951 Charbonneau et al. Apr 2013 A1
20130086952 Charbonneau et al. Apr 2013 A1
20130123990 Kulik et al. May 2013 A1
20130279532 Ohmstede et al. Oct 2013 A1
20130283861 Mobley et al. Oct 2013 A1
20130327092 Charbonneau Dec 2013 A1
20140090421 Shock et al. Apr 2014 A1
20140090422 Charbonneau et al. Apr 2014 A1
20140090423 Charbonneau et al. Apr 2014 A1
20140144185 Shock et al. May 2014 A1
20160116214 Kirschen Apr 2016 A1
Foreign Referenced Citations (47)
Number Date Country
254 502 May 1948 CH
10 38 721 Sep 1958 DE
11 05 116 Apr 1961 DE
36 29 965 Mar 1988 DE
40 00 358 Mar 1993 DE
44 24 814 Jan 1996 DE
196 19 919 Aug 1997 DE
100 29 983 Jan 2002 DE
100 29 983 Sep 2003 DE
10 2005 033330 Aug 2006 DE
0 181 248 Oct 1989 EP
1 337 789 Dec 2004 EP
1 990 321 Nov 2008 EP
2 133 315 Dec 2009 EP
2 138 465 Dec 2009 EP
1 986 966 Apr 2010 EP
1 667 934 Feb 2011 EP
2 397 446 Dec 2011 EP
2 404 880 Jan 2012 EP
2 433 911 Mar 2012 EP
2 578 548 Apr 2013 EP
2 740 860 Sep 1997 FR
191301772 Jan 1914 GB
191407633 Mar 1914 GB
164073 May 1921 GB
250 536 Jul 1926 GB
959 895 Jun 1964 GB
1449439 Sep 1976 GB
1 514 317 Jun 1978 GB
2 424 644 Oct 2006 GB
1208172 Jul 1989 IT
S58 199728 Nov 1983 JP
H08 290918 Nov 1996 JP
2000 0050572 Aug 2000 KR
100465272 Dec 2004 KR
114827 Jul 1999 RO
986873 Jul 1983 SU
1998055411 Dec 1998 WO
2008103291 Aug 2008 WO
2009091558 Jul 2009 WO
2010011701 Jan 2010 WO
2010045196 Apr 2010 WO
2012048790 Apr 2012 WO
2012125665 Sep 2012 WO
2013 162986 Oct 2013 WO
2013 188082 Dec 2013 WO
2013188167 Dec 2013 WO
Non-Patent Literature Citations (28)
Entry
JP 58-199728 A (Suzuki) Nov. 21, 1983 (English language translation). Translated Jul. 2015 by Phoenix Translations. (Year: 1983).
“Gamma Irradiators for Radiation Processing” Booklet, International Atomic Energy Agency, Vienna, Austria.
Furman, BJ, ME 120 Experimental Methods Vibration Measurement, San Jose University Department of Mechanical and Aerospace Engineering.
Higley, BA, Glass Melter System Technologies for Vitrification of High-Sodium Content Low-Level, Radioactive, Liquid Wastes—Phase I: SBS Demonstration With Simulated Low-Level Waste—Final Test Report, Westinghouse Hanford Company.
Report for Treating Hanford LAW and WTP SW Simulants: Pilot Plant Mineralizing Flowsheet Apr. 2009, Department of Energy Environmental Management Consolidated Business Center by THOR Treatment Technologies, LLC.
Gerber, J., “Les Densimetres Industriels,” Petrole et Techniques, Association Francaise des Techniciens du Petrole, Jun. 1, 1989, pp. 26-27, No. 349, Paris, France.
Rue et al, “Submerged Combustion Melting of Glass,” International Journal of Applied Glass Science, Nov. 9, 2011, pp. 262-274, vol. 2, No. 4.
National Laboratory; US DOE Contract No. DE-AC09-08SR22470, Oct. 2011.
“AccuTru Temperature Measurement,” AccuTru International Corporation, 2003.
“Glass Technologies—The Legacy of a Successful Public-Private Partnership”, 2007, U.S. Department of Energy, pp. 1-32.
“Glass Melting Technology—A Technical and Economic Assessment,” 2004, U.S. Department of Energy, pp. 1-292.
Muijsenberg, H. P. H., Neff, G., Muller, J., Chmelar, J., Bodi, R. and Matustikj, F. (2008) “An Advanced Control System to Increase Glass Quality and Glass Production Yields Based on GS ESLLI Technology”, in A Collection of Papers Presented at the 66th Conference on Glass Problems: Ceramic Engineering and Science Proceedings, vol. 27, Issue 1 (ed W. M. Kriven), John Wiley & Sons, Inc., Hoboken, NJ, USA. doi: 10.1002/9780470291306.ch3.
Rue, “Energy-Efficient Glass Melting—The Next Generation Melter”, Gas Technology Institute, Project No. 20621 Final Report (2008).
Muijsenberg, E., Eisenga, M. and Buchmayer, J. (2010) “Increase of Glass Production Efficiency and Energy Efficiency with Model-Based Predictive Control”, in 70th Conference on Glass Problems: Ceramic Engineering and Science Proceedings, vol. 31, Issue 1 (ed C. H. Drummond), John Wiley & Sons, Inc., Hoboken, NJ, USA. doi: 10.1002/9780470769843.ch15.
Sims, Richard, “Batch charging technologies—a review”, www.glassonweb.com, Nikolaus Sorg Gmbh & Co KG (May 2011).
“Canty Process Technology” brochure, date unknown, copy received in Apr. 2012 at American Institute of Chemical Engineers, Spring Meeting, Houston, TX.
“Glass Melting”, Battelle PNNL MST Handbook, U.S. Department of Energy, Pacific Northwest Laboratory, retrieved from the Internet Apr. 20, 2012.
“Roll Compaction”, brochure from The Fitzpatrick Company, Elmhurst, Illinois, retrieved from the Internet Apr. 20, 2012.
“Glass Industry of the Future”, United States Department of Energy, report 02-GA50113-03, pp. 1-17, Sep. 30, 2008.
Stevenson, “Foam Engineering: Fundamentals and Applications”, Chapter 16, pp. 336-389, John Wiley & Sons (Mar. 13, 2012).
Clare et al., “Density and Surface Tension of Borate Containing Silicate Melts”, Glass Technology—European Journal of Glass Science and Technology, Part A, pp. 59-62, vol. 44, No. 2, Apr. 1, 2003.
Seward, T.P., “Modeling of Glass Making Processes for Improved Efficiency”, DE-FG07-96EE41262, Final Report, Mar. 31, 2003.
Conradt et al, Foaming behavior on glass melts, Glastechniche Berichte 60 (1987) Nr. 6, S. 189-201 Abstract Fraunhofer ISC.
Kim et al., “Foaming in Glass Melts Produced by Sodium Sulfate Decomposition under Isothermal Conditions”, Journal of the American Ceramic Society, 74(3), pp. 551-555, 1991.
Kim et al., “Foaming in Glass Melts Produced by Sodium Sulfate Decomposition under Ramp Heating Conditions”, Journal of the American Ceramic Society, 75(11), pp. 2959-2963, 1992.
Kim et al., “Effect of Furnace Atmosphere on E-glass Foaming”, Journal of Non-Crystalline Solids, 352(50/51), pp. 5287-5295, 2006.
Van Limpt et al., “Modelling the evaporation of boron species. Part 1. Alkali-free borosilicate glass melts”, Glass Technology—European Journal of Glass Science and Technology, Part. A, 52(3): pp. 77-87, 2011.
Olabin, V.M. et al, “Submerged Combustion Furnace for Glass Melts,” Ceramic Engineering and Science Proceedings, Jan. 1, 1996, pp. 84-92, vol. 17—No. 2, American Ceramic Society Inc., US.
Related Publications (1)
Number Date Country
20170073262 A1 Mar 2017 US
Divisions (1)
Number Date Country
Parent 13633979 Oct 2012 US
Child 15358286 US