[go: up one dir, main page]

WO2011136086A1 - Four de fusion du verre et procédé afférent - Google Patents

Four de fusion du verre et procédé afférent Download PDF

Info

Publication number
WO2011136086A1
WO2011136086A1 PCT/JP2011/059621 JP2011059621W WO2011136086A1 WO 2011136086 A1 WO2011136086 A1 WO 2011136086A1 JP 2011059621 W JP2011059621 W JP 2011059621W WO 2011136086 A1 WO2011136086 A1 WO 2011136086A1
Authority
WO
WIPO (PCT)
Prior art keywords
glass
burners
melting
melting chamber
burner
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/JP2011/059621
Other languages
English (en)
Japanese (ja)
Inventor
英樹 櫛谷
敦 市川
元之 広瀬
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
AGC Inc
Original Assignee
Asahi Glass Co Ltd
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.)
Filing date
Publication date
Application filed by Asahi Glass Co Ltd filed Critical Asahi Glass Co Ltd
Priority to KR1020127028072A priority Critical patent/KR101453639B1/ko
Priority to CN201180021090.7A priority patent/CN102858697B/zh
Priority to JP2012512791A priority patent/JP5598541B2/ja
Publication of WO2011136086A1 publication Critical patent/WO2011136086A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • 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
    • C03B5/2353—Heating the glass by combustion with pure oxygen or oxygen-enriched air, e.g. using oxy-fuel burners or oxygen lances
    • 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
    • C03B5/04—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture in tank furnaces
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/50—Glass production, e.g. reusing waste heat during processing or shaping

Definitions

  • the present invention relates to a glass melting furnace for melting a glass raw material and a glass melting method.
  • a method for producing a glass product includes a melting step for melting a glass raw material to obtain a molten glass, a clarification step for clarifying the molten glass by removing bubbles of the molten glass, and a predetermined molten glass after clarification. And a molding step of molding into the shape.
  • the melting step is a step in which a plurality of types of raw materials are weighed and mixed in accordance with the composition of the glass product, put into a melting furnace, heated to a temperature corresponding to the type of glass and melted. is there.
  • the melting furnace has a raw material inlet on the front wall of the melting chamber for melting the glass raw material, an outlet on the rear wall of the melting chamber, and a plurality of burners on the side wall of the flow path from the raw material inlet to the outlet.
  • a plurality of burners jets a flame into the melting chamber to heat and melt the glass in the melting chamber.
  • the burner ejects a flame in which fuel such as natural gas or heavy oil is mixed with gas and burned.
  • either air or oxygen gas is used as the gas mixed with the fuel.
  • nitrogen gas occupying about 78% by volume of air is exhausted outside the furnace without contributing to combustion.
  • oxyfuel combustion using oxygen gas since the amount of exhaust is small compared to the case of air combustion, the thermal efficiency is high, and the amount of CO 2 emission and NO x emission is small.
  • Non-Patent Documents 1 As the gas to be mixed with the fuel, when using a mixed gas of air and oxygen gas, even when compared with the case of air combustion, sometimes NO x emissions increased (e.g., Non-Patent Documents 1). More specifically, in the case where the oxygen concentration in the mixed gas is more than 25% by volume less than 93% by volume, as compared with the case of air combustion, comprising a number NO x emissions.
  • both the air combustion burner and the oxyfuel combustion burner are dissolved for the purpose of adjusting the amount of water dissolved in the molten glass in the melting chamber while suppressing an increase in the emission amount of CO 2 and NO x.
  • the moisture concentration in the gas after combustion in the melting chamber is sufficiently controlled by the influence of the exhaust port provided on the side wall of the melting chamber. It may be difficult to do. As a result, it may be difficult to sufficiently adjust the amount of water dissolved in the molten glass in the melting chamber.
  • the present invention has been made in view of the above problems, and provides a glass melting furnace capable of sufficiently adjusting the amount of water dissolved in molten glass while suppressing an increase in the discharge amount of CO 2 and NO x.
  • the purpose is to provide.
  • the present invention comprises a melting chamber for melting a glass raw material, and a plurality of burners provided on a side wall of a flow path from the front wall to the rear wall of the melting chamber, wherein the plurality of burners In a glass melting furnace in which a flame is jetted into the melting chamber to heat and melt the glass in the melting chamber,
  • a glass melting furnace in which a flame is jetted into the melting chamber to heat and melt the glass in the melting chamber
  • both an oxyfuel burner that ejects a flame that is burned by mixing fuel with oxygen gas and an air combustion burner that ejects a flame that is burned by mixing fuel with air are used.
  • At least one each of the oxyfuel burner and the air combustion burner is provided in a region separated by 0.6 L or more in the direction, In the glass melting furnace, 5% or more and 95% or less of the total amount of combustion heat per hour of the burner provided in the region is due to the air combustion burner.
  • the glass melting furnace which can fully adjust the moisture content dissolved in a molten glass can be provided, suppressing the increase in NOx discharge
  • This glass melting furnace is particularly effective when the moisture content is reduced while sufficiently heating the molten glass.
  • FIG. 1 is a process diagram of a glass product manufacturing method according to an embodiment of the present invention.
  • FIG. 2 is a side view of the internal structure of the glass melting furnace in the first embodiment.
  • FIG. 3 is a top view of the internal structure of the glass melting furnace in the first embodiment.
  • FIG. 4 is a side view of the internal structure of the glass melting furnace in the second embodiment.
  • FIG. 5 is a top view of the internal structure of the glass melting furnace in the second embodiment.
  • FIG. 6 is a side view of the internal structure of the glass melting furnace in the third embodiment.
  • FIG. 7 is a top view of the internal structure of the glass melting furnace in the third embodiment.
  • FIG. 8 is a top view of a modified example of the internal structure of the glass melting furnace.
  • FIG. 9 is a top view of another modification of the internal structure of the glass melting furnace.
  • FIG. 1 is a process diagram of a glass product manufacturing method according to an embodiment of the present invention.
  • FIG. 2 is a side view of the internal structure of the glass melting furnace in the first embodiment.
  • FIG. 3 is a top view of the internal structure of the glass melting furnace in the first embodiment. In FIG. 3, the combustion region of each burner (the outer edge of the flame of each burner) is shown surrounded by a dotted line.
  • the glass product manufacturing method includes a melting step (S100) in which a glass raw material is melted to obtain molten glass, and a clarification step (S102) in which bubbles of the molten glass are removed to clarify the molten glass. And a forming step (S104) of forming the clarified molten glass into a predetermined shape.
  • the clarification step (S102) is a step of supplying the molten glass obtained in the melting step to the clarification tank and floating and removing bubbles in the molten glass.
  • a method for promoting the rising of bubbles for example, there is a method of degassing by depressurizing the inside of a clarification tank.
  • the forming step (S104) is a step of forming the clarified molten glass into a plate having a predetermined plate thickness.
  • a method for forming a plate for example, there is a well-known float method or a fusion method.
  • the melting step (S100) is a step in which a plurality of kinds of raw materials are weighed according to the composition of the glass product and mixed to add a glass raw material to a melting furnace and heated to a temperature corresponding to the type of glass to be melted.
  • the melting furnace 1 is provided with a raw material charging port 21 on the upstream front wall 11 of the melting chamber 10 for melting the glass raw material, and is attached to the rear wall 12 on the downstream side of the melting chamber 10.
  • An outlet 22 is provided, and a plurality of burners 31 to 50 and a pair of exhaust ports 24 and 25 are provided on both side walls 13 and 14 of the flow path 23 from the raw material inlet 21 to the outlet 22. Both side walls 13 and 14 extend in the front-rear direction.
  • the glass material G1 charged from the material charging port 21 is heated by the radiant heat from the flames of the plurality of burners 31 to 50 together with the molten glass G2 in the melting chamber 10, and gradually enters the molten glass G2. Blend into.
  • the molten glass G2 obtained in this way flows backward, is taken out from the outlet 22 and is supplied to the clarification tank.
  • the melting chamber 10 is formed by a melting tank 15 that contains a molten glass obtained by melting a glass raw material, and a ceiling 16 that covers an upper space in the melting tank 15.
  • the dissolution tank 15 and the ceiling 16 are made of a refractory material such as brick.
  • the size of the melting chamber 10 is not particularly limited, but for example, the longitudinal dimension X1 of the melting chamber 10 is 10 to 30 m, preferably 10 to 25 m.
  • the dimension Y1 in the width direction of the melting chamber 10 is 5 to 10 m.
  • the height direction dimension Z1 of the melting chamber 10 is 3 to 8 m.
  • the pair of exhaust ports 24 and 25 are for exhausting the burned gas in the melting chamber 10 to the outside.
  • the pair of exhaust ports 24 and 25 are disposed at one end in the front-rear direction of the side walls 13 and 14 and are disposed in the vicinity of the front wall 11.
  • the exhaust port 24 arranged on the left side wall 13 and the exhaust port 25 arranged on the right side wall 14 are arranged to face each other with the flow path 23 interposed therebetween. If the pair of exhaust ports 24 and 25 are arranged so as to be displaced in the front-rear direction, the exhaust is performed asymmetrically with respect to the flow path 23, so that it is difficult to control the temperature distribution of the molten glass.
  • the size of the exhaust ports 24 and 25 is not particularly limited.
  • the front-rear direction dimension X2 of the exhaust ports 24 and 25 is about 1 m
  • the height direction dimension Z2 of the exhaust ports 24 and 25 is about 1 m.
  • the plurality of burners 31 to 50 jet a flame into the melting chamber 10 and heat and melt the glass in the melting chamber 10.
  • the plurality of burners 31 to 50 may eject a flame continuously or may eject a flame intermittently. When the flame is intermittently ejected, the plurality of burners 31 to 50 may eject the flame at the same time or may eject the flame at different timings.
  • the plurality of burners 31 to 50 are disposed on the side walls 13 and 14 so that the flames do not interfere with each other.
  • the plurality of burners 31 to 40 arranged on the left side wall 13 and the plurality of burners 41 to 50 arranged on the right side wall 14 are arranged to face each other with the flow path 23 interposed therebetween. That is, the plurality of burners 31 to 50 are arranged symmetrically with the flow path 23 in between. Note that the plurality of burners 31 to 50 may be arranged in a staggered manner with the flow path 23 interposed therebetween.
  • the plurality of burners 31 to 40 arranged on the left side wall 13 may be arranged at unequal pitches in the front-rear direction along the flow path 23, or may be arranged at equal pitches. The same applies to the plurality of burners 41 to 50 arranged on the right wall 14.
  • the plurality of burners 31 to 50 eject a flame in which fuel is mixed with gas and burned.
  • fuel used for the burners 31 to 50 for example, gaseous fuel such as natural gas or city gas, or liquid fuel such as heavy oil is used. When liquid fuel is used, liquid combustion is sprayed in a mist form.
  • the same type of fuel may be used, or different types of fuel may be used.
  • either air or oxygen gas is used as the gas mixed with the fuel.
  • nitrogen gas occupying about 78% by volume of air is exhausted outside the furnace without contributing to combustion.
  • oxyfuel combustion using oxygen gas since the amount of exhaust is small compared to the case of air combustion, the thermal efficiency is high, and the amount of CO 2 emission and NO x emission is small.
  • the gas to be mixed with the fuel when using a mixed gas of air and oxygen gas, even when compared with the case of air combustion, sometimes NO x emissions increased. More specifically, in the case where the oxygen concentration in the mixed gas is more than 25% by volume less than 93% by volume, as compared with the case of air combustion, comprising a number NO x emissions.
  • the burners 31 to 50 eject an air combustion burner for ejecting a flame in which fuel is mixed with air and a flame in which fuel is mixed with oxygen gas and combusted.
  • An oxyfuel burner is used.
  • the oxygen gas refers to a gas having an oxygen concentration of 93% by volume or more.
  • 30% or more (preferably 35% or more) and 90% or less (preferably 87% or less) of the total combustion heat quantity Qa per hour of the plurality of burners 31 to 50 is due to the oxyfuel combustion burner. is there.
  • the total heating amount Qb per hour used for heating the glass in the melting chamber 10 is the total amount of combustion heat Qa per hour of the plurality of burners 31 to 50, and after the combustion in the melting chamber 10 Is the difference (Qa-Qc) from the total exhaust heat quantity Qc per hour that is taken out of the melting chamber 10 through the exhaust ports 24, 25.
  • the total exhaust heat quantity Qc per hour is calculated based on the exhaust quantity per hour, the temperature of the exhaust gas, and the like.
  • the contribution rate of the oxyfuel burner to the total combustion heat quantity Qa as described above, it is possible to suppress a decrease in thermal efficiency, an increase in CO 2 emissions, and an increase in NO x emissions due to the use of the air combustion burner. it can. Moreover, since the fall of thermal efficiency can be suppressed, it is easy to keep the temperature in the melting chamber 10 at a relatively high temperature. For this reason, in addition to soda-lime glass products, it is particularly suitable for the production of glass products with a high melting point. Examples of such high melting point glass products include glass substrates for liquid crystal displays (so-called non-alkali glass substrates). The alkali-free glass has a melting point of 100 ° C. or more higher than that of general soda lime glass.
  • the gas after combustion in the melting chamber 10 is affected by the exhaust ports 24 and 25 provided in the side walls 13 and 14 of the melting chamber 10. In some cases, it is difficult to sufficiently adjust the moisture concentration contained in the water. As a result, it may be difficult to sufficiently adjust the amount of water dissolved in the molten glass in the melting chamber 10.
  • the amount of water dissolved in the molten glass is too small, it is not possible to sufficiently promote the floating of bubbles in the molten glass in the refining process.
  • the amount of water dissolved in the molten glass is too large, bubbles may remain in the molten glass in the clarification step.
  • the amount of water dissolved in the molten glass is too large, bubbles may be generated at the interface between the molten glass and platinum when the inner wall surface of the flow path of the molten glass is covered with platinum in the clarification process or the like.
  • the amount of water dissolved in the molten glass is too small, it is not possible to sufficiently promote the floating of bubbles in the molten glass in the refining process.
  • the amount of water dissolved in the molten glass is too large, bubbles may remain in the molten glass in the clarification step.
  • the amount of water dissolved in the molten glass is too large, bubbles may be generated at the interface between the molten glass and platinum when the inner wall surface of the flow path
  • At least one air combustion burner and oxyfuel combustion burner are provided in a region separated by 0.6 L or more (preferably 0.7 L or more) in the rearward direction from the exhaust ports 24 and 25.
  • L is the maximum distance among the distance L1 in the front-rear direction between the exhaust ports 24, 25 and the front wall 11 and the distance L2 in the front-rear direction between the exhaust ports 24, 25 and the rear wall 12 (FIG. 2).
  • L2 is represented.
  • At least one air combustion burner and oxyfuel combustion burner are provided in the region separated by 0.6 L or more in the rearward direction from the exhaust ports 24 and 25, the gas after air combustion and the gas after oxyfuel combustion are separated from each other. A sufficient area can be secured. Therefore, it is possible to sufficiently secure a region where the concentration of moisture contained in the gas after combustion can be adjusted, and the amount of moisture dissolved in the molten glass in the melting chamber 10 can be varied over a wide range. As a result, the amount of water dissolved in the molten glass in the melting chamber 10 can be sufficiently adjusted, and in the refining process, the growth of bubbles in the molten glass can be promoted and the rising of bubbles can be promoted. A glass product with a small amount can be produced.
  • the amount of water dissolved in the molten glass in the melting chamber 10 is appropriately adjusted according to changes in the composition and type of the glass product, as well as deterioration of the furnace wall, changes in the glass raw material lot, and fuel lots. It may be adjusted appropriately according to the change of the above.
  • the amount of water dissolved in the molten glass in the melting chamber 10 is adjusted by adjusting the combustion heat amount ratio per hour between the air combustion burner and the oxyfuel combustion burner.
  • the objects of this adjustment are mainly burners 37 to 40 and 47 to 50 provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24 and 25.
  • 5% or more and 95% or less of the combustion heat quantity Qd per hour of the burners 37 to 40 and 47 to 50 provided in a region separated by 0.6 L or more in the rearward direction from the pair of exhaust ports 24 and 25 (preferably 10% to 90%, more preferably 15% to 90%) is due to the air combustion burner.
  • the moisture concentration contained in the gas after combustion in the melting chamber 10 is too high, and the amount of water dissolved in the molten glass in the melting chamber 10 is too large.
  • it exceeds 95% the water concentration contained in the gas after combustion in the melting chamber 10 is too low, and the amount of water dissolved in the molten glass in the melting chamber 10 is too small.
  • the amount of water dissolved in the molten glass is considered to be equivalent to the amount of water in the produced glass, and is represented by the value of ⁇ -OH (unit: / mm) in the produced glass.
  • the value B of ⁇ -OH is calculated by measuring the thickness C and transmittance T of glass and substituting the measurement results into the following equation.
  • a general Fourier transform infrared spectrophotometer (FT-IR) is used for measuring the transmittance of glass.
  • ⁇ -OH is preferably 0.25 to 0.52 / mm, more preferably 0.3 to 0.5 / mm, and further preferably 0.35 to 0.48 / mm. .
  • At least one oxyfuel combustion burner for example, burner 39
  • two air combustion burners for example, burners 38 and 40.
  • only one exhaust port 24, 25 is arranged opposite to each of the side walls 13, 14 of the flow path 23, but the exhaust port is only one side wall of the flow path.
  • a configuration in which only one is arranged may be used.
  • the exhaust ports 24 and 25 are disposed at one end in the front-rear direction of the side walls 13 and 14 and are disposed in the vicinity of the front wall 11, but the position of the exhaust port is not limited.
  • the exhaust port may be disposed in the vicinity of the rear wall.
  • the exhaust port may be provided in the middle between the front-rear direction end and the front-rear direction center of the side wall.
  • the second embodiment relates to a glass melting furnace according to the present invention. Specifically, a pair of exhaust ports are arranged at the center in the front-rear direction of the side wall. That is, a pair of exhaust ports are arranged in the center between the front wall and the rear wall.
  • FIG. 4 is a side view of the internal structure of the glass melting furnace in the second embodiment.
  • FIG. 5 is a top view of the internal structure of the glass melting furnace in the second embodiment. In FIG. 5, the outer edge of the flame of each burner is shown surrounded by a dotted line. 4 and FIG. 5, the same components as those in FIG. 2 and FIG.
  • the melting furnace 1 ⁇ / b> A includes a raw material inlet 21 on the front wall 11 of the melting chamber 10, and an outlet 22 on the rear wall 12 of the melting chamber 10.
  • a plurality of burners 31A to 50A and a pair of exhaust ports 24A and 25A are provided on the side walls 13 and 14 of the flow path 23 leading to the outlet 22.
  • the pair of exhaust ports 24 ⁇ / b> A and 25 ⁇ / b> A are disposed in the center in the front-rear direction of the side walls 13 and 14, and are disposed in the center between the front wall 11 and the rear wall 12.
  • the exhaust port 24 ⁇ / b> A disposed on the left side wall 13 and the exhaust port 25 ⁇ / b> A disposed on the right side wall 14 are disposed to face each other with the flow path 23 interposed therebetween.
  • air burners and oxyfuel burners are used for the burners 31A to 50A. Therefore, as in the first embodiment, an increase in the NO x emission amount can be suppressed.
  • 30% or more (preferably 35% or more) of the total combustion heat quantity Qa per hour of the plurality of burners 31A to 50A is 90% or less (preferably 87). % Or less) is due to the oxyfuel burner.
  • the air combustion burner and the oxyfuel combustion burner are located in a region separated by 0.6 L or more (preferably 0.7 L or more) in the rearward direction from the exhaust ports 24A and 25A. At least one is provided.
  • a sufficient region for adjusting the moisture concentration contained in the gas after combustion can be secured, and the amount of moisture dissolved in the molten glass in the melting chamber 10 can be varied over a wide range. It can be.
  • the amount of water dissolved in the molten glass in the melting chamber 10 can be sufficiently adjusted, and in the refining process, the growth of bubbles in the molten glass can be promoted and the rising of bubbles can be promoted.
  • a glass product with a small amount can be manufactured.
  • the amount of water dissolved in the molten glass in the melting chamber 10 is adjusted by adjusting the combustion heat amount ratio per hour between the air combustion burner and the oxyfuel combustion burner.
  • the targets of this adjustment are mainly the burners 39A to 40A and 49A to 50A provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24A and 25A.
  • the moisture concentration contained in the gas after combustion in the melting chamber 10 is too high, and the amount of water dissolved in the molten glass in the melting chamber 10 is too large.
  • it exceeds 95% the water concentration contained in the gas after combustion in the melting chamber 10 is too low, and the amount of water dissolved in the molten glass in the melting chamber 10 is too small.
  • only one exhaust port 24A, 25A is arranged to face each of the side walls 13, 14 of the flow path 23, but the exhaust port is only one side wall of the flow path.
  • a configuration in which only one is arranged may be used.
  • At least one air combustion burner and one oxygen combustion burner are provided in a region separated by 0.6 L or more (preferably 0.7 L or more) in the rearward direction from the exhaust ports 24A and 25A.
  • the present invention is not limited to this.
  • at least one air combustion burner and one oxyfuel combustion burner may be provided in a region separated by 0.6 L or more (preferably 0.7 L or more) in the forward direction from the exhaust ports 24A and 25A. Both configurations may be combined.
  • the third embodiment relates to a glass melting furnace according to the present invention. Specifically, a plurality of burners are arranged in a staggered manner across the flow path.
  • FIG. 6 is a side view of the internal structure of the glass melting furnace in the third embodiment.
  • FIG. 7 is a top view of the internal structure of the glass melting furnace in the third embodiment. In FIG. 7, the outer edge of the flame of each burner is shown surrounded by a dotted line. 6 and FIG. 7, the same components as those in FIG. 2 and FIG.
  • the melting furnace 1B includes a raw material inlet 21B on the front wall 11B of the melting chamber 10B, and an outlet 22B on the rear wall 12B of the melting chamber 10B.
  • a plurality of burners 31B to 33B, 41B to 42B and a pair of exhaust ports 24B and 25B are provided on the side walls 13B and 14B of the flow path 23B leading to the outlet 22B.
  • the size of the melting chamber 10B is not particularly limited.
  • the longitudinal dimension X3 of the melting chamber 10B is 2 to 5 m
  • the width dimension Y3 of the melting chamber 10B is 1 to 3 m
  • the height of the melting chamber 10B is 1 to 3 m.
  • the direction dimension Z3 is 1 to 3 m.
  • the pair of exhaust ports 24B and 25B are arranged at one end in the front-rear direction of both side walls 13B and 14B, and are arranged in the vicinity of the front wall 11B.
  • the exhaust port 24B disposed on the left side wall 13B and the exhaust port 25B disposed on the right side wall 14B are disposed to face each other with the flow path 23B interposed therebetween.
  • the size of the exhaust ports 24B and 25B is not particularly limited.
  • the front and rear dimension X4 of the exhaust ports 24B and 25B is about 0.3 m
  • the height direction dimension Z4 of the exhaust ports 24B and 25B is 0.2 m. Degree.
  • the plurality of burners 31B to 33B and 41B to 42B are arranged in a staggered manner with the flow path 23B interposed therebetween.
  • the plurality of burners 31B to 33B arranged on the left side wall 13B are arranged in the front-rear direction along the flow path 23B.
  • the plurality of burners 41B to 42B arranged on the right side wall 14B are arranged in the front-rear direction along the flow path 23B.
  • air burners and oxyfuel burners are used for the burners 31B to 33B and 41B to 42B. Therefore, similarly to the first embodiment, it is possible to suppress an increase in the emission amount of CO 2 and NO x .
  • 30% or more (preferably 35% or more) of the total combustion heat quantity Qa per hour of the plurality of burners 31B to 33B and 41B to 42B is 90% or less (preferably 35% or more).
  • 87% or less) is due to the oxyfuel burner.
  • an air combustion burner and an oxyfuel combustion burner are located in a region separated by 0.6 L or more (preferably 0.7 L or more) in the rearward direction from the exhaust ports 24B and 25B. At least one is provided.
  • L is the maximum distance among the distance L5 in the front-rear direction between the exhaust ports 24B, 25B and the front wall 11B and the distance L6 in the front-rear direction between the exhaust ports 24B, 25B and the rear wall 12B (FIG. 7). In the example shown in FIG.
  • the amount of moisture dissolved in the molten glass in the melting chamber 10B can be varied in a wide range. It can be.
  • the amount of water dissolved in the molten glass in the melting chamber 10B can be sufficiently adjusted, and in the refining process, the growth of bubbles in the molten glass can be promoted and the rising of bubbles can be promoted. A glass product with a small amount can be produced.
  • the amount of water dissolved in the molten glass in the melting chamber 10B is adjusted by adjusting the ratio of the amount of combustion heat per hour between the air combustion burner and the oxyfuel combustion burner.
  • the targets of this adjustment are mainly the burners 33B and 42B provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24B and 25B.
  • 5% or more and 95% or less (preferably 10% or more and 90% or less) of the amount of combustion heat Qd per hour of the burners 33B and 42B provided in the region separated by 0.6L or more rearward from the exhaust ports 24B and 25B. , More preferably 15% or more and 90% or less) is due to the air combustion burner.
  • the water concentration contained in the gas after combustion in the melting chamber 10B is too high, and the amount of water dissolved in the molten glass in the melting chamber 10B is too large.
  • it exceeds 95% the water concentration contained in the gas after combustion in the melting chamber 10B is too low, and the amount of water dissolved in the molten glass in the melting chamber 10B is too small.
  • a constricted portion 19 that divides the melting chamber 10C into two chambers 17 and 18 may be provided on both side walls 13C and 14C of the melting chamber 10C.
  • the rear room 18 is a room for adjusting the temperature of the molten glass, and no burner is provided on the side wall of the rear room 18.
  • the raw material charging port 21D may be provided on both side walls 13D and 14D of the melting chamber 10D, and the exhaust port 24D may be provided on the front wall 11D.
  • the exhaust port 24D may be provided in the front wall 11D and / or the rear wall 12D.
  • the gas mixed with the fuel of the air combustion burner in the present invention is preferably air.
  • the amount of NOx emission does not increase, specifically oxygen in the gas mixed with the fuel. If it is 25 volume% or less, oxygen gas can be mixed in addition to air.
  • an observation window for confirming the melting state of the glass is provided on the side wall of the melting chamber (not shown), and the door of the observation window is a little to improve the sealing property when opening and closing up and down. It is preferable to be provided with an inclination.
  • Examples 1 to 10 In Examples 1 to 10 (Tables 1 and 2), ⁇ -OH (unit: / mm) in the glass produced using the glass melting furnace shown in FIGS. 2 and 3 was obtained by calculation. ⁇ -OH is an index indicating the amount of water in the glass, and the larger the ⁇ -OH, the greater the amount of water in the glass. Examples 2, 4 to 6, and 10 are examples, and examples 1, 3, and 7 to 9 are comparative examples.
  • the method for calculating ⁇ -OH will be briefly described. First, based on the composition of the fuel and gas burned by each burner, the water concentration contained in the burned gas was calculated. Next, in consideration of the fact that the burned gas flows toward the exhaust port, the distribution of moisture concentration in the atmosphere in the melting chamber was calculated. Based on the moisture concentration distribution and the average flow rate of the molten glass, the amount of moisture finally diffused into the molten glass was calculated and converted to ⁇ -OH contained in the glass after production.
  • the longitudinal dimension X1 of the melting chamber 10 was set to 25 m
  • the width dimension Y1 of the melting chamber 10 was set to 10 m
  • the height dimension Z1 of the melting chamber 10 was set to 8 m.
  • the volume of the molten glass in the melting chamber 10 is set to 300 m 3
  • the volume of the glass raw material that is, the molten glass taken out from the melting chamber 10 per hour
  • the longitudinal dimension X2 of the exhaust ports 24 and 25 was set to 1 m
  • the height direction dimension Z2 of the exhaust ports 24 and 25 was set to 1 m.
  • the distance L1 in the front-rear direction between the front wall 11 and the exhaust port 24 is 2 m
  • the distance in the front-rear direction from the exhaust port 24 to each of the burners 31 to 40 is 2 m ⁇ N (N Is a natural number of 1 to 10, and the distance in the front-rear direction between the exhaust port 24 and the burner 40 is set to 20 m.
  • the arrangement of the exhaust port 25 and the plurality of burners 41 to 50 is also set on the right side wall 14.
  • each of the plurality of oxyfuel combustion burners is set to have the same amount of combustion heat per hour
  • each of the plurality of air combustion burners has the same amount of combustion heat per hour
  • each air combustion The amount of combustion heat per hour of the burner was set smaller than the amount of combustion heat per hour of each oxyfuel combustion burner.
  • Example 6 the combustion heat amount per hour of each of the plurality of oxyfuel combustion burners is set the same, the combustion heat amount per hour of each of the plurality of air combustion burners is set the same, and each air combustion The amount of combustion heat per hour of the burner was set larger than the amount of combustion heat per hour of each oxyfuel combustion burner.
  • the oxyfuel burner was used for the burners 31 to 50 of Examples 1 and 9, and the oxyfuel burner and the air combustion burner were used for the burners 31 to 50 of Examples 2 to 8.
  • Nm 3 which is a unit of CO 2 emission represents a volume in a standard state (0 ° C., 1 atm) (the same applies to Tables 3 and 4).
  • the air combustion burner No. No. of the oxyfuel combustion burner is indicated. Is omitted (the same applies to Tables 3 and 4).
  • Example 1 to 8 where the fuel is natural gas, in Examples 2 and 4 to 6, air is disposed in a region separated by 0.6 L or more from the exhaust ports 24 and 25 in the rearward direction. At least one combustion burner and one oxyfuel combustion burner are provided, and the ⁇ -OH in the glass is reduced by 10% or more compared to the case of Example 1.
  • Example 10 where the fuel is heavy oil, in Example 10, at least one air combustion burner and one oxyfuel combustion burner are provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24 and 25. In comparison with Example 9, ⁇ -OH in the glass is reduced by 10% or more.
  • ⁇ -OH can be sufficiently adjusted by changing the combustion heat quantity ratio per hour between the air combustion burner and the oxyfuel combustion burner. Therefore, in Examples 2, 4 to 6, and 10, the amount of water dissolved in the molten glass in the melting chamber 10 is sufficiently adjusted by adjusting the combustion heat ratio per hour between the air combustion burner and the oxyfuel combustion burner. can do.
  • Example 3 as in Example 2, at least one air combustion burner and one oxygen combustion burner are provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24, 25. Unlike the above, 99% of the total heating amount Qb per hour used for heating the glass in the melting chamber is due to the oxygen combustion burner. For this reason, in Example 3, ⁇ -OH in the glass does not decrease by more than 10% compared to Example 1. Therefore, in Example 3, it can be seen that it is difficult to sufficiently reduce the amount of water dissolved in the molten glass in the melting chamber 10.
  • Example 11-12 In Examples 11 to 12 (Table 3), ⁇ -OH (unit: / mm) in the glass produced using the glass melting furnace shown in FIGS. 4 and 5 was determined by the above calculation.
  • Example 12 is an example and Example 11 is a comparative example.
  • Example 11 to 12 the size of the melting chamber, the size of the exhaust port, and the front-rear direction between the exhaust port and each burner, except that the exhaust ports 24A, 25A are arranged in the center in the front-rear direction of the side walls 13, 14.
  • the distance and the like were set in the same manner as in Examples 1-10.
  • the amount of combustion heat per hour of each of the plurality of burners 31A to 50A was set to be the same. Note that only the oxyfuel burner was used for the burners 31A to 50A of Example 11, and the oxyfuel burner and the air combustion burner were used for the burners 31A to 50A of Example 12.
  • Example 12 As understood from Table 3, in Example 12, at least one air combustion burner and oxyfuel combustion burner are provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24A, 25A. Compared with the case of, ⁇ -OH in the glass is reduced by 10% or more. Therefore, in Example 12, it can be seen that the amount of water dissolved in the molten glass in the melting chamber 10 can be sufficiently adjusted by adjusting the combustion heat amount ratio per hour between the air combustion burner and the oxyfuel combustion burner. .
  • Example 13 to 14 In Examples 13 to 14 (Table 4), ⁇ -OH (unit: / mm) in the glass produced using the glass melting furnace shown in FIGS. 6 and 7 was obtained by the above calculation.
  • Example 14 is an example and Example 13 is a comparative example.
  • the longitudinal dimension X3 of the melting chamber 10B was set to 3 m
  • the width dimension Y3 of the melting chamber 10B was set to 2 m
  • the height dimension Z3 of the melting chamber 10B was set to 2 m.
  • the volume of the molten glass in the melting chamber 10B is set to 4.5 m 3
  • a glass raw material charged into the melting chamber 10B per hour ie, molten glass taken out from the melting chamber 10B per hour.
  • the longitudinal dimension X4 of the exhaust ports 24B and 25B was set to 0.3 m
  • the height direction dimension Z4 of the exhaust ports 24B and 25B was set to 0.3 m.
  • the distance L5 in the front-rear direction between the front wall 11B and the exhaust port 24B is 0.2 m
  • the distance in the front-rear direction between the exhaust port 24B and the burner 31B is 0.3 m.
  • the distance in the front-rear direction between the port 24B and the burner 32B was set to 1.0 m
  • the distance in the front-rear direction between the exhaust port 24B and the burner 33B was set to 2.0 m.
  • the distance L5 in the front-rear direction between the front wall 11B and the exhaust port 25B is 0.2 m
  • the distance in the front-rear direction between the exhaust port 25B and the burner 41B is 0.5 m.
  • the distance in the front-rear direction between the mouth 25B and the burner 42B was set to 1.5 m.
  • the amount of combustion heat per hour of each of the plurality of burners 31B to 33B and 41B to 42B was set to be the same. Note that only the oxyfuel burner was used for the burners 31B to 33B and 41B to 42B of Example 13, and the oxyfuel burner and the air combustion burner were used for the burners 31B to 33B and 41B to 42B of Example 14.
  • Example 14 As understood from Table 4, in Example 14, at least one air combustion burner and oxyfuel combustion burner are provided in a region separated by 0.6 L or more in the rearward direction from the exhaust ports 24B and 25B. Compared with the case of, ⁇ -OH in the glass plate is reduced by 10% or more. Therefore, in Example 14, it can be seen that the amount of water dissolved in the molten glass in the melting chamber 10B can be sufficiently adjusted by adjusting the combustion heat amount ratio per hour between the air combustion burner and the oxyfuel combustion burner. .
  • the glass melting furnace which can fully adjust the moisture content dissolved in a molten glass can be provided, suppressing the increase in NOx discharge
  • This glass melting furnace is particularly effective when the moisture content is reduced while sufficiently heating the molten glass.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Glass Melting And Manufacturing (AREA)

Abstract

Cette invention concerne un four de fusion du verre qui est capable de supprimer une augmentation des émissions de CO2 et NOX et de réguler de manière adéquate la teneur en eau dissoute dans le verre fondu. Le four de fusion du verre selon l'invention comprend une pluralité de brûleurs (31-50) sur les parois latérales (13, 14) d'un circuit d'écoulement (23) allant d'une paroi avant (11) à une paroi arrière (12) d'une chambre de fusion (10), de 30 à 90 % de la chaleur de combustion totale Qa par heure de la pluralité de brûleurs (31-50) étant générés par des brûleurs à combustion d'oxygène. Chaque paroi latérale (13, 14) de la chambre de fusion (10) comporte un orifice d'évacuation (24, 25) placé de façon que les orifices d'évacuation soient face à face, et qu'au moins un de chaque type de brûleur parmi les brûleurs à combustion d'oxygène et les brûleurs à combustion d'air soit présent dans une région située à une distance d'au moins 0,6 L dans une direction vers l'arrière par rapport aux orifices d'évacuation (24, 25). Sur la chaleur de combustion totale par heure des brûleurs qui se trouvent dans cette région, de 5 à 95 % de ladite chaleur sont générés par un brûleur à combustion d'air.
PCT/JP2011/059621 2010-04-26 2011-04-19 Four de fusion du verre et procédé afférent Ceased WO2011136086A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
KR1020127028072A KR101453639B1 (ko) 2010-04-26 2011-04-19 유리 용해로 및 유리 용해 방법
CN201180021090.7A CN102858697B (zh) 2010-04-26 2011-04-19 玻璃熔化炉及玻璃熔化方法
JP2012512791A JP5598541B2 (ja) 2010-04-26 2011-04-19 ガラス溶解炉及びガラス溶解方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2010101312 2010-04-26
JP2010-101312 2010-04-26

Publications (1)

Publication Number Publication Date
WO2011136086A1 true WO2011136086A1 (fr) 2011-11-03

Family

ID=44861393

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2011/059621 Ceased WO2011136086A1 (fr) 2010-04-26 2011-04-19 Four de fusion du verre et procédé afférent

Country Status (5)

Country Link
JP (1) JP5598541B2 (fr)
KR (1) KR101453639B1 (fr)
CN (1) CN102858697B (fr)
TW (1) TWI498301B (fr)
WO (1) WO2011136086A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017178712A (ja) * 2016-03-31 2017-10-05 ＡｖａｎＳｔｒａｔｅ株式会社 ガラス基板の製造方法、及び、ガラス基板の製造装置
JP2017186217A (ja) * 2016-04-08 2017-10-12 旭硝子株式会社 溶解方法、および無アルカリガラス板の製造方法
KR20230125744A (ko) 2022-02-21 2023-08-29 에이지씨 가부시키가이샤 유리 용해로, 유리 제품의 제조 설비 및 유리 제품의 제조 방법
KR20230125741A (ko) 2022-02-21 2023-08-29 에이지씨 가부시키가이샤 유리 용해로, 유리 제품의 제조 설비, 및 유리 제품의 제조 방법
WO2023199910A1 (fr) 2022-04-15 2023-10-19 日本電気硝子株式会社 Procédé de fabrication d'article en verre
WO2023199909A1 (fr) 2022-04-15 2023-10-19 日本電気硝子株式会社 Procédé de production d'un article en verre
WO2024150688A1 (fr) 2023-01-10 2024-07-18 日本電気硝子株式会社 Procédé de production d'un article en verre

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103771686A (zh) * 2014-01-15 2014-05-07 温州市康尔微晶器皿有限公司 一种微晶玻璃熔化池炉
JP6292090B2 (ja) * 2014-09-03 2018-03-14 旭硝子株式会社 溶解窯、溶解方法、および無アルカリガラス板の製造方法
US10759688B2 (en) * 2015-06-26 2020-09-01 Owens Corning Intellectual Capital, Llc Glass melter with oxygen/gas heat-up burner system

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0597444A (ja) * 1991-09-18 1993-04-20 Union Carbide Ind Gases Technol Corp ガラス溶融用の交差火炎型蓄熱炉における補助酸素バーナー技法
JP2001316121A (ja) * 2000-03-23 2001-11-13 Air Prod And Chem Inc 溶融帯域にわたる酸素−燃料燃焼および清澄帯域にわたる空気−燃料燃焼を有するガラス溶融方法ならびにそのための炉
DE10055924A1 (de) * 2000-08-19 2002-03-07 Horn Glasanlagen Gmbh Verfahren zum Betrieb eines Glasschmelzofens
JP2005035826A (ja) * 2003-07-18 2005-02-10 Japan Air Gases Ltd ガラス溶融窯
WO2009118336A1 (fr) * 2008-03-25 2009-10-01 Agc Flat Glass Europe Sa Four de fusion du verre

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5793419B2 (ja) * 2008-06-05 2015-10-14 エージーシー グラス ユーロップ ガラス溶融炉

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0597444A (ja) * 1991-09-18 1993-04-20 Union Carbide Ind Gases Technol Corp ガラス溶融用の交差火炎型蓄熱炉における補助酸素バーナー技法
JP2001316121A (ja) * 2000-03-23 2001-11-13 Air Prod And Chem Inc 溶融帯域にわたる酸素−燃料燃焼および清澄帯域にわたる空気−燃料燃焼を有するガラス溶融方法ならびにそのための炉
DE10055924A1 (de) * 2000-08-19 2002-03-07 Horn Glasanlagen Gmbh Verfahren zum Betrieb eines Glasschmelzofens
JP2005035826A (ja) * 2003-07-18 2005-02-10 Japan Air Gases Ltd ガラス溶融窯
WO2009118336A1 (fr) * 2008-03-25 2009-10-01 Agc Flat Glass Europe Sa Four de fusion du verre

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017178712A (ja) * 2016-03-31 2017-10-05 ＡｖａｎＳｔｒａｔｅ株式会社 ガラス基板の製造方法、及び、ガラス基板の製造装置
JP2017186217A (ja) * 2016-04-08 2017-10-12 旭硝子株式会社 溶解方法、および無アルカリガラス板の製造方法
KR20230125744A (ko) 2022-02-21 2023-08-29 에이지씨 가부시키가이샤 유리 용해로, 유리 제품의 제조 설비 및 유리 제품의 제조 방법
KR20230125741A (ko) 2022-02-21 2023-08-29 에이지씨 가부시키가이샤 유리 용해로, 유리 제품의 제조 설비, 및 유리 제품의 제조 방법
JP2023121645A (ja) * 2022-02-21 2023-08-31 Ａｇｃ株式会社 ガラス溶解炉、ガラス製品の製造設備、およびガラス製品の製造方法
JP7722217B2 (ja) 2022-02-21 2025-08-13 Ａｇｃ株式会社 ガラス溶解炉、ガラス製品の製造設備、およびガラス製品の製造方法
WO2023199910A1 (fr) 2022-04-15 2023-10-19 日本電気硝子株式会社 Procédé de fabrication d'article en verre
WO2023199909A1 (fr) 2022-04-15 2023-10-19 日本電気硝子株式会社 Procédé de production d'un article en verre
WO2024150688A1 (fr) 2023-01-10 2024-07-18 日本電気硝子株式会社 Procédé de production d'un article en verre

Also Published As

Publication number Publication date
KR20130080783A (ko) 2013-07-15
JP5598541B2 (ja) 2014-10-01
TW201141803A (en) 2011-12-01
TWI498301B (zh) 2015-09-01
KR101453639B1 (ko) 2014-11-03
CN102858697A (zh) 2013-01-02
CN102858697B (zh) 2016-01-20
JPWO2011136086A1 (ja) 2013-07-18

Similar Documents

Publication Publication Date Title
JP5598541B2 (ja) ガラス溶解炉及びガラス溶解方法
US6715319B2 (en) Melting of glass
KR101971755B1 (ko) 용융 유리 제조 장치, 용융 유리 제조 방법 및 그것들을 사용한 판유리의 제조 방법
EP2168923B1 (fr) Four de fusion de verre et procédé de fabrication d'un produit de verre
EP4103523A1 (fr) Production de verre incolore par fusion par combustion en immersion
JP6292090B2 (ja) 溶解窯、溶解方法、および無アルカリガラス板の製造方法
TWI483913B (zh) A method for producing a molten glass, a method for producing a molten glass, and a method of manufacturing the same,
TWI704111B (zh) 熔解方法、及無鹼玻璃板之製造方法
CN201343485Y (zh) 一种用于玻璃熔化操作的熔窑
JP2017075069A (ja) ガラス溶解炉、ガラス溶解方法、およびガラス製造方法
JP7760930B2 (ja) ガラス溶解炉、ガラス製品の製造設備、およびガラス製品の製造方法
JP7722217B2 (ja) ガラス溶解炉、ガラス製品の製造設備、およびガラス製品の製造方法
EP3907196A1 (fr) Four pour fondre plusieurs verres simultanément

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 201180021090.7

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11774869

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2012512791

Country of ref document: JP

ENP Entry into the national phase

Ref document number: 20127028072

Country of ref document: KR

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 11774869

Country of ref document: EP

Kind code of ref document: A1