Glass furnace flue gas decontamination device

Abstract

The application discloses a glass melting furnace flue gas decontamination device, belonging to the technical field of tail gas treatment. The device comprises a flue gas conditioning tower, a ceramic tube dust collector, a denitration reactor, a second waste heat boiler section and a desulfurization tower connected in sequence through a flue. The device further comprises a first waste heat boiler section, which is located upstream of at least one of the flue gas conditioning tower, the ceramic tube dust collector or the denitration reactor in the conveying direction of the flue gas. The application is based on the process sequence of dust removal, denitration and desulfurization, and removes acidic gases and adsorbs basic oxides first to facilitate dust removal. Thus, the denitration process can avoid the blockage and poisoning of the denitration catalyst and the erosion of the catalyst by dust to improve the denitration efficiency. In the desulfurization process, the slurry poisoning phenomenon is also avoided to improve the desulfurization efficiency. The device can be operated synchronously with the main body of the melting furnace at 100%, that is, the ultra-low emission of pollutants can be realized.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of tail gas treatment, and particularly relates to a glass melting furnace flue gas decontamination device. BACKGROUND

[0002] In the conventional technology, in order to reduce the emission of pollutants in the glass manufacturing industry, the flue gas generated in the manufacturing process is generally treated from the aspects of denitration, desulfurization and dust removal.

[0003] However, the decontamination effect of the existing flue gas decontamination process is limited: for the denitration process, the current general method is SCR (selective catalytic oxidation reduction technology) denitration method, but the denitration parameter design at the present stage is not perfect, resulting in low denitration efficiency and large ammonia escape, which cannot meet the ultra-low emission requirement; for the desulfurization process, the current dry desulfurization, semi-dry desulfurization and wet desulfurization methods are all imperfect, and cannot have both desulfurization efficiency and application range, and are prone to cause secondary pollution; for the dust removal process, it is also impossible to have both dust removal effect and application range, and is prone to cause secondary dust raising. Therefore, the decontamination effect of the existing flue gas decontamination process is limited, and it is impossible to achieve ultra-low emission of pollutants. SUMMARY

[0004] The main purpose of the present application is to provide a glass melting furnace flue gas decontamination device, which aims to solve the technical problem that the decontamination effect of the flue gas of the glass melting furnace in the prior art is limited and it is impossible to achieve ultra-low emission of pollutants.

[0005] According to a first aspect of the present application, a glass melting furnace flue gas decontamination device is provided, which comprises a flue gas conditioning tower, a ceramic tube dust remover, a denitration reactor, a second waste heat boiler section and a desulfurization tower which are sequentially communicated through a flue.

[0006] The device further comprises a first waste heat boiler section, which is located upstream of at least one of the flue gas conditioning tower, the ceramic tube dust remover or the denitration reactor in the conveying direction of the flue gas.

[0007] In an embodiment, the flue gas conditioning tower comprises:

[0008] a tower body having a first flue gas inlet and a first flue gas outlet, the first flue gas inlet and the first flue gas outlet being respectively communicated with the flue;

[0009] a feeding assembly located in the tower body for applying calcium hydroxide to the flue gas;

[0010] a water spraying assembly located in the tower body and downstream of the feeding assembly for water spraying cooling of the flue gas.

[0011] In an embodiment, the ceramic tube dust collector comprises a plurality of dust removal sub-chambers, the plurality of dust removal sub-chambers are arranged in parallel, and each of the plurality of dust removal sub-chambers is in communication with the flue.

[0012] In an embodiment, the ceramic tube dust collector further comprises:

[0013] a plurality of first control pipes, each of the plurality of first control pipes corresponds to one of the plurality of dust removal sub-chambers, one end of each of the plurality of first control pipes is in communication with the flue, the other end of each of the plurality of first control pipes is in communication with the corresponding dust removal sub-chamber, and each of the plurality of first control pipes is provided with a first electrically operated gate for controlling the opening and closing of the first control pipe.

[0014] a plurality of second control pipes, each of the plurality of second control pipes corresponds to one of the plurality of dust removal sub-chambers, one end of each of the plurality of second control pipes is in communication with the flue, the other end of each of the plurality of second control pipes is in communication with the corresponding dust removal sub-chamber, and each of the plurality of second control pipes is provided with a second electrically operated gate for controlling the opening and closing of the second control pipe.

[0015] In an embodiment, when the flue gas volume of the flue gas is less than 50,000 m 3 / h, the number of the dust removal sub-chambers is 2-4; when the flue gas volume of the flue gas is 50,000 m 3 / h-120,000 m 3 / h, the number of the dust removal sub-chambers is 6-8; and when the flue gas volume of the flue gas is greater than or equal to 120,000 m 3 / h, one dust removal sub-chamber is arranged for each 20,000 m 3 / h of the flue gas volume.

[0016] In an embodiment, the flow rate of the flue gas in the ceramic tube dust collector is 0.5-1.2 m / min.

[0017] In an embodiment, the denitration reactor comprises:

[0018] a plurality of reaction chambers, the plurality of reaction chambers are connected in series along the conveying direction of the flue gas.

[0019] In an embodiment, the gas inlet pipe and the gas outlet pipe of each of the reaction chambers are in communication with the flue, and each of the gas inlet pipe and the gas outlet pipe is provided with a first electrically controlled valve;

[0020] the flue comprises a plurality of second electrically controlled valves, the plurality of second electrically controlled valves are arranged between the connection between the gas inlet pipe of each of the reaction chambers and the flue and the connection between the gas outlet pipe and the flue, and the state of the first electrically controlled valve and the state of the second electrically controlled valve are opposite.

[0021] In an embodiment, the denitration temperature of the denitration reactor is 320-410 DEG C, the denitration flue gas linear velocity of the denitration reactor is 1.8-3 m / s, and the denitration flue gas space velocity of the denitration reactor is 1800 h -1 -3000 h -1 .

[0022] In an embodiment, the first waste heat boiler section and the second waste heat boiler section are connected by an external damper.

[0023] In an embodiment, the desulfurization tower comprises:

[0024] a cylindrical body, the cylindrical body being provided with a second flue gas inlet and a second flue gas outlet, the second flue gas inlet and the second flue gas outlet being in communication with the flue;

[0025] a spraying device provided in the cylindrical body, the spraying device having a plurality of spraying heads for providing calcium hydroxide solution; and a 4-stage hip-type mist eliminator located above the spraying device.

[0026] In an embodiment, the flow rate of the flue gas in the desulfurization tower is 1.8-3 m / s.

[0027] The present application is based on the process sequence of dust removal, denitration and desulfurization. First, the flue gas conditioning tower is used to remove most of the strong acid gases such as SO3 and HCl, thereby reducing the acid corrosion of the device. Then, the flue gas flows through the ceramic tube dust collector and then enters the denitration reactor. After the dust and acid gases are removed, the denitration process can avoid the reaction of acid gases and ammonia to produce ammonium salt which easily blocks the catalyst, and also avoid the erosion of dust to the catalyst, thereby ensuring the quality and service life of the catalyst, and thus improving the denitration efficiency. In the desulfurization process, the slurry poisoning phenomenon caused by dust is also avoided, and the generation of aerosol is avoided, thereby improving the desulfurization efficiency of the flue gas in the desulfurization tower. With the improvement of dust removal, denitration and desulfurization effects, and the fact that the device can run synchronously with the main body of the furnace at 100%, the ultra-low emission of pollutants can be realized. BRIEF DESCRIPTION OF DRAWINGS

[0028] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the following will briefly introduce the drawings needed to be used in the embodiments or prior art description. Obviously, the drawings in the following description are only embodiments of the present application, and other drawings can also be obtained by those skilled in the art without creative labor on the basis of the provided drawings.

[0029] Figure 1 The overall framework schematic diagram of the glass furnace flue gas decontamination device according to the embodiment of the present application;

[0030] Figure 2 The structure schematic diagram of the flue gas conditioning tower in the present application Figure 1 The structure schematic diagram of the flue gas conditioning tower in the present application

[0031] Figure 3 The structure schematic diagram of the flue gas conditioning tower in the present application Figure 1 The structure schematic diagram of the ceramic tube dust collector in the present application

[0032] Figure 4 The structure schematic diagram of the flue gas conditioning tower in the present application Figure 1 The structure schematic diagram of the flue gas conditioning tower in the present application

[0033] Figure 5 The structure schematic diagram of the flue gas conditioning tower in the present application Figure 1 The structure schematic diagram of the denitration reactor in the present application, wherein the second reaction bin is a standby bin

[0034] Figure 6 The structure schematic diagram of the denitration reactor in the present application, wherein the third reaction bin is a standby bin Figure 1

[0035] Figure 7 The structure schematic diagram of the denitration reactor in the present application, wherein the first reaction bin is a standby bin Figure 1

[0036] Figure 8 The structure schematic diagram of the denitration reactor in the present application, wherein the fourth reaction bin is a standby bin Figure 1

[0037] The structure schematic diagram of the denitration reactor in the present application, wherein the fourth reaction bin is a standby bin Figure 9 Figure 1 The structure schematic diagram of the desulfurization tower in the present application

[0038] The implementation, functional features and advantages of the present application will be further explained with reference to the accompanying drawings. DETAILED DESCRIPTION

[0039] It should be understood that the specific embodiments described herein merely set forth preferred combinations of components and / or other features, and that persons of ordinary skill in the art would be able to design many other varieties thereof without departing from the principles of the present application.

[0040] ​​​In the prior art, in order to reduce the emission of pollutants in the glass manufacturing industry, the flue gas generated in the manufacturing process is generally treated from the aspects of denitration, desulfurization and dust removal. However, the current flue gas decontamination process has limited decontamination effect: for the denitration process, the current SCR (selective catalytic oxidation reduction technology) denitration method is generally used, but the current denitration parameter design is not perfect, resulting in low denitration efficiency and large ammonia escape, which cannot meet the ultra-low emission requirement; for the desulfurization process, the current dry desulfurization, semi-dry desulfurization and wet desulfurization methods are all imperfect, and cannot have both desulfurization efficiency and application range, and are prone to cause secondary pollution; for the dust removal process, it is also impossible to have both dust removal effect and application range, and is prone to cause secondary dust raising. Therefore, the current flue gas decontamination process has limited decontamination effect, and cannot achieve ultra-low emission of pollutants.

[0041] Based on the process sequence of dust removal, denitration and desulfurization, the application first uses a flue gas conditioning tower to apply calcium hydroxide to the flue gas to adsorb basic oxides in the flue gas and remove acidic gases, so that the basic oxides in the molten state are converted into solid dust, thereby facilitating dust removal treatment; after the flue gas flows through the ceramic tube dust collector, it enters the denitration reactor, that is, after the dust and acidic gases are removed, the denitration process can avoid the reaction of acidic gases and ammonia gas to produce ammonium salt which is easy to block the catalyst, and also avoid the erosion of dust to the catalyst, thereby ensuring the quality and service life of the catalyst, and thus facilitating the improvement of the denitration efficiency; in the desulfurization process, the dust poisoning phenomenon in the slurry is also avoided, and the generation of aerosols is avoided, thereby facilitating the improvement of the desulfurization efficiency of the flue gas in the desulfurization tower; thus, with the improvement of the effects of dust removal, denitration and desulfurization, the ultra-low emission of pollutants can be achieved.

[0042] To make the objectives, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be described below in connection with the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.

[0043] In the specification and claims of the embodiments of the present application, "first", "second" are used to distinguish similar objects, and do not necessarily describe a specific order or sequence. It should be understood that such data can be interchanged as appropriate, so that the embodiments described herein can be implemented in an order other than those illustrated or described herein.

[0044] Reference Figure 1 , Figure 1 The overall framework schematic diagram of the glass furnace flue gas decontamination device involved in the embodiment of the present application.

[0045] In the embodiment, the glass-melting-furnace flue gas decontamination device comprises, in sequence through a flue, a flue gas conditioning tower 1, a ceramic-tube dust collector 2, a denitration reactor 4, a second waste-heat boiler section 32, and a desulfurization tower 5.

[0046] The device further comprises a first waste-heat boiler section 31, which is upstream of at least one of the flue gas conditioning tower 1, the ceramic-tube dust collector 2, or the denitration reactor 4, in the conveying direction of the flue gas.

[0047] Specifically, as shown in Figure 1 The embodiment generally adopts a process flow of dust removal first, denitration second, and desulfurization last, and introduces a flue gas conditioning tower for pre-conditioning of the flue gas and a waste-heat boiler for absorption and utilization of the heat of the flue gas. The glass-melting-furnace flue gas decontamination device comprises:

[0048] a flue gas conditioning tower 1, which has a first flue gas inlet 11 and a first flue gas outlet 15 and is configured to apply calcium hydroxide to the flue gas;

[0049] First, before the formal first-step decontamination operation, i.e., dust removal, the embodiment can pre-condition the flue gas. This is because large glass-melting furnaces are all provided with a furnace regenerator, and the flue gas, after heat exchange in the regenerator, enters the main flue at a temperature of about 500°C. In addition, in glass production, raw materials containing strong alkaline oxides R2O (mainly Na2O and K2O) are used, and after high-temperature melting in the glass-melting furnace, most of the R2O enters the product as a glass component, and a small amount (about 3%) enters the flue gas as volatile matter. In the flue gas at 500°C, the R2O exists in a molten state, and if not treated, the molten R2O is easy to stick to the ceramic-tube dust collector at the back end, affecting use and dust removal effect.

[0050] Therefore, in order to solve the above problems, the embodiment sets a flue gas conditioning tower 1 before dust removal, which is used to apply calcium hydroxide to the flue gas, so that the molten strong alkaline oxide R2O is adsorbed by calcium hydroxide to form solid dust, thereby ensuring the smooth progress of subsequent dust removal operation. In order to be able to fully adsorb R2O, the amount of calcium hydroxide used is 3-5 times the mass of R2O. In addition, calcium hydroxide, as an alkaline substance, can also remove most of the strong acid gases such as SO3 (sulfur trioxide) and HCl (hydrogen chloride) in the flue gas. On the one hand, it can reduce the acid corrosion of the flue gas to the downstream decontamination device (including the dust removal device, i.e. the ceramic tube dust collector 2, the denitration device, i.e. the denitration reactor 3, and the desulfurization device, i.e. the desulfurization tower 5), thereby prolonging the service life of the subsequent decontamination device and improving the decontamination efficiency and effect. On the other hand, since SO3 and HCl also belong to pollution gases, a certain decontamination effect can also be achieved.

[0051] In a specific embodiment, referring to Figure 2 , Figure 2 the structure of the flue gas conditioning tower 1 in the present application Figure 1 . As shown in Figure 2 , the tower body of the flue gas conditioning tower 1 is provided with a first flue gas inlet 11 and a first flue gas outlet 15, i.e. the flue gas enters the flue gas conditioning tower 1 through the first flue gas inlet 11 after heat exchange in the heat storage chamber, and then leaves the flue gas conditioning tower 1 through the first flue gas outlet 15 after conditioning in the flue gas conditioning tower 1 and enters the ceramic tube dust collector 2 for dust removal; in order to complete the above-mentioned adsorption of strong alkaline oxide R2O and removal of strong acid gas, a feeding assembly 13 is also provided in the flue gas conditioning tower 1, which is arranged in the tower body and is used to apply calcium hydroxide to the flue gas. It can be understood that after the flue gas enters the flue gas conditioning tower 1 from the first flue gas inlet 11, the feeding assembly 13 applies calcium hydroxide to the tower, and the strong alkaline oxide in the flue gas will be adsorbed on the calcium hydroxide, and the strong acid gas will react with the calcium hydroxide to be removed; in addition, the flue gas conditioning tower 1 is also provided with a water spraying assembly 14, which can cool the flue gas when the downstream waste heat boiler fails, so that the flue gas temperature can be reduced to the required denitration temperature of the downstream denitration reactor 4, thereby ensuring the smooth progress of the subsequent operation; finally, since the flue gas contains a large amount of dust, and the excess material after adding calcium hydroxide and the products generated by the reaction may fall down, in order to avoid secondary pollution and to realize the recycling of waste materials, a dust discharge port 12 is also provided at the bottom of the tower body of the flue gas conditioning tower 1.

[0052] The ceramic tube dust collector 2 has a first inlet flue and a first outlet flue, and the first inlet flue is in communication with the first flue gas outlet;

[0053] After completing the pre-conditioning operations described above, the first step of decontamination, namely dust removal, can begin. In this embodiment, the dust collector is made of ceramic fiber tubes, a new type of high-temperature resistant (800℃) and high-efficiency material. The dust removal efficiency of the ceramic tube dust collector 2 made from it is superior to that of electrostatic precipitators and bag filters. After dust removal, the dust content in the flue gas is <10mg / m³. 3 It can fully meet the ultra-low emission requirements. Furthermore, in order to achieve better dust removal effect, in this embodiment, the flow rate of flue gas in the ceramic tube dust collector 2 is adapted to be 0.5-1.2m / min, such as 0.7m / min, and the dust removal efficiency that can be achieved is >99.99%.

[0054] Understandably, in this embodiment, since the ceramic tube dust collector 2 is located at the very front of the three decontamination devices (dust removal device, namely ceramic tube dust collector 2; denitrification device, namely denitrification reactor 4; and desulfurization device, namely desulfurization tower 5), the dust removal operation is performed first. Thus, after the efficient dust removal by the ceramic tube dust collector 2, the subsequent devices can perform their corresponding operations in a nearly dust-free state, which greatly improves the operational safety of the downstream facilities, extends the service life of the facilities, and also helps to improve the decontamination efficiency of subsequent decontamination operations.

[0055] In one specific implementation, refer to Figure 3 , Figure 3 For the present invention Figure 1 A schematic diagram of the structure of the ceramic tube dust collector 2. Figure 3 As shown, the ceramic tube dust collector 2 has a first inlet flue 21 and a first outlet flue 27. The first inlet flue 21 is connected to the first flue gas outlet 15 in the flue gas conditioning tower 1. That is, after the flue gas is pre-conditioned and discharged from the first flue gas outlet 15, it will enter the ceramic tube dust collector 2 through the first inlet flue 21. After entering the ceramic tube dust collector 2, the flue gas will then enter the dust collection compartment through the first control pipe 22 for dust collection. It should be emphasized that, unlike the electrostatic precipitators and bag filters in traditional technologies, the ceramic tube dust collector in this embodiment... The dust collector 2 adopts a compartmentalized design, with multiple dust collection compartments 24 connected in parallel. Each of the multiple dust collection compartments 24 is connected to the first inlet flue and the first outlet flue, respectively. As can be understood, since the multiple dust collection compartments 24 are independent of each other and can all be used for flue gas dust removal, if a compartment malfunctions, that compartment can be shut down for maintenance, replacement, or other operations without shutting down the entire dust collector. The other compartments can continue to perform dust removal operations. Therefore, this design enables online maintenance of the ceramic tube dust collector and allows for replacement at any time without affecting the dust removal operation.

[0056] Further, for each dust removal sub-chamber 24, a first control pipe 22 is arranged correspondingly to enable the flue gas to enter the dust removal sub-chamber 24 for dust removal, and a first electrically operated damper 23 is arranged on each first control pipe 22 to control the opening and closing of the corresponding first control pipe 22. It can be understood that, under normal circumstances, i.e. when the dust removal sub-chamber 24 is working normally, the first electrically operated dampers 23 are in an open state, and the flue gas can enter the sub-chamber through the first control pipe 22. If a fault occurs, the first electrically operated damper 23 corresponding to the dust removal sub-chamber 24 that has failed will be closed, while the other first electrically operated dampers 23 remain open. At this time, dust removal can still be completed through the other dust removal sub-chambers 24, and at the same time, the relevant maintenance personnel can also carry out maintenance and replacement of parts if necessary, so that real-time fault repair can be completed without affecting the dust removal operation.

[0057] Further, after the dust removal sub-chamber 24 filters and removes the dust from the flue gas, the flue gas can be discharged into the first outlet flue 27 through the second control pipe 25 to enter the next device. For each dust removal sub-chamber 24, a second control pipe 25 is arranged correspondingly to enable the flue gas to be discharged. A second electrically operated damper 26 is arranged on each second control pipe 25 to control the opening and closing of the corresponding second control pipe 25. It can be understood that, under normal circumstances, i.e. when the dust removal sub-chamber 24 is working normally, the second electrically operated dampers 26 are in an open state, and the flue gas can be discharged through the second control pipe 25. If a fault occurs, since it has been described above that the first electrically operated damper 23 corresponding to the dust removal sub-chamber 24 that has failed will be closed, i.e. the flue gas cannot enter the dust removal sub-chamber 24 that has failed, the corresponding second electrically operated damper 26 will also be closed to prevent the flue gas discharged from the other sub-chambers from entering the dust removal sub-chamber 24 that has failed, so as to facilitate maintenance.

[0058] The principle of the sub-chamber in this embodiment is further described as follows: first, in order to ensure that the ceramic tube dust collector 2 can meet the dust removal requirements under any circumstances, the total amount of flue gas that can be accommodated is greater than the actual maximum flue gas amount in production, specifically 1.2 times the actual maximum flue gas amount in production, so as to ensure that there is no situation of insufficient capacity; second, since the larger the actual flue gas amount, the larger the required dust removal space, the number of dust removal sub-chambers 24 is determined by the actual flue gas amount generated in production, specifically: when the flue gas amount is less than 50000 m 3 / h, the number of dust removal sub-chambers is 2-4; when the flue gas amount is 50000 m 3 / h-120000 m 3 / h, the number of dust removal sub-chambers is 6-8; and when the flue gas amount is greater than or equal to 120000 m 3 / h, then the number of dust removal sub-chambers is 8-10 per 20000 m 3The flue gas volume of / h sets one dust removal sub-bin. Of course, if the flue gas volume is greater than or equal to 120000 m 3 / h and cannot be divided by 20000, the dust removal sub-bin should be the integral value of the ratio of the flue gas volume to 20000 plus 1. For example, if the flue gas volume is 130000 m 3 / h at this time, the number of dust removal sub-bins 24 that need to be set can be 7. Therefore, the sub-bin design of the present embodiment can also flexibly increase or decrease the number of dust removal sub-bins 24, thereby meeting the efficient dust removal under any flue gas volume condition.

[0059] In the present embodiment, the first waste heat boiler section 31 and the second waste heat boiler section 32 jointly constitute a waste heat boiler.

[0060] As can be easily understood, the first waste heat boiler section 31 and the second waste heat boiler section 32 of the existing glass melting furnace waste heat boiler are connected by an internal gate, which has problems such as high-temperature deformation and dust accumulation in daily operation, resulting in difficulty in cleaning the gate and frequent occurrence of the phenomenon that the gate cannot be closed tightly, so that part of the flue gas in the first waste heat boiler section 31 that has not been denitrified directly enters the flue gas in the second waste heat boiler section 32 that has been denitrified, resulting in incomplete flue gas denitrification and failure to achieve ultra-low emission of denitrification.

[0061] In the present embodiment, the first waste heat boiler section 31 is located upstream of at least one of the flue gas conditioning tower 1, the ceramic pipe dust collector 2 or the denitrification reactor 4 in the conveying direction of the flue gas, and the second waste heat boiler section 32 is located between the denitrification reactor 4 and the desulfurization tower 5, so that the first waste heat boiler section 31 and the second waste heat boiler section 32 are independent of each other and each communicates with the flue. Specifically, the first waste heat boiler section 31 and the second waste heat boiler section 32 are connected by an external gate.

[0062] It is worth mentioning that the first waste heat boiler section 31 is located upstream of at least one of the flue gas conditioning tower 1, the ceramic pipe dust collector 2 or the denitrification reactor 4 in the conveying direction of the flue gas, i.e. the first waste heat boiler section 31 can be located before the flue gas conditioning tower 1, and after the flue gas passes through the first waste heat boiler section 31, it enters the flue gas conditioning tower 1. Or it can be located between the flue gas conditioning tower 1 and the ceramic pipe dust collector 2, or between the ceramic pipe dust collector 2 or the denitrification reactor 4.

[0063] Hereinafter, the first waste heat boiler section 31 is located between the ceramic pipe dust collector 2 or the denitrification reactor 4 as an example for further description.

[0064] The first waste heat boiler section 31 has a second flue gas inlet and a second flue gas outlet, and the second flue gas inlet is connected to the first outlet flue; the second waste heat boiler section 32 has a third flue gas inlet and a third flue gas outlet.

[0065] After completing the dust removal operation, based on the above process flow of dust removal, denitrification, and desulfurization, the denitrification operation should be performed next. However, before that, this embodiment also introduces a waste heat boiler to absorb heat and cool down the flue gas after dust removal. Its main functions are as follows: First, to utilize the waste heat of the high-temperature flue gas produced by the glass melting furnace, and the steam generated can be used for steam turbine power generation and other production and daily life; Second, to ensure that the temperature of the cooled flue gas can meet the technical requirements of the downstream medium-temperature SCR denitrification temperature (320℃-410℃), and the denitrification operating temperature can be adjusted by changing the evaporation rate according to actual needs.

[0066] In one specific implementation, refer to Figure 4 , Figure 4 For the present invention Figure 1 A schematic diagram of the structure of a medium-temperature waste heat boiler. (See diagram below.) Figure 4 As shown, the waste heat boiler can be divided into two parts: the first waste heat boiler section 31 and the second waste heat boiler section 32. First, the first waste heat boiler section 31 has a second flue gas inlet 311 and a second flue gas outlet 312. The second flue gas inlet 311 is connected to the first outlet flue duct 27. That is, after the flue gas is discharged from the ceramic tube dust collector 2, it will enter the first waste heat boiler section 31 through the second flue gas inlet 311. The first waste heat boiler section 31 absorbs heat and cools the flue gas, and generates steam for power generation and other production and daily life. The first waste heat boiler section 31 adjusts the temperature of the cooled flue gas by changing the evaporation rate so that it can meet the temperature requirements of the subsequent denitrification operation. Finally, the flue gas can be discharged through the second flue gas outlet 312 and enter the next decontamination device, namely the denitrification reactor 4.

[0067] Secondly, the second waste heat boiler section 32 is provided with a third flue gas inlet 321 and a third flue gas outlet 322. The third flue gas inlet 321 is used to receive the flue gas discharged after denitrification in the denitrification reactor 4 (the denitrification reactor 4 and its related denitrification operations will be described in detail below). That is to say, after the flue gas is discharged from the denitrification reactor 4, it will enter the second waste heat boiler section 32 of the waste heat boiler through the third flue gas inlet 321. The second waste heat boiler section 32 absorbs heat and cools the flue gas, and generates steam for power generation and other production and living purposes. Finally, the flue gas can be discharged through the third flue gas outlet 322 and enter the next decontamination device, namely the desulfurization tower.

[0068] Finally, the first waste heat boiler section 31 and the second waste heat boiler section 32 can also be connected through an external damper. In fact, the first and second sections of the waste heat boiler of the glass melting furnace at the present stage are generally connected through an internal damper, which is prone to high-temperature deformation, dust accumulation and other problems in daily operation, resulting in great difficulty in cleaning the damper and frequent phenomenon of being stuck and not tightly closed, so that part of the flue gas discharged from the first waste heat boiler section 31 which has not been denitrified directly enters the flue gas in the second waste heat boiler section 32 which has been denitrified, resulting in incomplete denitrification of the flue gas and failure to achieve ultra-low emission of denitrification. Therefore, the first waste heat boiler section 31 and the second waste heat boiler section 32 are connected through the design of the external damper in the embodiment, which avoids the problems of high-temperature deformation and dust accumulation, can completely solve the problem of incomplete denitrification caused by the internal damper, and is conducive to improving the denitrification efficiency.

[0069] a denitration reactor 4 having a second inlet flue and a second outlet flue, the second inlet flue being in communication with the second flue gas outlet, and the second outlet flue being in communication with the third flue gas inlet;

[0070] After the above cooling treatment, the temperature of the flue gas can meet the temperature requirement of the SCR medium-temperature denitrification process involved in the embodiment, that is, the flue gas can be denitrified based on the SCR medium-temperature denitrification process, and the basic principle is that ammonia is sprayed into the flue gas, and then the denitrification catalyst is used to make the ammonia and the nitrogen oxides (mainly nitric oxide and nitrogen dioxide) in the flue gas undergo an oxidation-reduction reaction: 4NH3+4NO+O2=4N2+6H2O, 8NH3+6NO2=7N2+12H2O, and finally harmless N2 (nitrogen) and H2O (water) are generated.

[0071] As can be understood, since the flue gas conditioning tower 1 is arranged before denitrification, the strong acid gas in the flue gas is neutralized and treated by calcium hydroxide, so that the strong acid gas and ammonia are prevented from reacting to generate ammonium salt during the denitrification process, thereby avoiding the problem of clogging of the denitrification catalyst caused by the ammonium salt, greatly improving the stability of the denitrification operation, and being conducive to improving the denitrification efficiency; and since the ceramic tube dust collector 2 is arranged before denitrification, the dust in the flue gas is removed, thereby avoiding the scouring of the dust on the SCR denitrification catalyst during the denitrification stage, improving the service life of the catalyst, and also being conducive to improving the denitrification efficiency, and also reducing the use amount of the purge medium (steam, compressed air) by about 95% during denitrification operation, thereby also reducing the cost.

[0072] In addition, the linear velocity and space velocity of the denitrification operation and the ammonia injection grid design are also optimized in the embodiment to make them more suitable for the flue gas characteristics of the glass melting furnace. As can be understood, due to high-temperature combustion, the glass melting furnace generates a large amount of thermal NO x , and the glass melting furnace NOx Concentration is generally >1300 mg / m³ 3 Some melting furnaces even have concentrations as high as 4000 mg / m³ 3 Therefore, the denitrification design of glass melting furnaces needs to be selected based on the characteristics and configuration of the flue gas.

[0073] In this embodiment, the linear velocity of the denitrification flue gas can be between 1.8-3 m / s, such as 2.2 m / s, ensuring a more uniform distribution of the flue gas in the catalyst space, with the distribution range controllable within ±2%; while the velocity of the denitrification flue gas in the space can be 1800-3000 h⁻¹. -1 , such as 2100h -1 This ensures the reaction rate between the flue gas and the catalyst, allowing the denitrification efficiency to remain consistently above 95% over the long term. It should be noted that the denitrification flue gas linear velocity refers to the flue gas volume (unit: m³ / s). 3 / h) and the cross-sectional area of ​​the denitrification catalyst (in m²) 2 The ratio of the volume of flue gas to the volume of flue gas in denitrification (m³ / s) is used to determine the volume of flue gas in denitrification. 3 / h) and the volume of the denitrification catalyst (in m³) 3 The ratio of the linear velocity and spatial velocity of the denitrification flue gas is important because both need to be appropriately valued. Too high a value may cause catalyst blockage, affecting desulfurization efficiency, while too low a value will result in insufficient catalyst utilization. In addition, this embodiment optimizes the setting of the ammonia injection grid; specifically, the ammonia injection points can be set to 30 per 10,000 m³. 3 Furthermore, the pressure of ammonia injection at each point is consistent, allowing ammonia to form staggered and uniform distribution points in the flue gas space. This ensures that the mixing uniformity error between ammonia and flue gas can be controlled within 1%, thereby improving denitrification efficiency. Considering the catalyst's lifespan (generally around 36 months), a conventional denitrification tower design would inevitably lead to denitrification shutdowns during catalyst replacement, resulting in NOx emissions. x Emissions do not meet standards.

[0074] In one specific implementation, refer to Figures 5 to 8 , Figures 5 to 8 For the present invention Figure 1 A schematic diagram of the structure of the denitrification reactor 4. Figure 5 As shown, the denitrification reactor 4 includes a second inlet flue 41 and a second outlet flue 44. The second inlet flue 41 is connected to the second flue gas outlet 312. That is, after the flue gas is cooled by the first waste heat boiler section 31, it can enter the denitrification reactor 4 through the second inlet flue 41. The denitrification reactor 4 includes multiple reaction chambers 42, which are connected in series along the flue gas conveying direction.

[0075] It can be understood that, considering the service life of the catalyst (generally about 36 months), if the overall denitration tower is designed, it will inevitably cause the denitration to stop running when the catalyst is replaced, thereby causing the NOx emission to be unqualified. Therefore, in the present embodiment, a plurality of reaction bins 42 are connected in series along the conveying direction of the flue gas, so that the catalyst in part of the reaction bins 42 can be conveniently replaced.

[0076] As an option of the present embodiment, the gas inlet pipe and the gas outlet pipe of the reaction bin 42 are both communicated with the flue, and the gas inlet pipe and the gas outlet pipe are both provided with an electric control valve, wherein the flue is composed of the second inlet flue 41 and the second outlet flue 44, specifically the part of the flue involved in the flue gas transmission. As for the plurality of reaction bins 42, they can be specifically divided into a plurality of operation bins and at least one standby bin, so that the flue gas transmission path can be changed by controlling the opening and closing of the electric control valve. Figure 5 For example, as shown in the figure, it includes 3 operation bins (solid line) and 1 standby bin (dashed line), and the gas inlet pipe and the gas outlet pipe of each reaction bin are provided with a first electric control valve 431 to control the on-off of each reaction bin and the transmission path of the flue gas, and the flue includes a plurality of second electric control valves 432, which are arranged between the connection of the gas inlet pipe of each reaction bin 42 and the flue and the connection of the gas outlet pipe and the flue, and the state of the first electric control valve 431 and the second electric control valve 432 is opposite. In this way, the real-time cyclic replacement of the denitration catalyst in different bins can be realized.

[0077] Specifically, as shown in the figure, Figures 5 to 8For example, the present embodiment can be designed to have different service life and different replacement time for catalysts in each reaction chamber, such as the first reaction chamber 42a can be set for 24 months, the third reaction chamber 42c for 30 months, and the fourth reaction chamber 42d for 36 months. The initial normal operation mode is to operate the first reaction chamber 42a, the third reaction chamber 42c, and the fourth reaction chamber 42d, and the second reaction chamber 42b is standby, that is, the initial installation of the denitration reactor 4 only has three reaction chambers 42a, 42c, and 42d participating in the denitration operation. Correspondingly, the first electric control valve 431 on the inlet and outlet pipes related to the reaction chambers 42a, 42c, and 42d is opened, and the second electric control valve 432 between the inlet and outlet pipes of any one of the reaction chambers 42a, 42c, and 42d is closed to form the main flue gas pipeline. At this time, the flue gas passes through the reaction chambers 42a, 42c, and 42d in turn for denitration, while the first electric control valve 431 on the inlet and outlet pipes of the second reaction chamber 42b is in a closed state and does not participate in the denitration operation. Correspondingly, the second electric control valve 432 between the inlet and outlet pipes of the second reaction chamber 42b is in an open state. After 24 months, that is, when the replacement time of the denitration catalyst in the first reaction chamber 42a is reached, the first electric control valve 431 on the inlet and outlet pipes of the first reaction chamber 42a is closed, the second electric control valve 432 between the inlet and outlet pipes of the first reaction chamber 42a and the first electric control valve 431 on the inlet and outlet pipes of the second reaction chamber 42b are opened. At this time, the flue gas passes through the reaction chambers 42b, 42c, and 42d in turn for denitration, while the denitration catalyst in the first reaction chamber 42a can be replaced at the same time.After 30 months, i.e. when the replacement time of the denitration catalyst of the third reaction chamber 42c is reached, the second electrically controlled valve 432 between the gas inlet pipe and the gas outlet pipe of the first reaction chamber 42a and the first electrically controlled valve 431 on the gas inlet pipe and the gas outlet pipe of the third reaction chamber 42c are closed, and the second electrically controlled valve 432 between the gas inlet pipe and the gas outlet pipe of the third reaction chamber 42c and the first electrically controlled valve 431 on the gas inlet pipe and the gas outlet pipe of the first reaction chamber 42a are opened, at this time, the flue gas passes through the reaction chambers 42a, 42b, 42d in sequence for denitration, and at the same time, the denitration catalyst of the reaction chamber 42c can be replaced; after 36 months, i.e. when the replacement time of the denitration catalyst of the fourth reaction chamber 42d is reached, the first electrically controlled valve 431 on the gas inlet pipe and the gas outlet pipe of the fourth reaction chamber 42d and the second electrically controlled valve 432 between the gas inlet pipe and the gas outlet pipe of the third reaction chamber 42c are closed, and the first electrically controlled valve 431 on the gas inlet pipe and the gas outlet pipe of the third reaction chamber 42c and the second electrically controlled valve 432 between the gas inlet pipe and the gas outlet pipe of the fourth reaction chamber 42d are opened, at this time, the flue gas passes through the reaction chambers 42a, 42b, 42c in sequence for denitration, and at the same time, the denitration catalyst of the reaction chamber 42d can be replaced. Such a cycle operation can ensure the smooth progress of the denitration operation without the problem of suspension of the denitration operation due to replacement of the catalyst, and regular replacement of the denitration catalyst can also ensure the quality of the denitration catalyst, which is conducive to improving the denitration efficiency. Finally, after the denitration is completed, the denitrated flue gas can enter the above-mentioned second waste heat boiler section through the second outlet flue 44 for subsequent waste heat utilization and desulfurization operation.

[0078] A desulfurization tower 5 is in communication with the third flue gas outlet for applying calcium hydroxide solution to the flue gas and discharging the desulfurized flue gas.

[0079] After the above-mentioned denitrated flue gas is cooled by the second waste heat boiler section 32, the flue gas can enter the desulfurization tower 5 through the third flue gas outlet of the second waste heat boiler section 32 for desulfurization. In the desulfurization tower 5, calcium hydroxide solution can be applied to the flue gas to react with SO2 in the flue gas to achieve the purpose of desulfurization.

[0080] It can be understood that, since the flue gas conditioning tower 1 is arranged at the front end, most of the strong acid gas is removed, so that the corrosion of the flue gas to the desulfurization tower 5 is greatly reduced after the flue gas enters the desulfurization tower 5, the service life of the desulfurization tower 5 is prolonged, and the smooth progress of the desulfurization operation is ensured; and since the ceramic tube dust collector 2 is arranged at the front end, the dust in the flue gas entering the desulfurization tower 5 is <10 mg / m 3 , the phenomenon of slurry poisoning caused by strong basic oxides and soot dust generated by the glass melting furnace is basically avoided, the generation of aerosol is avoided, and the desulfurization efficiency is greatly improved.

[0081] In addition, in order to improve desulfurization efficiency, the flow velocity of flue gas in the desulfurization tower can be adaptively set between 1.8-3 m / s, such as 2.3 m / s, and the desulfurization tower 5 is designed with the same diameter, that is, the desulfurization tower 5 is designed as a cylinder to avoid problems such as flue gas deflection and wall slagging caused by diameter change.

[0082] Finally, in practical applications, a small amount of ammonia gas will inevitably escape without reacting during the above denitrification operation. Since the desulfurization tower 5 is located after the denitrification reactor 4 in this embodiment, the ammonia gas that escapes in the desulfurization tower 5 will react with SO2 to form sulfate, which greatly reduces the amount of ammonia escape. In this embodiment, the amount of ammonia escape can be less than 0.5 ppm.

[0083] In one specific implementation, refer to Figure 9 , Figure 9 For the present invention Figure 1 A schematic diagram of the structure of the desulfurization tower 5. (See diagram below.) Figure 6 As shown, the desulfurization tower 5 has a fourth flue gas inlet 51 and a fourth flue gas outlet 54 on its cylindrical body. The fourth flue gas inlet 51 is connected to the third flue gas outlet 322. This means that after the flue gas is cooled by the second waste heat boiler section 32, it can enter the desulfurization tower 5 through the fourth flue gas inlet 51 for desulfurization. Specifically, the desulfurization tower 5 includes a spray device 52 with multiple spray heads that can spray calcium hydroxide solution to remove SO2 from the flue gas. The spray device is a high-pressure self-cleaning spray device. The desulfurization tower 5 is equipped with multiple spray heads, ensuring 100% wet spray coverage of the flue gas with a uniformity deviation of less than 1%, achieving a desulfurization efficiency of over 99%. Furthermore, the desulfurization tower 5 includes a four-stage ridge-type demister 53, located above and downstream of the spray equipment 52. Its function is to progressively demister the desulfurized flue gas, completely separating the solution from the gas, achieving a demisting efficiency of over 99.99%. It also separates the gas from the solid products (sulfates) generated during desulfurization, ensuring flue gas dust levels remain below 10 mg / m³. 3 emission.

[0084] The embodiment is based on the process sequence of dust removal, denitration and desulfurization. First, calcium hydroxide is used to adsorb alkaline oxides in flue gas and remove acid gases, so that the molten alkaline oxides are converted into solid dust, thereby facilitating dust removal treatment. After removing the dust and acid gases, the denitration process can avoid the reaction of acid gases and ammonia gas to produce ammonium salt which is easy to block the catalyst, that is, the denitration catalyst is prevented from being blocked and poisoned, and the catalyst is also prevented from being washed by the dust, thereby ensuring the quality and service life of the catalyst, and thus improving the denitration efficiency. In addition, in the desulfurization process, the poisoning phenomenon of the desulfurization slurry caused by the dust is also avoided, and the generation of aerosol is avoided, thereby improving the desulfurization efficiency. Thus, with the improvement of the effects of dust removal, denitration and desulfurization, the ultra-low emission of pollutants can be realized. In addition, by designing the ceramic tube dust collector 2 and the denitration reactor 4 into separate compartments, the normal operation of dust removal and denitration can be ensured while the ceramic tube dust collector 2 is maintained and the catalyst in the denitration reactor 4 is replaced. Furthermore, by designing the waste heat boiler in sections, not only the waste heat of the flue gas can be fully utilized, but also the problems such as high-temperature deformation and dust accumulation of the internal gate plate can be avoided, thereby avoiding the difficulty of cleaning the gate plate and the situation of being stuck and not tightly closed, solving the problem of incomplete denitration caused by the internal gate plate, and greatly improving the denitration efficiency. That is, the present application can ensure that the flue gas meets the ultra-low emission requirements (NOx<100 mg / m³, SO2<50 mg / m³, and dust<10 mg / m³).

[0085] The above is only the preferred embodiment of the present application, and does not limit the patent scope of the present application. Any equivalent structure or equivalent process transformation, or direct or indirect application in other related technical fields, which is based on the content of the specification and drawings of the present application, is also included in the patent protection scope of the present application.

Claims

1. A glass melter offgas decontamination apparatus characterized by, The device comprises a flue gas conditioning tower, a ceramic tube dust collector, a denitration reactor, a second waste heat boiler section and a desulfurization tower which are sequentially communicated through the flue; The device further comprises a first waste heat boiler section, which is located upstream of at least one of the flue gas conditioning tower, the ceramic tube dust collector or the denitration reactor in the conveying direction of the flue gas; The first waste heat boiler section and the second waste heat boiler section are connected by an external gate; The denitration reactor comprises: a plurality of reaction bins which are connected in series along the conveying direction of the flue gas; The gas inlet pipe and the gas outlet pipe of the reaction bin are both communicated with the flue, and the gas inlet pipe and the gas outlet pipe are both provided with a first electric control valve; The flue comprises a plurality of second electric control valves, which are arranged between the connection of the gas inlet pipe of each reaction bin and the flue and the connection of the gas outlet pipe and the flue, and the state of the first electric control valve and the second electric control valve is opposite.

2. The apparatus of claim 1, wherein, The flue gas conditioning tower comprises: a tower body having a first flue gas inlet and a first flue gas outlet, which are respectively communicated with the flue; a feeding assembly located in the tower body for applying calcium hydroxide to the flue gas; a water spraying assembly located in the tower body and downstream of the feeding assembly for water spraying cooling of the flue gas.

3. The apparatus of claim 1, wherein, The ceramic tube dust collector comprises a plurality of dust removal sub-chambers which are arranged in parallel and each communicated with the flue.

4. The apparatus of claim 3, wherein, The ceramic tube dust collector further comprises: a plurality of first control pipes corresponding to the plurality of dust removal sub-chambers, one end of any first control pipe being communicated with the flue, the other end of the first control pipe being communicated with the corresponding dust removal sub-chamber, and a first electric gate being arranged on the first control pipe to control the opening and closing of the first control pipe; the flue gas enters the dust removal sub-chamber through the first control pipe; a plurality of second control pipes corresponding to the plurality of dust removal sub-chambers, one end of any second control pipe being communicated with the flue, the other end of the second control pipe being communicated with the corresponding dust removal sub-chamber, and a second electric gate being arranged on the second control pipe to control the opening and closing of the second control pipe, the flue gas being discharged from the dust removal sub-chamber through the second control pipe.

5. The apparatus of claim 4, wherein, when the flue gas quantity of the flue gas is less than 50000m 3 / h, the number of the dust removal sub-chambers is 2-4; when the flue gas quantity of the flue gas is 50000m 3 / h-120000m 3 / h, the number of the dust removal sub-chambers is 6-8; when the flue gas quantity of the flue gas is greater than or equal to 120000m 3 / h, one dust removal sub-chamber is set for every 20000m 3 / h of the flue gas quantity.

6. The apparatus of claim 1, wherein, In the ceramic tube dust collector, the flow rate of the flue gas is 0.5-1.2 m / min.

7. The apparatus of claim 1, wherein, The denitration temperature of the denitration reactor is 320-410℃, the denitration flue gas linear velocity of the denitration reactor is 1.8-3m / s, and the denitration flue gas space velocity of the denitration reactor is 1800h -1 -3000h -1 .

8. The apparatus of claim 1, wherein, The desulfurization tower comprises: a cylindrical body having a second flue gas inlet and a second flue gas outlet, which are respectively communicated with the flue; a spraying device arranged in the cylindrical body and having a plurality of spraying heads for providing calcium hydroxide solution; and a 4-stage ridge-type mist eliminator located above the spraying device.

9. The apparatus of claim 8, wherein, In the desulfurization tower, the flow rate of the flue gas is 1.8-3 m / s.

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