Energy-saving process for decomposing glass batch outside kiln and feeding glass batch into kiln

Abstract

The invention relates to the technical field of glass production, and particularly discloses an energy-saving process for decomposing glass batch into a kiln outside, which comprises the following steps of: adding liquid fuel in the mixing process of a mixer in advance, pushing the batch to a plate conveyor by an inclined blanket type batch feeder, forwards conveying the batch containing the liquid fuel by the plate conveyor, and synchronously preheating; when the batch containing the liquid fuel is conveyed to the joint of the preheating furnace and the decomposing furnace, the temperature of the batch containing the liquid fuel is controlled to be 550 + / -10 DEG C, carbonate is continuously decomposed, and when a batch sintering solid solution with most of the decomposed carbonate is conveyed to the joint of the kiln-entering high-temperature slide way, the temperature of the batch sintering solid solution is controlled to be 550 + / -10 DEG C; the temperature of a batch sintering solid solution is controlled to be 880 + / -10 DEG C, finally, the batch slides into a kiln through a kiln-entering high-temperature slide way, the batch does not need to maintain the temperature all the time in a preheating furnace and a decomposing furnace, most carbonate is decomposed before the batch enters the kiln, and the purposes of shortening the size of the kiln, reducing the number of small furnaces and saving energy are achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of glass production, and particularly relates to an energy-saving process for pre-decomposing glass batch outside the kiln and then feeding it into the kiln. Background Art

[0002] Traditional glass batch is to mix raw materials such as quartz sand, feldspar, dolomite, limestone, soda ash, and mirabilite with a certain particle size in proportion, and then transport them to the melting furnace in a loose state for melting operation. Its disadvantage is that the batch is in a piled state in the melting furnace, covered with a gas foam layer, with poor thermal conductivity. Coupled with the relatively large space in the melting furnace and the relatively fast flow rate of the combustion flue gas, a large amount of heat is carried away by the flue gas in the kiln, resulting in high energy consumption.

[0003] In order to reduce energy consumption, the applicant retrieved a Chinese invention patent with a publication number of CN103102057A, which discloses moving the carbonate decomposition process with huge heat consumption out of the melting furnace and using a calciner outside the kiln to achieve high energy efficiency. Specifically, this technical solution is to pre-heat and decompose carbonate mineral raw materials such as dolomite and limestone in the calciner, and then mix the decomposed products with other glass raw materials to prepare the batch, which is granulated and then fed into the kiln. Its disadvantage is that the mineral raw materials decomposed by heating in the calciner will cool down during subsequent storage and weighing, losing a large amount of heat energy. Then, the glass batch at room temperature needs to be heated again during the melting process, so the energy-saving effect is limited. In order to overcome the defects of the above-mentioned pre-decomposition process outside the kiln, the inventor purposefully provides an energy-saving process for pre-decomposing glass batch outside the kiln and then feeding it into the kiln, which is simple, ingenious and easy to implement. Summary of the Invention

[0004] The purpose of the present invention is to provide an energy-saving process for pre-decomposing glass batch outside the kiln and then feeding it into the kiln, which is simple, ingenious and easy to implement, so as to solve the technical problem that the pre-decomposition process outside the kiln in the prior art needs to reheat the batch, resulting in poor energy-saving effect.

[0005] The purpose of the present invention can be achieved by the following technical solutions: An energy-saving process for pre-decomposing glass batch outside the kiln and then feeding it into the kiln, the specific steps of which are as follows: S1: Add a small amount of low-viscosity liquid fuel to the batch in advance. The liquid fuel is ethylene tar or heavy diesel, and the mass percentage of the liquid fuel to the batch is less than 1.5%. Use a mixer to mix the batch containing the liquid fuel to ensure that its uniformity meets the production requirements of the glass batch; S2: Use a belt conveyor to transport the batch containing the liquid fuel discharged from the mixer to a heat-insulated kiln head bin, and at this time, the bin gate of the kiln head bin is in a closed state; S3: Open the bunker gate. The discharging rate can be controlled by adjusting the opening size of the bunker gate. The inclined blanket feeder located below the bunker gate receives the batch material containing liquid fuel and pushes it onto the plate conveyor in the preheating furnace. The plate conveyor conveys the batch material containing liquid fuel forward and preheats it synchronously. When the batch material containing liquid fuel is conveyed to the connection between the preheating furnace and the decomposition furnace, the temperature of the batch material containing liquid fuel and already starting carbonate decomposition is controlled at 550 ± 10 °C. S4: The plate conveyor runs continuously, and in the decomposition furnace, it continues to convey the batch material that has started carbonate decomposition forward and the carbonate continues to decompose. When the sintered solid melt of the batch material with most of the carbonates decomposed is conveyed to the connection between the decomposition furnace and the high-temperature chute leading to the kiln, the temperature of the sintered solid melt of the batch material is controlled at 880 ± 10 °C. S5: The sintered solid melt of the batch material slides into the kiln through the high-temperature chute leading to the kiln composed of fused cast bricks, and the temperature from the end of the decomposition furnace to the high-temperature chute leading to the kiln is maintained within the range of 880 ± 10 °C.

[0006] As a further optimization or improvement of this solution.

[0007] In S3, fuel is sprayed into the preheating furnace through multiple fuel nozzles opened on the side of the preheating furnace for combustion heating. The fuel sprayed into the preheating furnace heats the batch material by combustion from the outside to the inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside by combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor until the temperature of the batch material containing liquid fuel and already starting carbonate decomposition is controlled at 550 ± 10 °C when it is conveyed to the connection between the preheating furnace and the decomposition furnace. The fuel injection amount of the multiple fuel nozzles on the side of the preheating furnace gradually increases along the conveying direction of the plate conveyor.

[0008] As a further optimization or improvement of this solution.

[0009] In S3, electric heating is directly set on the side of the preheating furnace for heating. The electric heating heats the batch material from the outside to the inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside by combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor until the temperature of the batch material containing liquid fuel and already starting carbonate decomposition is controlled at 550 ± 10 °C when it is conveyed to the connection between the preheating furnace and the decomposition furnace. The electric heating power on the side of the preheating furnace gradually increases along the conveying direction of the plate conveyor.

[0010] As a further optimization or improvement of this solution.

[0011] In S4, fuel is injected into the decomposition furnace through multiple fuel nozzles opened on the side of the decomposition furnace for combustion heating. The fuel injected into the decomposition furnace heats the batch material from the outside to the inside through combustion. At the same time, the liquid fuel contained in the batch material on the plate conveyor continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside through combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor until it is conveyed to the connection between the decomposition furnace and the high-temperature slideway of the kiln inlet, and the temperature of the sintered solid melt of the batch material is controlled at 880 ± 10 °C; The fuel injection amount of multiple fuel nozzles on the side of the decomposition furnace gradually increases along the conveying direction of the plate conveyor.

[0012] As a further optimization or improvement of this solution.

[0013] In S4, electric heating is directly arranged on the side of the decomposition furnace for heating. The electric heating heats the batch material from the outside to the inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside through combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor until it is conveyed to the connection between the decomposition furnace and the high-temperature slideway of the kiln inlet, and the temperature of the sintered solid melt of the batch material is controlled at 880 ± 10 °C; The electric heating power on the side of the decomposition furnace gradually increases along the conveying direction of the plate conveyor.

[0014] As a further optimization or improvement of this solution.

[0015] The combustion-supporting air of the preheating furnace and the decomposition furnace is introduced from the top of the regenerator of the existing glass kiln. The temperature of the combustion-supporting air is 1000 °C. The introduced combustion-supporting air with a relatively high temperature enters the decomposition furnace from the outlet of the decomposition furnace after adjusting the air volume, and then enters the preheating furnace. The flow direction of the combustion-supporting air is opposite to the conveying direction of the plate conveyor.

[0016] As a further optimization or improvement of this solution.

[0017] A combustion-supporting air channel is arranged between the upper part of the hanging flat arch at the outlet of the decomposition furnace and the regenerator of the small furnace of the glass kiln. A combustion-supporting air regulating damper for controlling the opening and closing size of the channel is arranged on the combustion-supporting air channel. The hot air in the combustion-supporting air pipe enters the decomposition furnace through the upper part of the connection between the decomposition furnace and the hanging flat arch.

[0018] As a further optimization or improvement of this solution.

[0019] The inclined blanket feeder, preheating furnace, decomposition furnace, high-temperature slideway into the kiln and the front end of the glass kiln are completely sealed and thermally insulated.

[0020] As a further optimization or improvement of this solution.

[0021] The conveying method of the plate conveyor is the relay pushing of the thrust plates. Each thrust plate on the plate conveyor is higher than the lower one, and each thrust plate moves reciprocally independently, continuously pushing the upper layer of batch material onto the lower layer of thrust plates.

[0022] Advantages of the present invention: 1. In this process, liquid fuel is added to the batch material, and liquid or gaseous fuel is added from the fuel nozzles or the electric heating method is adopted, which can realize the simultaneous combustion and decomposition inside and outside the batch material. The batch material is uniformly heated inside and outside, and less fuel is required for the decomposition of the same mass of batch material, thus achieving energy saving.

[0023] 2. In this process, as the plate conveyor gradually advances, due to the insufficient oxygen in the preheating furnace and the decomposition furnace, the fuel will not all burn concentratedly in the preheating furnace. Instead, with the advancement of the plate conveyor and the reverse movement of the combustion-supporting air volume and the running direction of the batch material, the fuel shows a gradually burning phenomenon. Relatively speaking, as the temperature of the batch material gradually increases, the decomposition reaction rate of carbonate gradually accelerates. It only needs to reach 880 ± 10 °C before entering the kiln and most of the carbonate is decomposed, without the batch material maintaining 880 ± 10 °C in the preheating furnace and the decomposition furnace all the time, thereby achieving the purpose of energy saving.

[0024] 3. In this process, since the fuel nozzles of the preheating furnace and the decomposition furnace are separated from the outlet of the combustion-supporting air channel 9, only a part of the injected fuel will burn due to insufficient oxygen supply, and the remaining part will fall onto the surface of the batch material and gradually burn as the plate conveyor moves forward, promoting the direct contact between the gaseous fuel and the batch material and improving the efficiency of heat conduction, thereby achieving energy saving. Description of the drawings

[0025] The present invention will be further described below in conjunction with the drawings.

[0026] Figure 1 It is a schematic diagram of the overall structure of the present invention.

[0027] The labels in the figure are: 1. Kiln head bin; 2. Bin gate; 3. Inclined blanket feeder; 4. Preheating furnace; 5. Fuel nozzle; 6. Decomposition furnace; 7. Hanging flat arch; 8. Combustion-supporting air regulating damper; 9. Combustion-supporting air channel; 10. Plate conveyor; 11. High-temperature slideway into the kiln; 12. Glass kiln regenerator. Specific embodiments

[0028] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0029] First of all, it should be noted that: The structure shown in the Figure 1 specification drawings can be obtained by the conventional layout of the glass furnace in the prior art. Among them, the kiln head bin 1, the bin gate 2, the inclined blanket feeder 3, the preheating furnace 4, the fuel nozzle 5, the decomposition furnace 6, the hanging flat arch 7, the combustion air regulating damper 8, the combustion air channel 9, the plate conveyor 10, the high-temperature slideway into the kiln 11, and the glass furnace port regenerator 12 are all common knowledge of those skilled in the art and will not be described in detail. The focus of the present invention lies in the process of decomposition outside the kiln.

[0030] Furthermore, it is also necessary to introduce that the polymorphic transformation and changes of each component of the glass batch during heating are as follows in the table:

[0031] Through the data analysis of the above table: 1. MgNa2(CO3)2 is generated at < 300 °C 2. MgCO3 starts to decompose at 300 °C 3. CaNa2(CO3)2 starts to be generated at < 400 °C 4. CaCO3 starts to decompose at 420 °C 5. MgNa2(CO3)2 + 2SiO2 → MgSiO3 + Na2SiO3 + 2CO2 at 340 - 620 °C 6. MgCO3 + SiO2 → MgSiO3 + CO2 at 450 - 700 °C 7. CaNa2(CO3)2 + 2SiO2 → CaSiO3 + Na2SiO3 + 2CO2 at 585 - 900 °C 8. Na2CO3 + SiO2 → Na2SiO3 + CO2 at the stage of violent reaction at 700 - 900 °C 9. CaCO3 + SiO2 → CaSiO3 + CO2 at 600 - 920 °C 10. The decomposition of MgCO3 reaches the highest speed at 620 °C 11. The liquid phase caused by the eutectic mixture of MgSiO3, Na2SiO3, SiO2, double silicate of silicic acid and Na2SiO3 and Na2CO3 starts to appear at 780 - 880 °C. 12. The decomposition of CaCO3 reaches the highest speed at 915 °C. 13. The stage where the reaction of MgO + SiO2 → MgSiO3 proceeds vigorously is at 980 - 1150 °C. 14. The stage where the reaction of CaO + SiO2 → CaSiO3 proceeds vigorously is at 1010 - 1150 °C. 15. The double silicate of silicic acid CaSiO3MgSiO3 is formed from CaSiO3 and MgSiO3 at 600 - 1200 °C. 16. Quartz particles, calcium silicate and magnesium silicate dissolve in the melt at 1150 - 1200 °C. It can be seen from the above reactions that calcium carbonate starts to decompose at 420 °C and the decomposition rate gradually increases with the increase of temperature. Magnesium carbonate reaches the highest decomposition speed at 620 °C. Below 915 °C, the decomposition reaction of the carbonates in the batch is basically completed and a partial liquid phase eutectic is produced (the appearance of the batch is a sintered block solid solution). Theoretically, 915 °C is an ideal temperature for decomposition outside the kiln. In this temperature range, the carbonates are basically decomposed. Considering the equipment investment and the influence of high temperature on the material properties, the goal of decomposition outside the kiln is to generate a eutectic mixture (i.e., a sintered block solid solution), and it is only necessary to meet the requirement of rapid melting after entering the kiln. Therefore, it is more appropriate to set the temperature of the batch after decomposition outside the kiln and entering the kiln at 880 °C, which can basically meet the process goal of decomposition outside the kiln. This case is also implemented based on the above control of the temperature of the batch after decomposition outside the kiln and entering the kiln at 880 ± 10 °C.

[0032] See Figure 1 , an energy-saving process for the batch decomposition outside the kiln and entering the kiln of glass batch, and its specific steps are as follows: S1: Add a small amount of low-viscosity liquid fuel to the batch in advance. The liquid fuel is ethylene tar or heavy diesel, and the mass percentage of the liquid fuel to the batch is less than 1.5%. The mixer mixes the batch containing the liquid fuel to ensure that its uniformity meets the requirements for the production of glass batch.

[0033] S2: Use a belt conveyor to transport the batch containing the liquid fuel discharged from the mixer to the heat-insulated kiln head bin 1. At this time, the bin gate 2 of the kiln head bin 1 is in the closed state.

[0034] S3: Open the silo gate 2. The discharging rate can be controlled by adjusting the opening size of the silo gate 2. The inclined blanket feeder 3 located below the silo gate 2 receives the batch material containing liquid fuel and pushes it onto the plate conveyor 10 in the preheating furnace 4. The plate conveyor 10 conveys the batch material containing liquid fuel forward and preheats it synchronously. When the batch material containing liquid fuel is conveyed to the connection between the preheating furnace 4 and the decomposition furnace 6, the temperature of the batch material containing liquid fuel and already starting carbonate decomposition is controlled at 550 ± 10 °C.

[0035] Specifically, fuel is injected into the preheating furnace 4 through multiple fuel nozzles 5 opened on the side of the preheating furnace 4 for combustion heating. The fuel is liquid fuel or gas fuel. It is also possible to directly set electric heating on the side of the preheating furnace 4 without opening the fuel nozzles 5 for heating. The fuel injected into the preheating furnace 4 heats the batch material through combustion from the outside to the inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor 10 continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside through combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor 10 until the temperature of the batch material containing liquid fuel and already starting carbonate decomposition is controlled at 550 ± 10 °C when it is conveyed to the connection between the preheating furnace 4 and the decomposition furnace 6.

[0036] More specifically, the fuel injection amount of multiple fuel nozzles 5 on the side of the preheating furnace 4 gradually increases along the conveying direction of the plate conveyor 10; or the electric heating power on the side of the preheating furnace 4 gradually increases along the conveying direction of the plate conveyor 10, so as to realize the process that the temperature of the batch material gradually increases as the plate conveyor 10 gradually advances.

[0037] S4: The plate conveyor 10 runs continuously, and continues to convey the batch material that has started carbonate decomposition forward in the decomposition furnace 6 and the carbonate continues to decompose. When the sintered solid melt of the batch material in which most of the carbonates have decomposed is conveyed to the connection between the decomposition furnace 6 and the high-temperature chute 11 leading to the kiln, the temperature of the sintered solid melt of the batch material is controlled at 880 ± 10 °C.

[0038] Specifically, fuel is injected into the decomposition furnace 6 through multiple fuel nozzles 5 opened on the side of the decomposition furnace 6 for combustion heating. The fuel is liquid fuel or gas fuel. It is also possible to directly set electric heating on the side of the decomposition furnace 6 without opening the fuel nozzles 5 for heating. The fuel injected into the decomposition furnace 6 heats the batch material through combustion from the outside to the inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor 10 continues to burn, and the liquid fuel contained in the batch material heats the batch material from the inside to the outside through combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor 10 until the temperature of the sintered solid melt of the batch material is controlled at 880 ± 10 °C when it is conveyed to the connection between the decomposition furnace 6 and the high-temperature chute 11 leading to the kiln.

[0039] More specifically, the fuel injection amounts of multiple fuel nozzles 5 on the side of the decomposition furnace 6 gradually increase along the conveying direction of the plate conveyor 10; or the electric heating power on the side of the decomposition furnace 6 gradually increases along the conveying direction of the plate conveyor 10, so as to realize the process that the temperature of the batch gradually increases as the plate conveyor 10 gradually advances.

[0040] S5: The batch sintered solid solution slides into the kiln through the high-temperature slideway 11 into the kiln composed of fused cast bricks, and the temperature from the tail end of the decomposition furnace 6 to the high-temperature slideway 11 into the kiln is maintained within the range of 880 ± 10 °C.

[0041] See Figure 1 , the combustion-supporting air of the preheating furnace 4 and the decomposition furnace 6 is introduced from the top of the regenerator of the existing glass kiln. The temperature of the combustion-supporting air is about 1000 °C. The introduced combustion-supporting air with a relatively high temperature enters the decomposition furnace 6 from the outlet of the decomposition furnace 6 after adjusting the air volume, and then enters the preheating furnace 4. The flow direction of the combustion-supporting air is opposite to the conveying direction of the plate conveyor 10. As the combustion-supporting air flows, its temperature gradually decreases, which also promotes the temperature of the batch to gradually increase as the plate conveyor 10 gradually conveys, and this can also realize the process that the temperature of the batch gradually increases as it advances.

[0042] Specifically, a combustion-supporting air channel 9 is provided between the upper part of the hanging flat arch 7 at the outlet of the decomposition furnace 6 and the regenerator of the small furnace of the glass kiln 12. A combustion-supporting air regulating damper 8 for controlling the opening and closing size of the channel is provided on the combustion-supporting air channel 9. The hot air in the combustion-supporting air pipe enters the decomposition furnace 6 from above the connection between the decomposition furnace 6 and the hanging flat arch 7, and its air volume is adjusted by the combustion-supporting air regulating damper 8.

[0043] The inclined blanket type feeder 3, the preheating furnace 4, the decomposition furnace 6, the high-temperature slideway 11 into the kiln and the front end of the glass kiln are hermetically and thermally insulated and connected.

[0044] The conveying mode of the plate conveyor 10 is the relay pushing of the thrust plates. Each layer of thrust plates on the plate conveyor 10 is higher than the lower layer of thrust plates. Each thrust plate moves reciprocally independently, and continuously pushes the batch on the upper layer to the thrust plate on the lower layer.

[0045] The specific energy-saving principle of the energy-saving process into the kiln disclosed in this technical solution is: First: In this process, liquid fuel is added to the batch. Liquid fuel or gaseous fuel is added from the fuel nozzle 5, or by electric heating method, which can realize the simultaneous combustion and decomposition inside and outside the batch. The batch is heated evenly inside and outside, and less fuel is required for the decomposition of the batch with the same mass fraction, thus realizing energy saving.

[0046] Second: In this process, as the plate conveyor 10 gradually advances, due to the insufficient oxygen in the preheating furnace 4 and the decomposition furnace 6, not all of the fuel will be concentrated and burned in the preheating furnace. Instead, as the plate conveyor advances and the combustion-supporting air volume moves in the opposite direction to the running direction of the batch material, the fuel shows a gradual combustion phenomenon. Relatively speaking, with the temperature gradually increasing, the decomposition reaction rate of the carbonate accelerates. It only needs to reach 880 ± 10 °C before entering the kiln and the carbonate is completely decomposed, without the batch material having to maintain 880 ± 10 °C in the preheating furnace 4 and the decomposition furnace 6 all the time, thereby achieving the purpose of energy conservation.

[0047] Third: In this process, since the fuel nozzles 5 of the preheating furnace 4 and the decomposition furnace 6 are separated from the outlets of the combustion-supporting air channels 9, the injected gaseous fuel will only burn a part due to insufficient oxygen supply, and the remaining part will fall onto the surface of the batch material and gradually burn as the plate conveyor 10 moves forward, promoting the direct contact between the gaseous fuel and the batch material, improving the efficiency of heat conduction, and thus achieving energy conservation.

[0048] In this case, there are two important temperature control nodes, that is, when the batch material is conveyed to the tail end of the preheating furnace 4, the temperature of the batch material is controlled at 550 ± 10 °C, and when the batch material is conveyed to the tail end of the decomposition furnace 6, the temperature of the batch material is controlled at 880 ± 10 °C. It can be controlled by the addition amount of the liquid fuel in the batch material, the fuel injection amount or the electric heating power in the preheating furnace 4 or the decomposition furnace 6, and the air volume of the combustion-supporting air. It is very easy to achieve in combination with conventional temperature control technologies and will not be elaborated here.

[0049] The above has described a specific embodiment of the present invention in detail, but the content described is only the preferred embodiment of the present invention and cannot be considered as limiting the scope of implementation of the present invention. All equivalent changes and improvements made according to the scope of the application of the present invention should still fall within the scope covered by the patent of the present invention.

Claims

1. An energy-saving process for pre-decomposing and feeding into the kiln of a glass batch, characterized in that: The specific steps are as follows: S1: Add a small amount of low-viscosity liquid fuel to the batch in advance. The liquid fuel is ethylene tar or heavy diesel, and the mass percentage of the liquid fuel to the batch is less than 1.5%. The mixer mixes the batch containing the liquid fuel to ensure that its uniformity meets the requirements for the production of glass batch. S2: Use a belt conveyor to transport the batch containing the liquid fuel discharged from the mixer to the heat-insulated kiln head bin (1). At this time, the bin gate (2) of the kiln head bin (1) is in the closed state. S3: Open the bin gate (2). The discharge rate can be controlled by adjusting the opening size of the bin gate (2). The inclined blanket feeder (3) located below the bin gate (2) receives the batch containing the liquid fuel and pushes it onto the plate conveyor (10) in the preheating furnace (4). The plate conveyor (10) transports the batch containing the liquid fuel forward and preheats it synchronously. When the batch containing the liquid fuel is transported to the connection between the preheating furnace (4) and the decomposition furnace (6), control the temperature of the batch containing the liquid fuel that has started carbonate decomposition at 550 ± 10 °C. S4: The plate conveyor (10) runs continuously, and continues to transport the batch that has started carbonate decomposition forward in the decomposition furnace (6) and the carbonate continues to decompose. When the sintered solid melt of the batch in which most of the carbonates have decomposed is transported to the connection between the decomposition furnace (6) and the high-temperature slideway (11) entering the kiln, control the temperature of the sintered solid melt of the batch at 880 ± 10 °C. S5: The sintered solid melt of the batch slides into the kiln through the high-temperature slideway (11) entering the kiln composed of fused cast bricks. The temperature from the end of the decomposition furnace (6) to the high-temperature slideway (11) entering the kiln is maintained within the range of 880 ± 10 °C.

2. The energy-saving process for externally decomposing and feeding into the kiln of a glass batch according to claim 1, characterized in that, In S3, fuel is sprayed into the preheating furnace (4) through multiple fuel nozzles (5) opened on the side of the preheating furnace (4) for combustion heating. The fuel sprayed into the preheating furnace (4) heats the batch from the outside to the inside through combustion. At the same time, the liquid fuel contained in the batch on the plate conveyor (10) continues to burn, and the liquid fuel contained in the batch heats the batch from the inside to the outside through combustion. The temperature of the batch gradually increases as it is transported forward by the plate conveyor (10) until the batch containing the liquid fuel that has started carbonate decomposition is transported to the connection between the preheating furnace (4) and the decomposition furnace (6), and control the temperature of the batch containing the liquid fuel that has started carbonate decomposition at 550 ± 10 °C. The fuel injection amount of the multiple fuel nozzles (5) on the side of the preheating furnace (4) gradually increases along the conveying direction of the plate conveyor (10).

3. The energy-saving process for decomposing outside the furnace and feeding into the furnace of a glass batch according to claim 1, characterized in that, In S3, electric heating is directly set on the side of the preheating furnace (4) for heating. The electric heating heats the batch from the outside to the inside. At the same time, the liquid fuel contained in the batch on the plate conveyor (10) continues to burn, and the liquid fuel contained in the batch heats the batch from the inside to the outside through combustion. The temperature of the batch gradually increases as it is transported forward by the plate conveyor (10) until the batch containing the liquid fuel that has started carbonate decomposition is transported to the connection between the preheating furnace (4) and the decomposition furnace (6), and control the temperature of the batch containing the liquid fuel that has started carbonate decomposition at 550 ± 10 °C. The electric heating power on the side of the preheating furnace (4) gradually increases along the conveying direction of the plate conveyor (10).

4. The energy-saving process for externally decomposing and feeding into the kiln of a glass batch according to claim 1, characterized in that, In S4, fuel is injected and burned into the decomposition furnace (6) through multiple fuel nozzles (5) opened on the side of the decomposition furnace (6) to heat by combustion. The fuel injected into the decomposition furnace (6) heats the batch material from outside to inside by combustion. At the same time, the liquid fuel contained in the batch material on the plate conveyor (10) continues to burn, and the liquid fuel contained in the batch material heats the batch material from inside to outside by combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor (10). When it is conveyed to the connection between the decomposition furnace (6) and the high-temperature slideway (11) entering the kiln, the sintered solid melt temperature of the batch material is controlled at 880 ± 10 °C; The fuel injection amount of multiple fuel nozzles (5) on the side of the decomposition furnace (6) gradually increases along the conveying direction of the plate conveyor (10).

5. The energy-saving process for externally decomposing and feeding into the kiln of a glass batch according to claim 1, wherein, In S4, electric heating is directly provided on the side of the decomposition furnace (6) for heating. The electric heating heats the batch material from outside to inside. At the same time, the liquid fuel contained in the batch material on the plate conveyor (10) continues to burn, and the liquid fuel contained in the batch material heats the batch material from inside to outside by combustion. The temperature of the batch material gradually increases as it is conveyed forward by the plate conveyor (10). When it is conveyed to the connection between the decomposition furnace (6) and the high-temperature slideway (11) entering the kiln, the sintered solid melt temperature of the batch material is controlled at 880 ± 10 °C; The electric heating power on the side of the decomposition furnace (6) gradually increases along the conveying direction of the plate conveyor (10).

6. The energy-saving process for externally decomposing and charging into the kiln of a glass batch according to claim 1, characterized in that, The combustion-supporting air for the preheating furnace (4) and the decomposition furnace (6) is introduced from the top of the regenerator of the existing glass kiln. The temperature of the combustion-supporting air is 1000 °C. The introduced relatively high-temperature combustion-supporting air enters the decomposition furnace (6) through the outlet of the decomposition furnace (6) after adjusting the air volume, and then enters the preheating furnace (4). The flow direction of the combustion-supporting air is opposite to the conveying direction of the plate conveyor (10).

7. The energy-saving process for externally decomposing and feeding into the kiln of a glass batch according to claim 6, characterized in that, A combustion-supporting air passage (9) is provided between the upper part of the hanging flat arch (7) at the outlet of the decomposition furnace (6) and the regenerator of the small furnace of the glass kiln (12). A combustion-supporting air regulating damper (8) for controlling the opening and closing size of the passage is provided on the combustion-supporting air passage (9). The hot air in the combustion-supporting air pipe enters the decomposition furnace (6) through the upper part of the connection between the decomposition furnace (6) and the hanging flat arch (7).

8. A pre-calcining energy-saving process for feeding glass batch into a kiln, as claimed in claim 1, wherein, The inclined blanket feeder (3), the preheating furnace (4), the decomposition furnace (6), the high-temperature slideway (11) entering the kiln and the front end of the glass kiln are hermetically and thermally insulated and connected.

9. A pre-calcining and in-kiln energy-saving process for glass batch outside the kiln according to claim 1, characterized in that The conveying method of the plate conveyor (10) is the relay push of the thrust plate. Each thrust plate on the plate conveyor (10) is higher than the lower thrust plate. Each thrust plate moves reciprocally independently and continuously pushes the batch material on the upper layer to the thrust plate on the lower layer.

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