TW201141803A - Glass melting furnace and method for melting glass - Google Patents

Abstract

Disclosed is a glass melting furnace which is capable of suppressing an increase in the amount of emission of CO2 and NOX and adequately regulating the water content dissolved in molten glass. The glass melting furnace comprises a plurality of burners (31-50) on side walls (13, 14) of a flow path (23) from a front wall (11) to a rear wall (12) of a melting chamber (10), wherein 30% to 90% of the total combustion heat Qa per hour of the plurality of burners (31-50) is generated by oxygen combustion burners. Each side wall (13, 14) of the melting chamber (10) has one exhaust port (24, 25) positioned so that the exhaust ports face one another, and at least one each of an oxygen combustion burner and an air combustion burner is provided in a region at least 0.6 L away in a backward direction from the exhaust ports (24, 25). Of the total combustion heat per hour of the burners provided in the region, 5% to 95% is generated by the air combustion burner.

Description

201141803 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a glass melting furnace for melting a glass raw material and a glass melting method. [Prior Art] A method of producing a glass article generally comprises a melting step of obtaining a marten glass by dissipating a glass raw material; a clarifying step of removing the bubbles of the molten glass to clarify the molten glass; and forming the clarified molten glass into The shaping step of a specific shape is formed. In the above steps, the melting step is a step of weighing and mixing the glass raw materials obtained by mixing the plurality of raw materials against the composition of the glass product into a melting furnace, and heating to a temperature corresponding to the type of the glass to dissolve. The melting furnace is provided with a raw material input port on the wall of the melting chamber of the molten glass raw material, and has a plurality of burners on the side wall of the flow path from the raw material input port to the take-out port after the melting chamber is provided, and the plurality of burners are combusted The device sprays a flame into the melting chamber to heat and melt the glass in the melting chamber. The burner is sprayed to mix a fuel such as natural gas or heavy oil with a gas and burn the flame. In general, as a gas mixed in a fuel, any of air and oxygen is used. In the case of burning with air, air containing about 78% by volume of air does not contribute to combustion and is exhausted to the outside of the furnace. When using oxygen-burning oxygen, it is more efficient than the case of air combustion. The exhaust gas volume is higher than that of the plant, and the C〇2 discharge amount or the krypton discharge amount is small. As a gas mixed in the fuel, it is also possible to use a mixed gas obtained by mixing air and oxygen 155915.doc I » 201141803 (for example, refer to Patent Document 1). In this case, the proportion of oxygen in the mixed gas is higher. The higher the concentration of water contained in the gas after combustion, the larger the amount of water dissolved in the molten glass in the melting chamber. The water dissolved in the molten glass becomes the bubble Z in the clarification step. The amount of water dissolved in the glass is optimized, and in the clarification step, the growth of the bubbles in the molten glass is promoted, and the floating of the bubbles is promoted, so that a glass product having less defects can be produced. However, as a gas mixed in the fuel, When a mixed gas obtained by mixing air and oxygen is used, the amount of NOx emission is also increased as compared with the case of air combustion (for example, refer to Non-Patent Document 丨). In detail, oxygen in a mixed gas When the concentration is less than 93% by volume and exceeds 5% by volume, the amount of ruthenium discharge is increased as compared with the case of air combustion. Patent Document Patent Document 1: Japanese Patent Laid-Open No. 2000-128549 Non-Patent Document Non-Patent Document 1: Research & Development, Kobe Steel Engineering Reports, Vol. 51, No. 2 (Sep. 2001) 'ρ·8 〜 12, "Research on Energy Saving and Low-Temperature Combustion of Oxygen-Enhanced Air" [Disclosure] The problem to be solved by the present invention is to reduce the amount of discharge of C〇2 or ΝΟχ and to adjust the melting chamber. The amount of water dissolved in the molten glass, and it is studied to set both the air burner and the oxygen burner in the melting furnace. 155915.doc 201141803 However, if both the air burner and the oxygen burner are set only in the melting furnace In the middle, it is difficult to sufficiently adjust the concentration of water contained in the gas after combustion in the melting chamber by the influence of the exhaust port provided on the side wall of the melting chamber. As a result, there is a case where the molten glass in the melting chamber is sufficiently adjusted. The amount of water dissolved in the medium becomes difficult. The present invention has been accomplished in the above-mentioned problems, and an object thereof is to provide an increase in the amount of discharge of C〇2 or NOx. A glass melting furnace capable of sufficiently adjusting the amount of water dissolved in the molten glass. Technical Solution to Problem In order to solve the above object, the present invention is a glass melting furnace comprising a melting chamber for melting a glass raw material, and a melting chamber disposed therein a plurality of burners from the front wall to the side wall of the flow path of the rear wall, wherein the plurality of burners spray a flame into the melting chamber to heat and melt the glass in the melting chamber; and the plurality of burners are used to eject An oxygen burner that mixes the fuel with oxygen and combusts the generated flame, and an air burner that ejects a flame that is mixed with the fuel and combusted, and the total combustion heat per hour of the plurality of burners 3% or more and 9% by weight or less are generated by the oxygen burner, and an exhaust port for exhausting the burned gas in the melting chamber to the outside is opposed to each other on both side walls of the melting chamber Only i are disposed in the ground, and are disposed only on the two side walls of the dissolution chamber, and are disposed only in i or disposed on the front wall or the rear of the melting chamber. , If the distance between the longitudinal direction of the exhaust port and the front wall and 155915.doc 201141803

The maximum distance among the distance between the exhaust port and the rear wall in the front-rear direction is L, and at least 1 is provided in each of the regions from the exhaust port toward the front and/or the rear away from the 〇6L or more. Each of the above oxygen burners and the above air burners are disposed in the above-mentioned burners in the area! 5% or more and 95% or less of the total combustion heat of the hour is generated by the above air burner. Advantageous Effects of Invention According to the present invention, it is possible to provide a glass melting furnace capable of suppressing an increase in the amount of discharge and sufficiently adjusting the amount of water dissolved in the molten glass. This glass melting furnace is particularly effective in the case where the molten glass is sufficiently heated and the moisture content is lowered. [Embodiment] Hereinafter, embodiments for carrying out the invention will be described with reference to the drawings. In the respective drawings, the same components are denoted by the same reference numerals, and the description thereof will be omitted. (First Embodiment) Fig. 1 is a view showing the steps of a method for producing a glass product according to an embodiment of the present invention. Fig. 2 is a side elevational view showing the internal structure of the glass melting furnace of the first embodiment. Fig. 3 is a plan view showing the internal structure of the glass melting furnace of the first embodiment. In Fig. 3, the combustion zone of each burner (the outer edge of the flame of each burner) is surrounded by a broken line. As shown in FIG. 1, the manufacturing method of the glass article comprises: melting the glass raw material to obtain a melting step of the molten glass (sl〇〇); removing the bubbles of the molten glass to clarify the clarification step of the molten glass (sl〇2): and clarifying The subsequent molten glass 1559l5.doc 201141803 is formed into a specific shape forming step (S104). In these steps, the clarification step (S1G2) is a step of supplying the molten glass obtained in the series step to the clarification tank to float the bubbles in the molten glass and to remove them. As a method of promoting the bubbling of the bubbles, there is, for example, a method of degassing under reduced pressure and the like. The forming step (S1G4) is a step of forming the clarified (four) glass into a plate shape having a specific thickness. As a method of forming into a plate shape, there are known floating methods and melting methods, for example. The melting step (S100) is a step in which a plurality of raw materials are weighed and mixed, and the obtained glass raw materials are placed in a melting furnace and heated to a temperature corresponding to the type of the glass to be melted. As shown in Fig. 2 and Fig. 3, the melting furnace is provided on the upstream side of the melting chamber 10 of the molten glass raw material, and the raw material inlet port 21 is provided in the wall, and the downstream wall 12 has a take-out port 22 on the downstream side of the melting chamber 1 The two side walls 13, 14 of the flow path 23 from the raw material input port 21 to the take-out port 22 are provided with a plurality of burners 31 to 5A and a pair of exhaust ports 24'25. The two side walls 13, 14 extend in the front-rear direction. In the melting furnace 1, the glass raw material (1) fed from the raw material input port 21 and the molten glass G2 melted into 10 are heated by radiant heat from a flame of a plurality of burners 31 to 50, and gradually refined into Hyun glass G2. The molten glass G2 thus obtained flows backward, is taken out from the take-out port 22, and is supplied to the clarification tank. The melting chamber 10 is formed by accommodating a melting tank 15 for melting molten glass obtained by melting a glass raw material, and a ceiling 16 covering the upper space in the dissolution tank 15. The melting tank 15 and the ceiling 16 are made of a refractory such as a brick. 155915.doc 201141803 Hyun solution to the size of 1 并 and Yite pp ^ ..., will be limited to 疋 ' For example, the melting direction of the chamber 10 before and after the direction X1 is 1 〇 ~ 3 〇 m, preferably for the certificate 10~25 m . Further, the width direction dimension Y1 of the dissolution chamber 1 is 5 〜 i 〇 m.隹 进而 Further, the height direction dimension Z1 of the melting chamber is 3 to 8 m. The exhaust ports 24 and 25 are for exhausting the burned gas in the melting chamber 1 to the outside. The pair of exhaust ports 24 and 25 are disposed at one end in the front and rear directions of the side walls 13 and 14, and are disposed in the vicinity of the front wall. The exhaust port 24 disposed on the left side wall 13 and the exhaust port disposed on the right side (four) 25 is disposed opposite to each other via the flow path 23. If the % exhaust port and the front-rear direction are shifted, the exhaust flow is asymmetrically left and right across 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. For example, the size X2 of the exhaust ports 24 and 25 in the rear direction is about 1 m, and the dimension Z2 in the height direction of the exhaust ports 24 and 25 is about 1 m. The burners 31 to 50 discharge a flame into the refining chamber, and heat and melt the glass in the melting chamber ίο. The plurality of burners 31 to 5 〇 can continuously eject the flame, and the flame can be intermittently ejected. When the flame is ejected, a plurality of burners 31 to 50 can simultaneously eject the flame, and the flame can be ejected at different timings. The plurality of burners 3 1 to 50 are arranged in such a manner as to not interfere with each other's flames. Two side walls 13, 14 such as 'a plurality of disposed on the left side wall 13 The burners 31 to 40 and the plurality of burners 41 to 5 disposed on the right side wall 14 are disposed to face each other across the flow path 23. That is, the plurality of burners 3丨 to the spell are symmetrically sandwiched by the flow path 23. Further, the plurality of burners 3 1 to 50 may be alternately arranged via the flow path 23 155915.doc 201141803. The plurality of burners 31 to 40 disposed on the left side wall 13 are along the flow path 23 in the front-rear direction. The fuel cells can be arranged at equal intervals, and can be arranged at equal intervals. The plurality of burners 41 to 50 disposed on the right side wall 14 are also the same. The plurality of burners 3 1 to 50 are sprayed to mix the fuel and the gas and burn. The flame is generated. As the fuel used in the burners 3 to 50, a liquid fuel such as natural gas or pipeline gas, or a liquid fuel such as heavy oil can be used. In the case of using a liquid fuel, the liquid is burned and sprayed into a mist. In the plurality of burners 3 1 to 50, the same kind of fuel may be used, or different kinds of fuels may be used. Generally, as the gas mixed in the fuel, any one of air and oxygen may be used. When the air is burning, it takes up air About 78% by volume of nitrogen gas is not burned and is exhausted to the outside of the furnace. When using oxygen-burning oxygen, the amount of exhaust gas is higher than that of air combustion, so the thermal efficiency is higher, c 〇2 discharge or N〇x discharge is less. As a gas mixed in the fuel, it is also possible to use a mixture of air and oxygen. In this case, the proportion of oxygen in the mixed gas :[Q] The higher the concentration of water contained in the gas after combustion, the more the amount of water dissolved in the molten glass in the solution chamber is increased. (4) The molten glass in the glass is floated in the step; By optimizing the water content of the lysate, and in the clarification step, the glassy soil product in the molten glass can be promoted less, and the bubble is promoted to float, so that the defect can be produced as a 'Kunhe in the fuel. In the case of using a mixed gas in which air is mixed with oxygen 155915.doc 201141803, there is a case where the amount of NOx emission is increased as compared with the case of air combustion. In detail, when the oxygen concentration in the mixed gas is less than 93% by volume and exceeds 25% by volume, the amount of NOx emission is increased as compared with the case of air combustion. In contrast, in the present embodiment, as the burners 3 to 5, an air burner that ejects a flame generated by mixing fuel and air and burns, and a fuel that is mixed with fuel and oxygen are produced by combustion. Oxygen burner for the flame. Here, the term "oxygen" means a gas having an oxygen concentration of 93% by volume or more. Thus, an increase in the amount of enthalpy discharge can be suppressed by using an air burner and an oxygen burner. Further, in the present embodiment, 30% or more (preferably 35% or more) of the total combustion heat amount Qa per one hour of the plurality of burners 31 to 5 is 9% or less (preferably 87 Å/min or less). Produced by an oxygen burner. Alternatively, 6% or more (preferably 68 〇/. or more) and 97% or less (preferably 95% or less) of the total heating amount Qb per hour used for heating the glass in the melting chamber (7) is oxidized by oxygen. Produced by the device. Here, the total heating amount Qb per hour used for heating the glass in the melting chamber 10 means the total combustion heat amount Qa of a plurality of burner hours, and the combustion gas in the melting chamber 1〇 via the exhaust gas. The difference (Qa-QC) of the total exhaust heat amount Qc per hour of the outside of the melting chamber 1 is discharged to the outside of the melting chamber 1 and 25. The total exhaust heat amount Qc per hour is calculated based on the exhaust gas amount per hour or the temperature of the exhaust gas. Setting the contribution rate of the oxy-combustor relative to the total heat of combustion in the above manner can thereby suppress the decrease in thermal efficiency caused by the use of the air burner or 155915.doc • 10-201141803 c〇2 increase in discharge amount 'N〇x The increase in the discharge amount can suppress the decrease in thermal efficiency, so that the temperature in the melting chamber 10 is easily maintained at a relatively high temperature. Therefore, in addition to Nayano glass products, it is also particularly suitable for the manufacture of glass products with high melting point. As such a high melting point glass product, for example, a glass substrate for a liquid crystal display (so-called money glass substrate) can be mentioned. Compared with the general sodium 33 glass, the melting point of the alkali-free glass is up to 100»c or more. However, if both the air burner and the oxygen burner are disposed only in the dazzling furnace, it is sometimes difficult to sufficiently adjust by the influence of the exhaust ports μ, 25 provided on the side walls 13, 14 of the melting chamber 10. The concentration of water contained in the gas after combustion in the dissolution chamber 1Q. As a result, it is difficult to sufficiently adjust the amount of water dissolved in the molten glass in the dissolution chamber 10. If the amount of water dissolved in the molten glass is too small, the bubbles in the molten glass are sufficiently promoted to float upward in the clarification step & On the other hand, if the amount of water dissolved in the molten glass is too large, bubbles remain in the molten glass in the clarification step. In addition, when the amount of water dissolved in the molten glass is too large, it is generally known that bubbles are formed at the interface between the molten glass and the platinum when the inner wall surface of the flow path of the molten glass is covered with platinum in the clarification step or the like. However, the burned gas in the melting chamber 10 tends to move toward the exhaust ports 24, 25. Therefore, in the present embodiment, at least one air burner and an oxygen burner are provided in each of the regions which are separated from the exhaust ports 24 and 25 by 0.6 L or more (preferably 0.7 L or more). Here, L represents the distance L1 in the front-rear direction between the exhaust ports 24, 25 and the front wall 11, and the distance in the front-rear direction between the exhaust ports 24, 25 and the rear wall 12 of 155915.doc -11 - 201141803 The maximum distance in L2 (L2 in the example shown in Figures 2 and 3). In this way, at least one air burner and the oxygen burner are provided in each of the regions which are separated from the exhaust ports 24 and 25 toward the rear by 〇6L or more, so that the gas after the combustion of the air and the gas after the combustion of the oxygen can be sufficiently ensured. The area. As a result, it is possible to sufficiently ensure that the concentration of the water contained in the gas after the combustion is adjusted, and the amount of water 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 1 can be sufficiently adjusted, and in the clarification step, the growth of the bubbles in the molten glass can be promoted, and the floating of the bubbles can be promoted, whereby the glass having less defects can be produced. product. Further, the amount of water dissolved in the molten glass in the melting chamber 10 can be appropriately adjusted according to the composition or type of the glass product, or can be adjusted according to the deterioration of the furnace wall, the batch of the glass raw material, and the batch of the fuel. The second change can be appropriately adjusted. The adjustment of the amount of water dissolved in the molten glass in the dissolution chamber 10 is carried out by adjusting the ratio of the heat of combustion per hour of the air burner to the oxygen burner. The target to be adjusted is mainly the burners 37 to 4, 47 to 50 which are disposed in the region which is separated from the exhaust ports 24 and 25 by 0.6 L or more. The higher the combustion heat ratio of the air burner relative to the oxygen burner, the lower the concentration of water contained in the gas after combustion in the melting chamber 1 ,, so that the molten glass in the melting chamber is dissolved in the molten glass. The amount of water is reduced. Here, the burners 37 to 40, 47 to 50 in the region which is separated from the pair of exhaust ports 24 and 25 toward the rear by 〇.6L or more are 155915.doc per hour of heat combustion 2d 201141803 5/ 95% or less of the crucible (preferably 1% or more and 9% or less, more preferably 15% or more and 90% or less) is produced by an air burner. When the amount is less than 5%, the concentration of water contained in the gas after combustion in the melting chamber 1 is too high, and the amount of water dissolved in the molten glass in the melting chamber 10 is excessive. On the other hand, when it exceeds 95%, the concentration of water 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 is too small. It is considered that the amount of water dissolved in the molten glass is the same as the amount of water in the manufactured glass, and is represented by the value of β_〇Η (unit: /mm) in the manufactured glass. The larger the value of β-ΟΗ, the larger the amount of water in the glass. The value of ββ_ OH is calculated by measuring the plate thickness c and the transmittance τ of the glass and substituting the measurement result into the following formula. Further, in the measurement of the transmittance of glass, a general Fourier transform infrared spectrophotometer (FT IR) was used. Β = (l/C)l〇g1()(Tl/T2), Τ1. Reference wave number ^(^/(^ glass penetration rate (unit: %), T2: hydroxyl absorption wave number 357〇/ The minimum penetration rate of glass near cm (unit: %). For example, in the case of alkali-free glass, β_〇Η is preferably 〇.25~ 〇.52/mm 'better than 〇.3~〇 .5/mm, and more preferably 〇35~ 〇.48/mm. Furthermore, it is preferred to provide at least one oxygen burner between two air burners (for example, burners 38, 4). For example, the burner 39). If two air burners are arranged adjacent to each other, as described above, in the air combustion, the thermal efficiency is lower than that of the oxygen combustion, so that it is easy to locally generate a low temperature region. 155915.doc •13· In the present embodiment, in the present embodiment, only one of the exhaust ports 24' 25 is disposed opposite to each other on the side walls 13 and 14 of the flow path 23, but the exhaust port may be formed. Only one of the two side walls of the flow path is disposed, and only one of them is disposed. In the present embodiment, the exhaust ports 24 and 25 are disposed in front and rear end portions of the side walls 13 and 14 and disposed on the front wall. 11 In the vicinity, there is no restriction on the position of the exhaust port. For example, 'the exhaust port can also be placed near the rear wall. Also, the exhaust port can be placed in the middle of the rear side of the side wall and the center of the front and rear direction. (Second embodiment) The second embodiment is a glass melting furnace according to the present invention. Specifically, a pair of exhaust ports are disposed in the center in the rear direction of the side wall, that is, a pair of exhaust ports are disposed. Fig. 4 is a side view showing the internal structure of the glass melting furnace of the second embodiment. Fig. 5 is a plan view showing the internal structure of the glass melting furnace of the second embodiment. In Fig. 5, the outer edge of the flame of each of the burners is indicated by a broken line. The same components as those in Fig. 2 and Fig. 3 are denoted by the same reference numerals in Fig. 4 and Fig. 5, and the description thereof is omitted. 4. As shown in Fig. 5, the melting furnace is connected to the raw material inlet 21 before the melting chamber 1 is turned on, and the wall 12 is provided with the outlet 22 after the melting chamber 1 is turned, and the raw material inlet 21 reaches the outlet 22 The side walls 13, 14 of the flow path 23 are provided with a plurality of burners 3 1A ～50A and a pair of exhaust ports 24A and 25A. The pair of exhaust ports 24A and 25A are disposed at the center in the front-rear direction of the side walls 13 and 14, and are disposed at the center between the front wall U and the rear wall 12. Left side wall 155915.doc

The exhaust port 24A of S-14-201141803 13 and the exhaust port 25 disposed on the right side wall 14 are disposed opposite to each other via the flow path 23. In the present embodiment, as in the i-th embodiment, an air burner and an oxygen burner are used as the burners 3 1A to 50A. Therefore, as in the first embodiment, the increase in the amount of enthalpy discharge can be suppressed. Further, in the present embodiment, as in the third embodiment, the total combustion heat per one hour of the plurality of burners 3 1 - 50 ( (3 〇 0 /. or more (preferably 350 / ❶ or more) 90%) The following (preferably 87% or less) is produced by an oxygen burner. Alternatively, 60% or more (preferably 68% or more) of the total heating amount Qb per hour used for heating the glass in the melting chamber 10 is 97. % or less (preferably 95% or less) is generated by an oxygen burner. Therefore, similarly to the first embodiment, it is possible to suppress a decrease in thermal efficiency or an increase in the amount of C〇2 discharged by using an air burner, n. In addition, since the decrease in the heat efficiency is suppressed, the temperature in the melting chamber is easily maintained at a relatively high temperature. Further, in the present embodiment, the self-venting port is the same as in the first embodiment. 24A and 25A are provided with at least one air burner and an oxygen burner in an area of 0.6 L or more (preferably 0.7 L or more) toward the rear. Here, L denotes an exhaust port 24A, 25A and a front wall 11 The distance L3 between the front and rear directions and between the exhaust ports 24A, 25A and the rear wall 12 The maximum distance in the distance L4 in the front-rear direction (in the example shown in Fig. 5, L3 = L4). Therefore, as in the first embodiment, it is possible to ensure the concentration of water contained in the gas after the combustion can be adjusted. In the region, the amount of water dissolved in the molten glass in the melting chamber 10 can be varied within a wide range. As a result, the amount of water dissolved in the molten glass in the melting chamber 1 155915.doc 201141803 can be sufficiently adjusted, and In the clarification step, the growth of the bubbles in the molten glass is promoted, and the floating of the bubbles is promoted, so that the glass product having less defects can be produced. The adjustment of the amount of water dissolved in the molten glass in the melting chamber is regulated by adjusting the air. The ratio of the heat of combustion to the oxygen burner per hour is set. The target of the adjustment is mainly a burner 39 ～4〇A which is disposed in an area of 0.6L or more from the exhaust σ24Α, 25A toward the rear. 49A to 50A. The higher the combustion heat ratio of the air burner with respect to the oxygen burner, the lower the concentration of water contained in the gas after combustion in the melting chamber 10, and thus the melting in the melting chamber 10. The amount of water dissolved in the glass is reduced. Here, the burners 39A to 40A and 49A to 50A which are disposed in the region which is separated from the exhaust ports 24A and 25A toward the rear by 〇6L or more are 5% of the heat of combustion Qd per hour. 95% or less (preferably 1% or less, more preferably 150/〇 or more 90〇/〇) is produced by an air burner. In the case of less than 5%, the combustion in the melting chamber 10 The concentration of water in the gas 3 is too high, and the amount of water dissolved in the molten glass in the melting chamber 10 is excessive. On the other hand, in the case of exceeding 95%, the gas in the combustion chamber 10 is burned. If the concentration of water contained is too low, the amount of water dissolved in the molten glass in the dissolution chamber 1 is too small. Further, in the present embodiment, the exhaust ports 24A and 25A are formed so that only one of the two side walls 13 and 14 of the flow path 23 is disposed to face each other, but the exhaust port may be formed only. It is disposed on one of the two side walls of the flow path and is configured by only one of them. 155915.doc -16 - 201141803 Further, in the present embodiment, at least one air burner is provided in each of the regions which are separated from the exhaust ports 24A and 25A by 0.6 L or more (preferably 0.7 L or more). The configuration of the oxygen burner is not limited to this. For example, at least one air burner and an oxygen burner may be provided in each of the regions which are separated from the exhaust ports 24A and 25A by a distance of 6 liters or more (preferably 0.7 L or more). The composition is combined. (Third Embodiment) A third embodiment relates to a glass melting furnace of the present invention. Specifically, a plurality of burners are arranged in a staggered arrangement via a flow path. Fig. 6 is a side view showing the internal structure of a glass melting furnace according to a third embodiment. Fig. 7 is a plan view showing the internal structure of a glass melting furnace according to a third embodiment. In Fig. 7, 'the outer edge of the flame of each burner is surrounded by a broken line. In FIGS. 6 and 7, the same components as those in FIGS. 2 and 3 are denoted by the same reference numerals, and their description will be omitted. As shown in Fig. 6 and Fig. 7, the melting furnace (3) is provided in the melting chamber 1B before the wall 11] B is provided with the raw material input port 21B, and after the melting chamber 10B, the wall 12B is provided with the take-out port 22B, and is taken from the raw material input port 21B. The side walls 13B and 14B of the flow path 23B of the outlet 22B are provided with a plurality of burners 31B to 33B, 41B to 42B, and a pair of exhaust ports 24B and 25B. The size of the dissolution chamber 10B is not particularly limited. For example, the dimension X3 in the front and rear directions of the melting chamber 1B is 2 to 5 m, and the dimension Y3 in the width direction of the melting chamber 10B is 1 to 3 m, and the dimension in the height direction of the melting chamber 1B is considered to be丨^ claws. The pair of exhaust ports 24B and 25B are disposed in front and rear end portions of the side walls 13B and 14B, and are disposed in the vicinity of the front wall 11B. The exhaust port 25B disposed on the left side wall 13B 155915.doc • 17· 201141803 and the exhaust port 25B disposed on the right side wall 14B are disposed to face each other across the flow path 23B. The size of the exhaust ports 24B and 25B is not particularly limited. For example, the front and rear direction dimensions X4 of the exhaust ports 24B and 25B are about 0.3 m, and the height direction dimension Z4 of the exhaust ports 24B and 25B is about 0.2 m. The plurality of burners 31B to 33B and 41B to 42B are alternately arranged via the flow path 23B. The plurality of burners 31B to 33B disposed on the left side wall 13B are arranged in the front-rear direction along the flow path 2 3 B. Similarly, the plurality of burners 41B to 42B disposed on the right side wall 14b are arranged in the front-rear direction along the flow path 23B. In the present embodiment, as in the first embodiment, an air burner and an oxygen burner are used as the burners 31B to 33B and 41B to 42B'. Therefore, as in the first embodiment, the increase in the discharge amount of C〇2 or NOx can be suppressed. Further, in the present embodiment, as in the first embodiment, the plurality of burners 3 1B to 33B and 41B to 42B have a total combustion heat amount Qa of 3% or more (preferably 35% or more) per hour. % or less (preferably 87% or less) is produced by an oxygen burner. Alternatively, 60% or more (preferably 68% or more) of the total heating amount Qb per one hour used for heating the glass in the melting chamber 10B is 97 °/. The following (more preferably 95% or less) is produced by an oxygen burner. Therefore, similarly to the first embodiment, it is possible to suppress a decrease in thermal efficiency caused by the use of an air burner, an increase in the amount of c〇2 discharged, and an increase in the amount of helium discharged. Further, since the decrease in thermal efficiency can be suppressed, the temperature in the melting chamber 10 is easily maintained at a relatively high temperature. Therefore, it is suitable for the manufacture of glass products having a high melting point. In the same manner as the first embodiment, at least 1 in each of the regions from the exhaust ports 24B and 25B that are separated by 0.6 L or more (preferably 0.7 L or more) from the exhaust ports 24B and 25B are provided. An air burner and an oxygen burner. Here, L represents the distance L5 in the front-rear direction between the exhaust ports 24B, 25B and the front wall 11B and the maximum distance L6 in the front-rear direction between the exhaust ports 24B, 25B and the rear wall 12B (Fig. In the example shown in Figure 7, it is L6). Therefore, in the same manner as in the first embodiment, the region in which the concentration of water contained in the gas after combustion can be sufficiently ensured can be made such that the amount of water dissolved in the molten glass in the melting chamber 10B can be varied over a wide range. As a result, the amount of water dissolved in the molten glass in the melting chamber 10B can be sufficiently adjusted, and in the clarification step, the growth of the bubbles in the molten glass can be promoted, and the floating of the bubbles can be promoted, thereby making it possible to manufacture a glass product having fewer defects. . The adjustment of the amount of moisture dissolved in the molten glass in the melting chamber 10B is carried out by adjusting the combustion heat ratio of the air burner to the oxygen burner every hour. The person to be the target of the adjustment is mainly the burners 33B and 42B provided in the region which is separated from the exhaust ports 24B and 25B by 〇.6L or more. The higher the ratio of the heat of combustion of the air burner to the oxygen burner, the lower the concentration of water contained in the gas after combustion in the melting chamber 10B, so that the amount of water dissolved in the molten glass in the melting chamber 10B becomes less. Here, the burners 33B and 42B provided in the region of 0.6 L or more from the exhaust ports 24B and 25B are 5% or more and 95% or less of the combustion heat amount Qd per hour (preferably ι 〇 % or more 9) 〇% or less, more preferably 15% or more and 9% or less) is produced by an air burner. Not less than 5. /. In the case of the combustion gas in the melting chamber 1〇B, I559I5.doc •19· 201141803 The water concentration is too high, and the amount of water dissolved in the molten glass in the dissolution chamber 1 〇B is excessive. On the other hand, when it exceeds 95%, the concentration of water contained in the gas after combustion in the melting chamber 1B is too low, and the amount of water dissolved in the molten glass in the melting chamber B is too small. The third embodiment of the present invention has been described above, but the present invention is not limited to the above-described embodiments, and various modifications and changes can be made to the above-described embodiments without departing from the scope of the invention. For example, as shown in Fig. 8, the glass melting furnace 1 (in general, the narrowing of the melting chamber i 〇 C into the two chambers 17 and 18 may be provided in the side walls 13C and 14C of the melting chamber 10C. At the time, the chamber 18 on the rear side is a chamber for adjusting the temperature of the molten glass, and the burner is not provided on the side wall of the chamber 8 on the rear side.

Moreover, as shown in FIG. 9, the glass melting furnace 1] can also be used in the melting chamber i〇D

The two sides J 13D, 14D are provided with the raw material investment σ 2 1D, and the exhaust port 24D is disposed on the front wall. The exhaust gas D24D may also be disposed on the front wall ud and/or the rear wall 12D. Further, as a method of heating the molten glass, in addition to the method of using the radiant heat of the flame sprayed from the burner, a method of directly heating and heating the molten glass may be used. Moreover, it is preferable that the gas mixed in the fuel of the air burner of the present invention is such that the amount of air is not changed as much as described above, and specifically, if the amount of oxygen in the gas mixed in the fuel is 25% by volume or less, Oxygen can be mixed in addition to air. Furthermore, on the side wall of the melting chamber, it is preferable to provide a viewing window for the glass melting condition (not shown), and the baffle for the observation window is opened and closed for the purpose of raising the 155915.doc 201141803. The present invention is specifically described by way of examples, but the present invention is not limited by the following examples. (Examples 1 to 10) In Examples 1 to 10 (Tables 1 and 2), β_〇Η (unit: /mm) in the glass produced by using the glass melting furnace shown in Fig. 2 and Fig. 3 was calculated by calculation. ). Ρ_〇Η is an indicator of the amount of water in the glass. It means that the larger the Ρ_〇Η, the more water in the glass. Examples 2, 4 to 6, and 10 are examples, and examples i, 3, and 7 to 9 are comparative examples. Here, the calculation method of β-ΟΗ is briefly described. First, the concentration of water contained in the gas after combustion or the like is calculated based on the composition of the fuel and gas burned by each burner. Second, consider the flow of the burned gas toward the exhaust port to calculate the distribution of the water concentration in the environment inside the melting chamber. Then, based on the distribution of the water concentration and the average flow velocity of the molten glass, the amount of water which is finally diffused into the molten glass is calculated and converted into β-ΟΗ contained in the glass after the production. In each of Examples 1 to 10, the dimension XI in the front and rear directions of the melting chamber was set to 25 m. The dimension Υ1 in the width direction of the secret chamber 10 was set to 10 m, and the dimension Z1 in the direction of dissolution to 10 was set to 8 m. Further, the volume of the molten glass in the melting chamber (7) is set to 3 〇〇m3, and the volume of the glass raw material (i.e., the molten glass taken out from the melting chamber 1 〇 #1 hour) is supplied to the melting chamber 10 every H and hour. It is set to K25 m3e, and the front and rear direction dimensions X2 of the exhaust ports 24 and 25 are set to 1 m, and the height direction dimensions of the exhaust ports 24 and 25 are 1559l5.doc -21·201141803 " Further, on the left side wall 13, the distance L1 in the front-rear direction between the front wall 丨丨 and the exhaust port 24 is set to 2 m, and each of the self-venting ports 24 to the respective burners 3 1 to 40 The distance in the rear direction is set to 2 mxN (N is a natural number of 1 to 1 )), and the distance in the rear direction between the exhaust port 24 and the burner 4 is set to 2 〇 m. Similarly, on the right side wall 4, the arrangement of the exhaust port 25 and the plurality of burners 41 to 5 are also set. Further, in each of the examples i, 2, 4, 5, and 7 to 10, each of the plurality of burners 31 to 50 is each! The heat of combustion for the hour is set to be the same. On the other hand, in Example 3, the combustion heat per hour of each of the plurality of oxygen burners is set to be the same 'the combustion heat per hour of each of the plurality of air burners is set to be the same' and the respective air is burned The heat of combustion per hour is set to be less than the heat of combustion per hour of each oxygen burner. Further, in Example 6, the heat of combustion per one hour of each of the plurality of oxygen burners is set to be the same 'the combustion heat per hour of each of the plurality of air burners is set to be the same' and each of the air burners is 1 The heat of combustion for hours is set to be greater than the heat of combustion per hour of each oxygen burner. Further, as the burners 31 to 50 of Examples 1 and 9, only an oxygen burner was used, and as the burners 31 to 50 of Examples 2-8 and 10, an oxygen burner and an air burner were used. In Tables 1 and 2, the unit Nm3 of the C02 discharge amount indicates the volume in the standard state (〇°C, 1 atm) (the same applies to Table 3 and Table 4). In Tables 1 and 2, the No. (number) of the air burner is shown, so the No. of the oxygen burner is omitted (the same applies to Table 3 and Table 4). 155915.doc -22- 201141803 [Table l] Example 1 Example 2 Example 3 Example 4 Example 5 Oxygen burner fuel Natural gas Natural gas Natural gas Natural gas air burner No_ - 38, 48 38, 48 38 32, 38, 42 48 Air Burner Fuel - Natural Gas Natural Gas Natural Gas Burning Heat per 1 hour Qa(kWh) 10000 12200 10200 11100 14300 Contribution Rate of Oxygen Burner to Qa (%) 100 74 91 87 56 Total Heating per 1 hour Qb (kWh) 7300 7300 7300 7300 7300 Contribution rate of oxygen burner to Qb (%) 100 90 99 95 80 C02 discharge per hour (Nm3/h) 1050 1250 1050 1150 1475 Distance L(m) 22 22 22 22 22 Distance in the front-rear direction between the exhaust port and the air burner farthest from the exhaust port La(m) - 16 16 16 16 La/L - 0.73 0.73 0.73 0.73 Air burner relative to specific area Contribution rate (%) of total heat of combustion Qd per hour - 51 9 20 51 p-OH(mm') 0.50 0.39 0.47 0.42 0.37 [Table 2] Example 6 Example 7 Example 8 Example 9 Example 10 Oxygen burner Fuel Natural Gas Natural Gas Heavy Oil Heavy Oil Air Burner No. 38, 48 32'42 3 32, 41 > 42 - 38, 48 Air Burner Fuel Natural Gas Natural Gas - Total Combustion Heat per 1 hour of Heavy Oil Qa(kWh) 17800 12200 14300 9700 11800 Contribution Rate of Oxygen Burner to Qa (%) 36 74 56 100 74 Total heating per hour Qb (kWh) 7300 7300 7300 7300 7300 Contribution rate of oxygen burner to Qb (%) 64 90 80 100 90 . C02 emissions per hour (Nm3/h) 1830 1250 1475 1350 1500 Distance L(m) 22 22 22 22 22 Distance in the front-rear direction between the exhaust port and the air burner farthest from the exhaust port La(m) 16 4 2 - 16 La/L 0.73 0.18 0.09 - 0.73 Contribution rate of air burner to total combustion heat Qd per hour for a specific area (%) 84 0 0 - 51 β-ΟΗΟηηι·1) 0.32 0.47 0.46 0.40 0.32 •23- 155915.doc 201141803 As understood from Tables 1 and 2, in the examples 1 to 8 in which the fuel is natural gas, in the examples 2 and 4 to 6, in the region which is separated from the exhaust ports 24 and 25 toward the rear by 〇.6L or more, each of them is provided with at least 1 For the air burner and the oxygen burner, the β-OH in the glass was reduced by more than 10% compared with the case of Example 1. Further, in the case of the example 9 and 1 in which the fuel is heavy oil, in the example 10, at least one air burner and the oxygen burner are provided in each of the regions which are separated from the exhaust ports 24 and 25 by 0.6 L or more. 'Compared with the case of Example 9, β_〇Η in the glass decreased by 1 〇. Above /0. If it is lowered by 10% or more, the combustion heat ratio per hour of the air burner and the oxygen burner is changed, whereby β_〇Η can be sufficiently adjusted. Therefore, in Examples 2, 4 to 6, and 1 ', the moisture content of the f-storage in the molten glass in the melting chamber 1 can be sufficiently adjusted by adjusting the ratio of the combustion heat per hour of the air burner to the oxygen burner. . On the other hand, in Examples 7 and 8, in the region where the exhaust ports 24 and 25 were separated by 0.6 L or more from the rear, no air burner was provided, so that the sample 1 'β-ΟΗ did not fall by 1% or more. . From this, it was judged that even if the ratio of the heat of combustion of the air burner to the oxygen burner per hour was adjusted, it was difficult to sufficiently adjust the amount of water dissolved in the molten glass in the escapement chamber 10. In the same manner as in the example 2, at least one air burner and the oxygen burner are provided in each of the regions which are separated from the exhaust ports 24 and 25 by 0.6 L or more, but different from the example 2, 99% of the total heating amount Qb per hour used for heating the glass in the melting chamber is generated by an oxygen burner. Therefore, the β·〇Η in the glass in Example 3 was not lowered by 10 Å/〇 or more with respect to Example 1. From this, it was judged that in Example 3, it was difficult to sufficiently reduce the amount of water dissolved in the molten glass in the melting chamber. 155915.doc

S • 24· 201141803 (Examples 11 to 12) In Examples 11 to 12 (Table 3), β-ΟΗ in the glass produced by using the glass refining furnace shown in Figs. 4 and 5 was obtained by the above calculation. Unit: /mm). Example 12 is an example, and Example 11 is a comparative example. In each of the examples 11 to 12, the exhaust ports 24A and 25A are disposed in the center in the front and rear directions of the side walls 13 and 14, and the size of the melting chamber, the size of the exhaust port, the exhaust port, and each burner are used. The distance between the front and rear directions and the like are set in the same manner as in the examples 1 to 10. In each of Examples 11 to 12, the heat of combustion per one hour of each of the plurality of burners 31A to 50A was set to be the same. Further, as the burners 3 1A to 50A of Example 11, only an oxygen burner was used, and as the burners 31A to 50A of Example 12, an oxygen burner and an air burner were used. [Table 3] Example 11 Example 12 Oxygen burner fuel Natural gas Natural gas air burner No. - 39A, 49A Air burner fuel - Natural gas total combustion heat per hour Qa (kWh) 10000 12200 Oxygen burner relative to Contribution rate of Qa (%) 100 74 Total heating amount per hour Qb (kWh) 7300 7300 Contribution rate of oxygen burner to Qb (%) 100 90 CO2 emission per hour (Nm3/h) 1050 1250 Distance between the L(m) 12 12 exhaust port and the air burner farthest from the exhaust port in the front-rear direction La(m) - 8 La/L - 0.67 Air burner per 1 specific area Contribution rate (%) of total combustion heat Qd in hours - 51 P-OH (mm'') 0.51 0.45 As understood from Table 3, in Example 12, from the exhaust ports 24A, 25A toward the rear 155915.doc -25 - 201141803 In the area where the distance is 0.6L or more, each of the air burners and the oxygen burner is provided. Compared with the case of Example 11, the p_〇H in the glass is decreased by more than 1%. From this, it was judged that in Example 12, the amount of moisture dissolved in the glazing glass in the melting chamber 1 可 was sufficiently adjusted by adjusting the ratio of the combustion heat per hour of the air burner to the oxy-combustion burner. (Examples 13 to 14) In Examples 13 to 14 (Table 4), β_0Η (unit: /mm) in the glass produced by 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. In each of Examples 13 to 14, the melting direction of the melting chamber 10B was set to 3 m, the width direction γ3 of the melting chamber 10B was set to 2 m, and the height direction dimension 23 of the melting chamber 10B was set to 2 me. , set the volume of the molten glass in the melting chamber i〇b to 4.5 m3, which will be! The volume of the glass raw material (i.e., the smelting glass taken out from the refining chamber) which is melted into 10B is set to 〇〇4 m3 〇 and then the exhaust port 24b, 25B is set to the front and rear direction size X4. 〇.3 m, the height direction dimension Z4 of the exhaust ports 24B, 25B is set to 0 3 m. Further, in the left side wall nB, the distance l5 in the front-rear direction between the front wall 1 and the exhaust port 24B is set to 〇.2 m 'the distance between the exhaust port 24B and the burner 31B in the front-rear direction. Let 疋.3 m ' set the distance in the front-rear direction between the exhaust port 24B and the burner 32B to 10 m, and set the distance in the front-rear direction between the exhaust port 24B and the burner 33B to 2 〇m. On the other hand, in the right side wall 1, the distance L5 in the front-rear direction between the front wall 11B and the exhaust port 25B is set to 〇·2 m 'the front and rear direction between the exhaust port 25B and the burner 41B, respectively. 155915.doc

The distance on S • 26· 201141803 is set to 0.5 m, and the distance between the exhaust port 25B and the burner 42B in the front-rear direction is set to 1.5 m. Further, in each of Examples 13 to 14, the heat of combustion per one hour of each of the plurality of burners 31B to 33B and 41B to 42B was set to be the same. Further, as the burners 31B to 33B and 41B to 42B of the example 13, only the oxygen burner was used, and as the burners 31B to 33B and 41B to 42B of the example 14, the oxygen burner and the air burner were used. [Table 4] Example 13 Example 14 Fuel of Oxygen Burner Natural Gas Air Burner No. - 42B Fuel of Air Burner - Total Combustion Heat per Natural Gas Qa (kWh) 500 720 Oxygen Burner Relative to Qa Contribution rate (%) 100 56 Total heating amount per hour Qb (kWh) 370 370 Contribution rate of oxygen burner to Qb (%) 100 80 C02 emission per hour (Nm3/h) 50 75 Distance L (m) 2.5 Distance between the exhaust port and the air burner farthest from the exhaust port in the front-rear direction La(m) - 1.5 La/L - 0.6 Total of the air burner per hour for a specific area The contribution rate (%) of the heat of combustion Qd - 76 p - OH (mm · )) 0.52 0.46 As understood from Table 4, in the example 14, in the region which is separated from the exhaust ports 24B, 25B by 0.6 L or more, Each of the air burners and the oxygen burners was provided, and the β-ΟΗ in the glass plate was reduced by 10% or more as compared with the case of Example 13. From this, it was judged that in Example 14, the amount of moisture dissolved in the molten glass in the melting chamber 10 was sufficiently adjusted by adjusting the ratio of the combustion heat per hour of the air burner to the oxygen burner. The present invention has been described in detail above with reference to the specific embodiments thereof. However, it is to be understood that those skilled in the art can make various changes or modifications in the spirit and scope of the invention. The present application is based on a patent application No. 2010-101312 filed on Apr. 26, 2010, the content of which is hereby incorporated by reference. Industrial Applicability According to the present invention, it is possible to provide a glass melting furnace capable of suppressing an increase in the amount of NOx discharged and sufficiently adjusting the amount of water dissolved in the molten glass. This glass melting furnace is particularly effective in the case where the molten glass is sufficiently heated and the moisture content is lowered. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a view showing the steps of a method for producing a glass product according to an embodiment of the present invention. Fig. 2 is a side view showing the internal structure of the glass melting furnace of the first embodiment. Fig. 3 is a plan view showing the internal structure of the glass melting furnace of the first embodiment. Fig. 4 is a side view showing the internal structure of a glass melting furnace according to a second embodiment. Fig. 5 is a plan view showing the internal structure of a glass melting furnace according to a second embodiment. Fig. 6 is a side view showing the internal structure of the glass decontamination furnace of the third embodiment. Fig. 7 is a plan view showing the internal structure of a glass melting furnace according to a third embodiment. Fig. 8 is a plan view showing a modification of the internal structure of the glass melting furnace. Fig. 9 is a plan view showing another modification of the internal structure of the glass melting furnace. [Main component symbol description] 1, 1A, IB, 1D melting furnace 10, 10B, l〇C, 10D melting chamber 11, 11B, 11C, 11D front wall 155915.doc

S 201141803 12, 12B, 12D Rear wall 13, 13B, 13C, 13D Side wall (left side wall) 14, 14B, 14C, 14D Side wall (right side wall) 15 Melting tank 16 Ceiling 17 ' 18 Chamber 19 Constricted neck 21, 21B, 21D raw material input port 22, 22B take-out port 23, 23B flow path 24, 24B, 24C, 25, 25B, 25C exhaust port 31 to 50, 31B-33B, 41B to 42B burner G1 glass material G2 molten glass L, LI , L2, L3, L4, L5, L6 Distance XI, X2, X3, X4 Front and back direction dimension Yl, Y3 Width direction dimension Zl, Z2, Z3, Z4 South dimension size 155915.doc -29-

Claims (1)

201141803 VII. Patent application scope: 1. A glass melting furnace comprising a melting chamber for melting glass raw materials, and a plurality of burners disposed on sidewalls of the flow path of the melting chamber from the front wall to the rear wall. The burner extracts a flame into the melting chamber to heat and melt the glass in the melting chamber; the plurality of burners use an oxygen burner that sprays a flame generated by mixing the fuel with oxygen and combusts, and ejects the fuel The air burner of the flame which is mixed with air and burns the flame generated by the above-mentioned plurality of burners, which is generated by the above-mentioned oxygen burner, is used to make The exhaust port in which the gas after combustion in the melting chamber is exhausted to the outside is disposed on only one of the two side walls of the melting chamber, and is disposed only on one of the two side walls of the dissolution chamber. One, or disposed on the front wall or the rear wall of the melting chamber, and the distance between the exhaust port and the front wall in the front-rear direction and the exhaust port and the upper portion The distance between the rear wall of the front-rear direction of the maximum distance is L, then from the exhaust port in the forward and / or rearward away from the area above 0.6L, each provided with at least! The oxygen burner and the air burner are produced by the air burner in an amount of 5% or more and 95% or less of the total combustion heat per hour of the burner installed in the region. 2. The glass melting furnace of claim 1, wherein at least two of said air burners are arranged at a side wall of said melting chamber, and at least one of said oxygen is disposed between said two air burners burner. I55915.doc 201141803 3. A method of melting a glass using the glass melting furnace of claim 1 or 2. 155915.doc 2-