WO2011036939A1 - Dispositif de fabrication de verre fondu, procédé de fabrication de verre fondu, et procédé de fabrication de verre en feuille à l'aide dudit dispositif et procédé - Google Patents

Dispositif de fabrication de verre fondu, procédé de fabrication de verre fondu, et procédé de fabrication de verre en feuille à l'aide dudit dispositif et procédé Download PDF

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Publication number
WO2011036939A1
WO2011036939A1 PCT/JP2010/062444 JP2010062444W WO2011036939A1 WO 2011036939 A1 WO2011036939 A1 WO 2011036939A1 JP 2010062444 W JP2010062444 W JP 2010062444W WO 2011036939 A1 WO2011036939 A1 WO 2011036939A1
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Prior art keywords
molten glass
bubbler
row
bubblers
glass
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PCT/JP2010/062444
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English (en)
Japanese (ja)
Inventor
亮介 赤木
敦 市川
肇 伊藤
宏 等々力
Original Assignee
旭硝子株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Application filed by 旭硝子株式会社 filed Critical 旭硝子株式会社
Priority to KR1020127007567A priority Critical patent/KR101453629B1/ko
Priority to JP2011532932A priority patent/JP5549674B2/ja
Priority to CN201080042588.7A priority patent/CN102574719B/zh
Publication of WO2011036939A1 publication Critical patent/WO2011036939A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/18—Stirring devices; Homogenisation
    • C03B5/193—Stirring devices; Homogenisation using gas, e.g. bubblers
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/18—Stirring devices; Homogenisation
    • C03B5/183—Stirring devices; Homogenisation using thermal means, e.g. for creating convection currents
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/235—Heating the glass
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/42—Details of construction of furnace walls, e.g. to prevent corrosion; Use of materials for furnace walls
    • C03B5/43—Use of materials for furnace walls, e.g. fire-bricks

Definitions

  • the present invention relates to a molten glass production apparatus, a molten glass production method, and a plate glass production method using them. More specifically, the present invention relates to a molten glass manufacturing apparatus, a molten glass manufacturing method, and a plate glass manufacturing method using them for producing high-quality alkali-free glass with high homogeneity.
  • alkali-free glass that does not substantially contain alkali metal ions in order to increase the insulating properties of the glass substrate.
  • alkali-free glass is preferable for the production of a glass substrate for FPD because it has a small coefficient of thermal expansion.
  • the melting furnace described in Patent Document 1 the melting furnace is divided into an upstream zone and a downstream zone by a transverse sill, and a molten glass circulation flow (upstream circulation flow, downstream circulation flow) is formed in each zone. , Melting raw materials and homogenizing molten glass. More specifically, the glass raw material is melted by forming an upstream circulation flow in the upstream zone, and the molten glass is homogenized by forming a downstream circulation flow in the downstream zone.
  • a bubbler is provided on the upstream side of the crossing sill in order to control the upstream circulation flow and the downstream circulation flow.
  • the melting furnace (melting tank) described in Patent Document 2 does not have a structure corresponding to the transverse sill in the melting furnace described in Patent Document 1, but includes at least one row of bubblers and at least two opposite burners. It describes using glass to melt and clarify.
  • the melting furnaces described in Patent Documents 1 and 2 are not necessarily suitable for producing high-quality alkali-free glass.
  • T ⁇ As an index of the melting temperature of glass, T ⁇ , that is, a temperature at which the glass viscosity ⁇ becomes 10 2 [dPa ⁇ S] is used, but non-alkali glass has a T ⁇ of 1500 to 1760 ° C.
  • alkali-containing glass such as lime glass
  • T ⁇ is 100 ° C. or higher, and homogenization is difficult. For this reason, it cannot be sufficiently homogenized in a melting furnace having a layout for general mass production such as soda lime glass described in Patent Documents 1 and 2, and glass products (for FPDs) that require particularly high homogeneity. It was not necessarily suitable for the production of glass substrates and the like.
  • the alkali-free glass has a higher T ⁇ than the alkali-containing glass such as soda lime glass, and therefore the temperature of the molten glass in the melting furnace inevitably increases. If the temperature of the molten glass is high, the erosion action of the molten glass on the in-furnace structure is enhanced accordingly. Therefore, in the case of non-alkali glass, there is a step that affects the flow of the molten glass at the bottom of the melting furnace, such as a crossing threshold in the melting furnace described in Patent Document 1 and a fining table in the melting furnace described in Patent Document 2. Then, the erosion of the level
  • the present invention provides a molten glass manufacturing apparatus, a molten glass manufacturing method, and a plate glass using them, which are suitable for producing high-quality non-alkali glass with high homogeneity
  • An object is to provide a manufacturing method.
  • the present invention has been made on the basis of the above findings by the inventors of the present invention, and is used for producing a molten glass having a temperature T ⁇ of 1500 to 1760 ° C. at which the glass viscosity ⁇ is 10 2 [dPa ⁇ S].
  • the molten glass manufacturing apparatus has a melting tank for melting the glass raw material, A plurality of first bubblers and a plurality of second bubblers over the width direction of the molten glass flow path in the vicinity of the bottom surface of the melting tank;
  • the first bubbler is provided on the upstream side of the molten glass flow path from the second bubbler,
  • the dissolution tank has a burner for heating the upper space of the dissolution tank,
  • the distance from the downstream end of the molten glass flow path to the second bubbler row is 0.45L F to 0.55L F
  • the distance L between the first bubbler row and the second bubbler row P is 500 to 1000 mm
  • a distance L B1 between the row of the first bubblers and the burner closest to the upstream side of the row in the flow direction of the molten glass in the melting tank is 0 to 2000 mm
  • a distance L B2 between the second bubbler row and the burner closest to the downstream side of the row in the flow direction of the molten glass in the melting tank is 800 to 2500 mm
  • the molten glass manufacturing apparatus characterized by it being LB2 > LB1 is provided.
  • the present invention is also a method for producing molten glass using the above-described molten glass production apparatus, wherein the average flow rate of the gas supplied from the first bubbler is V 1 [liter / minute], and the first The average flow rate of the gas supplied from the second bubbler is V 2 [liter / min], the ambient temperature above the first bubbler is T 1 [° C.], and the ambient temperature above the second bubbler is Provided is a molten glass production method for producing molten glass under the conditions of V 1 > V 2 and T 1 > T 2 when T 2 [° C.] is satisfied.
  • the present invention also provides a plate glass manufacturing method for forming molten glass obtained by the above-described molten glass manufacturing method of the present invention into plate glass.
  • the molten glass manufacturing apparatus and molten glass manufacturing method of the present invention are suitable for the production of high-quality alkali-free glass with high homogeneity. Since the plate glass manufacturing method of this invention can manufacture plate glass with high homogeneity and high transparency, it is suitable for manufacture of the board
  • FIG. 1 is a cross-sectional view of an embodiment of a melting tank in the molten glass production apparatus of the present invention.
  • FIG. 2 is a plan view of the dissolution tank 10 shown in FIG. However, the upper wall surface of the dissolution tank 10 is omitted.
  • T ⁇ is used as an index of the melting temperature of glass.
  • the glass targeted by the present invention has a T ⁇ of 1500 to 1760 ° C., which is 100 ° C. or more higher than the T ⁇ of general alkali-containing glass such as soda lime glass, so it is difficult to homogenize the molten glass.
  • the molten glass manufacturing apparatus and the molten glass manufacturing method of the present invention are suitable for homogenizing such molten glass.
  • a specific example of the glass having a T ⁇ of 1500 to 1760 ° C. is particularly alkali-free glass. From this point, the molten glass production apparatus and the molten glass production method of the present invention produce a predetermined amount (20 to 100 tons / day) of glass products with strict quality requirements, such as glass substrates for FPD. Suitable for
  • FIG. 1 is a cross-sectional view of one embodiment of a melting tank in the molten glass production apparatus of the present invention
  • FIG. 2 is a plan view of the melting tank shown in FIG.
  • a glass raw material inlet 11 is provided at the upstream end of the melting tank 10.
  • the glass raw material charged from the charging port 11 is melted by heating by the burner 15 to become molten glass G, and is held in the melting tank 10.
  • a discharge port 12 for discharging the molten glass G to the next process is provided at the downstream end of the melting tank 10.
  • the discharge port 12 communicates with the downstream conduit 20.
  • a plurality of first bubblers 13 and a plurality of second bubblers 14 are provided in the vicinity of the bottom surface of the dissolution tank 10 shown in FIGS.
  • the plurality of first bubblers 13 and the plurality of second bubblers 14 have a predetermined interval (pitch) over the width direction of the melting tank 10, more specifically, the width direction of the molten glass flow path of the melting tank 10. ) Is opened.
  • the first bubbler 13 is provided upstream of the second bubbler 14 in the molten glass flow path, and a predetermined interval is provided between the first bubbler 13 row and the second bubbler 14 row. Is provided.
  • the preferred range of the pitches of the individual bubblers in the row direction of the first bubbler 13 and the second bubbler 14 and the distance between the row of the first bubblers 13 and the row of the second bubblers 14 is as follows. It will be described later.
  • burners 15 are arranged on both sides of the melting tank 10 so as to be positioned above the molten glass G held in the melting tank 10.
  • the burners 15 are provided at equal intervals over the entire length of the dissolution tank 10 except for an exception part to be described later.
  • the melting tank 10 in the molten glass manufacturing apparatus of the present invention has Patent Documents 1 and 2 at the bottom of the molten glass channel by arranging the first and second bubblers 13 and 14 and the burner 15 in a specific arrangement described later. Formation of a circulating flow of the molten glass G (upstream circulating flow 100, downstream circulating flow 101) in the melting tank 10 without providing a step structure that affects the molten glass flow as described in FIG. Further, the flow rate of the upstream circulating flow 100 and the flow rate of the downstream circulating flow 101 can be controlled to have a predetermined relationship.
  • the melting tank 10 in the molten glass production apparatus of the present invention is suitable for producing glass having a T ⁇ of 1500 to 1760 ° C. because there is no step structure that causes erosion by the molten glass at the bottom of the molten glass flow path. is there.
  • the melting tank 10 in the molten glass production apparatus of the present invention is a distance from the upstream end of the molten glass flow path to the first bubbler 13 row when the length of the molten glass flow path of the melting tank 10 is L F.
  • L F length of the molten glass flow path of the melting tank 10
  • a distance from the downstream end of the molten glass flow path to the row of the second bubbler 14 is 0.45L F ⁇ 0.55L F. Therefore, compared with the conventional melting tank (melting furnace) as described in Patent Documents 1 and 2, the length of the melting tank 10 is short, and the length of the part forming the downstream circulating flow in the melting tank is also short. .
  • the length L F of the molten glass channel of the melting tank 10 of the present invention varies depending on the width of the molten glass channel, but is preferably 10 to 30 m, more preferably 10 to 25 m, and even more preferably 15 to 22 m.
  • the width of the molten glass channel is preferably 5 to 10 m, more preferably 5.5 to 9 m, and still more preferably 6.5 to 8 m.
  • the flow rates of the gases 16 and 17 from the first bubbler 13 and the second bubbler 14 are set to a specific relationship described later, and the burner 15 is set to a specific arrangement described later.
  • the flow rate of the upstream circulating flow 100 and the flow rate of the downstream circulating flow 101 have a predetermined relationship. Can be controlled.
  • T ⁇ 1500 to 1760 ° C.
  • the gas 16 and 17 supplied from the first bubbler 13 and the second bubbler 14 should use molten glass G and those that do not adversely affect the components of the melting tank 10 such as the bubblers 13 and 14. Is preferred. Specific examples of such a gas include air, nitrogen, oxygen, helium, and argon.
  • the material of the bubblers 13, 14 it is preferable to use a gas that does not contain oxygen, such as nitrogen, helium, and argon, as the gases 16, 17 supplied from the bubbler 13, the bubbler 14. .
  • nitrogen is particularly preferred.
  • the distance from the upstream end of the molten glass flow path to the row of the first bubblers 13 is preferably 0.43L F to 0.46L F , and the second end from the downstream end of the molten glass flow path.
  • the distance to the row of bubblers 14 is preferably 0.47L F to 0.54L F.
  • L P is 500 to 1000 mm.
  • L P satisfies the above range, it is excellent in the effect of promoting the formation of a circulating flow of the molten glass G (upstream circulating flow 100, downstream circulating flow 101) in the melting tank 10, and upstream.
  • This is preferable in controlling the flow rate of the side circulation flow 100 and the flow rate of the downstream circulation flow 101 so as to have a predetermined relationship.
  • L P is less than 500 mm, the distance between the row of the first bubblers 13 and the row of the second bubblers 14 is too close, so the circulating flow of the molten glass G in the melting tank 10 (upstream circulating flow 100 In addition, the effect of promoting the formation of the downstream circulation flow 101) is poor, and it is difficult to control the flow rate of the upstream circulation flow 100 and the flow rate of the downstream circulation flow 101 to have a predetermined relationship.
  • L P is preferably 600 to 800 mm.
  • the pitch p between the individual bubblers in the row direction of the bubblers that is, the distance between the individual bubblers in the width direction of the molten glass flow path of the melting tank 10 is 400 to It is preferable that it is 700 mm. If the pitch p between the individual bubblers is in the above range, it is excellent in the effect of promoting the formation of a circulating flow (upstream circulating flow 100, downstream circulating flow 101) of the molten glass G in the melting tank 10, and upstream. This is preferable for controlling the flow rate of the side circulation flow 100 and the flow rate of the downstream circulation flow 101 so as to have a predetermined relationship, and is excellent in terms of manufacturing cost.
  • the pitch p between the individual bubblers exceeds 700 mm, the distance between the individual bubblers is too wide, so that the molten glass G circulating flow (upstream circulating flow 100, downstream circulating flow 101) in the melting tank 10
  • the effect of promoting the formation may be insufficient.
  • a difference occurs in the acceleration, and the flow rate of the circulating flow may be uneven, which is not preferable from the viewpoint of homogenizing the molten glass G.
  • the flow rate of the upstream circulation flow 100 and the flow rate of the downstream circulation flow 101 may be difficult to control the flow rate of the upstream circulation flow 100 and the flow rate of the downstream circulation flow 101 so as to have a predetermined relationship.
  • the pitch p between individual bubblers is less than 400 mm, it no longer contributes to the promotion of the formation of the circulating flow of the molten glass G (upstream circulating flow 100, downstream circulating flow 101) in the melting tank 10. Rather, from the viewpoint of cost effectiveness, the number of the first and second bubblers 13 and 14 provided in the melting tank 10 becomes excessive, which leads to an increase in the manufacturing cost of the molten glass, which is not preferable.
  • the first bubbler 13 and the second bubbler 14 are arranged so as not to be coaxial with respect to the flow direction of the molten glass in the melting tank 10.
  • the protruding ports of the first bubbler 13 and the protruding ports of the second bubbler 14 are arranged in a staggered manner, and the protruding port of the first bubbler 13 and the second bubbler 14 are arranged. There is no coexistence with the protruding port. In such an arrangement, even if one of the protruding ports of the first bubbler 13 stops functioning, due to the presence of the protruding ports of the second bubbler 14 arranged in a staggered manner downstream.
  • the effect of promoting the formation of the circulating flow of the molten glass G (upstream circulating flow 100, downstream circulating flow 101) in the melting tank 10 is not impaired, and the flow rate and the downstream of the upstream circulating flow 100 are not impaired.
  • the flow rate of the side circulation flow 101 can be controlled to have a predetermined relationship.
  • Burners 15 are provided at equal intervals over the entire length of the dissolution tank 10 on both sides of the dissolution tank 10 shown in FIGS. However, the burner 15 is not provided above the second bubbler 14. As will be described in detail later, in the present invention, the average flow rate V 2 of the gas 17 supplied from the second bubbler 14 is made smaller than the average flow rate V 1 of the gas 16 supplied from the first bubbler 13 (control 1). ) And lowering the ambient temperature T 2 above the second bubbler 14 to be lower than the ambient temperature T 1 above the first bubbler 13 (control 2), the unit of the downstream circulating flow 101 per unit time It is possible to control the flow rate of the upstream circulating flow 100 and the downstream circulating flow 101 so as to have a predetermined relationship by decreasing the flow rate. Thereby, when producing a molten glass having a T ⁇ of 1500 to 1760 ° C., homogenization of the molten glass can be promoted, and a high-quality molten glass with high homogeneity can be obtained.
  • the atmospheric temperature T 2 above the second bubbler can be made lower than the atmospheric temperature T 1 above the first bubbler.
  • L B2 ⁇ L B1 ⁇ 300 mm is preferable
  • L B2 ⁇ L B1 ⁇ 500 mm is more preferable
  • L B2 ⁇ L B1 ⁇ 800 mm is further preferable.
  • the burner 15 is provided above the row of the first bubblers 13, but as long as the relationship of L B2 > L B1 is satisfied,
  • the nearest burner 15 may be arranged some distance away from the upstream side of the row.
  • the ambient temperature above the first bubbler 13 becomes too low and the upstream side circulation flow 100 becomes weak, and the glass Problems such as insufficient melting of the raw materials and insufficient homogenization of the molten glass G in the downstream region of the melting tank 10 occur.
  • L B1 500 to 1500 mm is preferable.
  • the pitch between adjacent burners 15 is preferably 600 to 2600 mm, and more preferably 800 to 2400 mm, although it depends on the type of burner 15 and the layout of the dissolution tank 10.
  • Combustion in the burner 15 can be performed by mixing the fuel with oxygen gas and burning it, or mixing the fuel with oxygen gas and air and burning it. By using these methods, moisture can be contained in the molten glass.
  • the molten glass In the post-process of the molten glass sent from the melting tank 10 to the downstream conduit 20, when the bubbles in the molten glass are defoamed by vacuum degassing, the molten glass preferably contains moisture. Therefore, the combustion as described above is preferable.
  • the constituent material of the melting tank 10 in contact with the molten glass G is required to be excellent in heat resistance and corrosion resistance to the molten glass. Therefore, a refractory brick containing ZrO 2 is used. of the bottom surface of the dissolving tank 10, in a portion of the 0.1 L F ⁇ 0.3 L F to the upstream side from the row of first bubbler 13, ZrO 2 is not more than 97% 85% by mass%, the balance being SiO It is preferable to use a glassy hot-melt refractory mainly composed of 2 .
  • each hot-melt refractory is preferably 50 to 120 mm, and two to three hot-melt refractories are preferably laminated. Furthermore, 2 to 5 layers of other refractory bricks containing ZrO 2 can be laminated on the outside of the layer of the hot-melt refractory thus formed. In addition, it is preferable to comprise all the parts which contact
  • each refractory brick can be laminated
  • the molten glass manufacturing method of this invention is demonstrated.
  • the molten glass is manufactured while performing the above controls 1 and 2.
  • the flow rate per unit time of the downstream circulation flow 101 is lowered, and the flow rate of the upstream circulation flow 100 and the flow rate of the downstream circulation flow 101 have a predetermined relationship described later. Can be controlled.
  • V 1 is preferably 0.5 to 20 liters / minute, more preferably 0.7 to 5 liters / minute, and 0.9 to 3 liters / minute. More preferably, it is 1.8 to 2.6 liters / minute.
  • the V 2 is preferably 0.3 to 19.8 liters / minute, more preferably 0.4 to 4.8 liters / minute, and 0.5 to 2 liters / minute. Is more preferable, and 0.9 to 2.0 liter / min is particularly preferable.
  • V 1 ⁇ V 2 ⁇ 0.2 liter / min is preferable, V 1 ⁇ V 2 ⁇ 0.4 liter / min is more preferable, V 1 ⁇ V 2 ⁇ 0.6 liter / min is more preferable, V 1 ⁇ V 2 ⁇ 1.0 l / min is particularly preferred.
  • the T 1 is preferably 1590 to 1710 ° C., more preferably 1600 to 1695 ° C.
  • the T 2 is preferably 1570 to 1690 ° C., more preferably 1580 to 1675 ° C.
  • T 1 -T 2 is preferably 10 to 35 ° C.
  • T 1 -T 2 is more preferably 15 to 30 ° C., and further preferably 19 to 26 ° C.
  • T 1 and T 2 can be measured by the following method. (Measurement position) T 1 : Intermediate position between the burner closest to the upstream side of the first row of bubblers and the latest burner positioned further upstream than the burner.
  • F 1 and F 2 can be measured by the following method.
  • F 2 distance from the downstream end of the molten glass flow path at 0.22L F ⁇ 0.30L F, near the center in the width direction of the molten glass flow path.
  • Video of the flow of bubbles on the surface of the molten glass is taken, and the moving time with respect to the moving distance of the bubbles is measured to obtain the flow velocity. Repeat this procedure 2-3 times to determine the average flow rate.
  • the plate glass manufacturing method of the present invention the molten glass obtained by the above-described molten glass manufacturing method of the present invention is formed into a plate glass.
  • various forming methods such as a float method and a downdraw method can be used. In the case of a glass having a T ⁇ of 1500 to 1760 ° C., the float method is particularly preferable.
  • bubbles in the molten glass may be degassed by vacuum degassing.
  • the plate glass manufacturing method of the present invention since the molten glass having high homogeneity obtained by the molten glass manufacturing method of the present invention is formed into a plate glass, a plate glass having high homogeneity and high transparency can be obtained.
  • the plate glass production apparatus of the present invention can be applied to the production of plate glass for various uses. However, since a plate glass having high homogeneity and high transparency can be obtained, the homogeneity of the glass substrate for FPD can be obtained. It is particularly preferable to apply it to the production of plate glass for applications in which the demands of these are extremely strict.
  • T eta is the production of alkali-free glass of 1500 ⁇ 1760 ° C..
  • Molten glass flow path length L F 16 to 25 m Molten glass channel width: 5.5-9m Distance from the upstream end of the molten glass flow path to the first bubbler 13 row: 0.43L F to 0.46L F Distance from the downstream end of the molten glass flow path to the second bubbler 14 row: 0.47L F to 0.54L F Distance L P between first row of bubblers 13 and second row of bubblers 14: 600 to 800 mm Pitch of individual bubblers 13 and 14 in the row direction of bubblers p: 400 to 700 mm Distance L B1 between the row of first bubblers 13 and the burner 15 nearest to the upstream side of the row in the flow direction of the molten glass in the melting tank: 500 to 1500 mm Distance L B2 between the row of second bubblers 14 and the burner 15 closest to the downstream side of the row in the flow direction of the molten glass in the melting tank: 1000 to 2000 mm L B2 -L B1 ⁇ 500mm Distance between individual burners in the flow direction of the molten glass in the melting tank: 800
  • V 1 1.8 to 2.6 liters / minute
  • V 2 0.9 to 2.0 liters / minute
  • T 1 and T 2 are measured by the method described above.
  • T 1 1590-1710 ° C
  • T 2 1580 to 1675 ° C.
  • T 1 -T 2 10 to 35 ° C
  • the average flow rate F 2 in average flow rate F 1 and the downstream circulation flow 101 of the upstream circulation flow 100 in the dissolution tank 10 is measured by the method described above. The results are as follows.
  • the molten glass production apparatus and molten glass production method of the present invention are suitable for the production of high-quality alkali-free glass with high homogeneity. Moreover, since the plate glass manufacturing method of this invention can manufacture plate glass with high homogeneity and transparency, it is suitable for manufacture of the board
  • Dissolution tank 11 Input port 12: Discharge port 13: First bubbler 14: Second bubbler 15: Burner 16: Gas from the first bubbler 17: Gas from the second bubbler 20: Downstream side Conduit 100: Upstream circulating flow 101: Downstream circulating flow

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  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
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  • Thermal Sciences (AREA)
  • Glass Compositions (AREA)

Abstract

Cette invention concerne un dispositif de fabrication de verre fondu et un procédé de fabrication de verre fondu permettant de fabriquer un verre non alcalin de haute qualité, et un procédé de fabrication de verre en feuille à l'aide dudit dispositif et procédé. Le dispositif de fabrication d'un verre fondu qui a une viscosité (η) de 102 (dPa·S) à une température (Tη) dans la plage de 1500 à 1760˚C ci-décrit comprend un récipient de fusion, ledit récipient de fusion étant pourvu de seconds barboteurs, et de premiers barboteurs placés en amont desdits seconds barboteurs. Dans ledit dispositif de fabrication de verre fondu, si la longueur du trajet d'écoulement du verre fondu du récipient de fusion est LF, la distance entre l'extrémité amont du trajet d'écoulement du verre fondu à la rangée des premiers barboteurs est dans la plage de 0,4 à 0,5 LF, la distance entre l'extrémité aval du trajet d'écoulement du verre fondu à la rangée des seconds barboteurs est dans la plage de 0,45 à 0,55 LF, la distance (LP) entre la rangée des premiers barboteurs et la rangée des seconds barboteurs est dans la plage de 500 à 1000 mm, la distance (LB1) entre la rangée des premiers barboteurs et le brûleur le plus proche de la rangée côté amont de la rangée est dans la plage de 0 à 2000 mm, la distance (LB2) entre la rangée des seconds barboteurs et le brûleur le plus proche de la rangée côté aval de la rangée est dans la plage de 800 à 2500 mm, et LB2 > LB1.
PCT/JP2010/062444 2009-09-24 2010-07-23 Dispositif de fabrication de verre fondu, procédé de fabrication de verre fondu, et procédé de fabrication de verre en feuille à l'aide dudit dispositif et procédé WO2011036939A1 (fr)

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Application Number Priority Date Filing Date Title
KR1020127007567A KR101453629B1 (ko) 2009-09-24 2010-07-23 용융 유리 제조 장치, 용융 유리 제조 방법 및 그것을 사용한 판유리의 제조 방법
JP2011532932A JP5549674B2 (ja) 2009-09-24 2010-07-23 溶融ガラス製造装置、溶融ガラス製造方法およびそれらを用いた板ガラスの製造方法
CN201080042588.7A CN102574719B (zh) 2009-09-24 2010-07-23 熔融玻璃制造装置、熔融玻璃制造方法及使用了该装置和该方法的平板玻璃制造方法

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JP2009219347 2009-09-24
JP2009-219347 2009-09-24

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WO2011036939A1 true WO2011036939A1 (fr) 2011-03-31

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KR (1) KR101453629B1 (fr)
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WO (1) WO2011036939A1 (fr)

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* Cited by examiner, † Cited by third party
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WO2013094313A1 (fr) * 2011-12-19 2013-06-27 旭硝子株式会社 Appareil de production de verre fondu, procédé de production de verre fondu et procédé de production d'une plaque de verre à l'aide desdits appareil et procédé
WO2015033931A1 (fr) * 2013-09-06 2015-03-12 旭硝子株式会社 Procédé de fabrication pour verre fondu et procédé de fabrication pour plaque de verre l'utilisant
JP2016037444A (ja) * 2014-08-05 2016-03-22 興亜硝子株式会社 白色ガラス容器の自動製瓶装置

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105601087B (zh) * 2016-03-22 2018-07-10 株洲醴陵旗滨玻璃有限公司 一种浮法玻璃生产中的鼓泡熔化方法
CN106477852A (zh) 2016-09-21 2017-03-08 巨石集团有限公司 一种窑炉鼓泡排布结构

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5218715A (en) * 1975-08-04 1977-02-12 Nippon Electric Glass Co Method of homogenizing glass
JPH07144923A (ja) * 1993-08-13 1995-06-06 Beteiligungen Sorg Gmbh & Co Kg ガラスを溶解する方法及びタンク炉
WO2009005067A1 (fr) * 2007-07-02 2009-01-08 Asahi Glass Co., Ltd. Four de fusion de verre et procédé de fabrication d'un produit de verre

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3928014A (en) * 1974-04-29 1975-12-23 Ppg Industries Inc Method for producing flat glass
US20060174655A1 (en) * 2003-04-15 2006-08-10 Hisashi Kobayashi Process of fining glassmelts using helium bubblles
JP4941872B2 (ja) * 2003-09-02 2012-05-30 日本電気硝子株式会社 液晶ディスプレイ用透明無アルカリガラス基板

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5218715A (en) * 1975-08-04 1977-02-12 Nippon Electric Glass Co Method of homogenizing glass
JPH07144923A (ja) * 1993-08-13 1995-06-06 Beteiligungen Sorg Gmbh & Co Kg ガラスを溶解する方法及びタンク炉
WO2009005067A1 (fr) * 2007-07-02 2009-01-08 Asahi Glass Co., Ltd. Four de fusion de verre et procédé de fabrication d'un produit de verre

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013094313A1 (fr) * 2011-12-19 2013-06-27 旭硝子株式会社 Appareil de production de verre fondu, procédé de production de verre fondu et procédé de production d'une plaque de verre à l'aide desdits appareil et procédé
KR20140107233A (ko) 2011-12-19 2014-09-04 아사히 가라스 가부시키가이샤 용융 유리 제조 장치, 용융 유리 제조 방법 및 그것들을 사용한 판유리의 제조 방법
JPWO2013094313A1 (ja) * 2011-12-19 2015-04-27 旭硝子株式会社 溶融ガラス製造装置、溶融ガラス製造方法およびそれらを用いた板ガラスの製造方法
KR101971755B1 (ko) * 2011-12-19 2019-04-23 에이지씨 가부시키가이샤 용융 유리 제조 장치, 용융 유리 제조 방법 및 그것들을 사용한 판유리의 제조 방법
WO2015033931A1 (fr) * 2013-09-06 2015-03-12 旭硝子株式会社 Procédé de fabrication pour verre fondu et procédé de fabrication pour plaque de verre l'utilisant
JPWO2015033931A1 (ja) * 2013-09-06 2017-03-02 旭硝子株式会社 溶融ガラス製造方法およびそれを用いた板ガラスの製造方法
JP2016037444A (ja) * 2014-08-05 2016-03-22 興亜硝子株式会社 白色ガラス容器の自動製瓶装置

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KR20120086691A (ko) 2012-08-03
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CN102574719B (zh) 2014-07-09
CN102574719A (zh) 2012-07-11

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