An integrated treatment system and method for glass furnace flue gas with petroleum coke as fuel

Abstract

The present invention provides an integrated treatment system and method for flue gas of a glass furnace using petroleum coke as fuel, belonging to the technical field of flue gas purification. The system includes: a secondary waste heat boiler, a bypass heat exchanger, a primary desulfurization tower, a high-temperature electrostatic precipitator, a secondary desulfurization tower, a composite ceramic fiber filter tube dust removal and denitration integrated device, and an induced draft fan set connected in sequence; the secondary waste heat boiler includes: a high-temperature section and a low-temperature section; the high-temperature section of the secondary waste heat boiler is connected in parallel with the bypass heat exchanger; the composite ceramic fiber filter tube dust removal and denitration integrated device includes multiple stages of dust removal and denitration bins connected in parallel, and each stage of dust removal and denitration bin can be independently controlled. The system of the present invention has a simple structure. When a failure occurs in the high-temperature section, the high-temperature section can be replaced by the bypass heat exchanger, and when a failure occurs in each dust removal and denitration bin, it can be independently shut down to achieve online maintenance.

Description

Technical Field

[0001] Embodiments of the present disclosure relate to the technical field of flue gas purification and treatment, and in particular, to an integrated flue gas treatment system and method for a glass furnace with petroleum coke as fuel. Background Art

[0002] Currently, for a flue gas treatment system of a glass furnace using petroleum coke powder as fuel, a semi-dry desulfurization technology is often adopted, and an SCR system is used for denitrification to remove nitrogen oxides (NOx) in the flue gas. Then, the process route of the traditional flue gas treatment process is: furnace flue gas → high-temperature section of the waste heat boiler → high-temperature electrostatic precipitator → SCR denitrification → low-temperature section of the waste heat boiler → NID semi-dry desulfurization → bag filter → induced draft fan → chimney.

[0003] Disadvantages of the traditional process:

[0004] 1. Cannot be repaired online: When the hot boiler fails, the SCR denitrification fails, the NID semi-dry desulfurization fails, or the bag filter fails, shutdown maintenance is required, and the shutdown will affect the normal production of the furnace.

[0005] 2. The service life of the SCR denitrification catalyst is 2 years: The general service life of the furnace is more than 5 years. When the catalyst life reaches the service life, it will cause shutdown and affect production.

[0006] 3. The service life of the bag is 2 years: The general service life of the furnace is more than 5 years. When the bag life reaches the service life, it will cause shutdown and affect production. Summary of the Invention

[0007] The purpose of the embodiments of the present disclosure is to provide an integrated flue gas treatment system and method for a glass furnace with petroleum coke as fuel, so as to solve the foregoing problems existing in the prior art.

[0008] To achieve the above purpose, the technical solutions adopted in the embodiments of the present disclosure are as follows:

[0009] On the one hand, the embodiments of the present disclosure provide an integrated flue gas treatment system for a glass furnace with petroleum coke as fuel, which is applied to a glass furnace with petroleum coke powder as fuel. The system includes: a secondary waste heat boiler, a bypass heat exchanger, a primary desulfurization tower, a high-temperature electrostatic precipitator, a secondary desulfurization tower, an integrated dust removal and denitrification device with composite ceramic fiber filter tubes, and an induced draft fan group; the secondary waste heat boiler includes: a high-temperature section and a low-temperature section;

[0010] The inlet end of the high-temperature section of the secondary waste heat boiler is connected to the flue gas pipeline in parallel with the bypass heat exchanger, and the exhaust end is sequentially connected to the primary desulfurization tower, the high-temperature electrostatic precipitator, the secondary desulfurization tower, the integrated dust removal and denitrification device with composite ceramic fiber filter tubes, the low-temperature section of the secondary waste heat boiler, and the induced draft fan group;

[0011] The integrated dust removal and denitration equipment of the composite ceramic fiber filter tube includes multiple stages of serially connected dust removal and denitration bins. The gas transmission pipeline of the secondary desulfurization tower passes through each stage of the dust removal and denitration bins in sequence, and an intake branch is arranged in each stage of the dust removal and denitration bin. A control valve is arranged on each intake branch. The outlet of each stage of the dust removal and denitration bin is connected to an outlet branch, and a control valve is arranged on each outlet branch. And each outlet branch is arranged on the gas transmission pipeline communicating with the low-temperature section.

[0012] Exemplarily, the induced draft fan group includes: at least one induced draft fan. When there are multiple induced draft fans, each induced draft fan is connected in parallel with each other, and each induced draft fan is also connected to the gas transmission pipeline between the integrated dust removal and denitration equipment of the composite ceramic fiber filter tube and the low-temperature section through a bypass pipeline.

[0013] Exemplarily, the system further includes: a first hydrated lime silo, which is arranged on the gas transmission pipeline between the primary desulfurization tower and the high-temperature section of the secondary waste heat boiler, and is used to supply hydrated lime to the primary desulfurization tower.

[0014] Exemplarily, the system further includes: a spare sodium bicarbonate silo and a second hydrated lime silo that are sequentially arranged on the gas transmission pipeline between the high-temperature electrostatic precipitator and the secondary desulfurization tower, and are used to supply sodium bicarbonate and hydrated lime to the secondary desulfurization tower.

[0015] Exemplarily, the system further includes: a cyclone dust collector and a return bin. The inlet of the cyclone dust collector is connected to the outlet of the secondary desulfurization tower, the discharge outlet of the cyclone dust collector is connected to the inlet of the return bin, the outlet of the cyclone dust collector passes through each dust removal and denitration bin of the integrated dust removal and denitration equipment of the composite ceramic fiber filter tube through a gas transmission pipeline in sequence, and the discharge outlet of the return bin is connected to the recovery port of the secondary desulfurization tower.

[0016] Exemplarily, a first gas flow rate sensor and a first sulfide gas concentration detection sensor are arranged in the flue gas pipeline, and a second gas flow rate sensor is arranged in the gas transmission pipeline between the high-temperature section of the secondary waste heat boiler and the primary desulfurization tower.

[0017] Exemplarily, a second sulfide gas concentration detection sensor is arranged in the pipeline between the smoke outlet of the primary desulfurization tower and the high-temperature electrostatic precipitator; a third gas flow rate sensor is arranged in the pipeline between the high-temperature electrostatic precipitator and the secondary desulfurization tower;

[0018] A fourth gas flow rate sensor and a third sulfide gas concentration detection sensor are arranged in the pipeline between the smoke outlet of the secondary desulfurization tower and the integrated dust removal and denitration equipment of the composite ceramic fiber filter tube.

[0019] Exemplarily, a fifth gas flow rate sensor and a sixth gas flow rate sensor are respectively arranged in each intake air branch and each exhaust air branch of the integrated dust removal and denitration equipment of the composite ceramic fiber filter tube; a seventh gas flow rate sensor is arranged in the gas transmission pipeline between the integrated dust removal and denitration equipment of the composite ceramic fiber filter tube and the low-temperature section of the secondary waste heat boiler; an eighth gas flow rate sensor is arranged at the exhaust gas end of the low-temperature section of the secondary waste heat boiler.

[0020] Exemplarily, the system further includes: a reflux pipeline, which connects the secondary desulfurization tower and the primary desulfurization tower; the reflux pipeline is arranged between the primary desulfurization tower and the secondary desulfurization tower, so that the flue gas of the secondary desulfurization tower flows back to the primary desulfurization tower.

[0021] On the other hand, an embodiment of the present disclosure provides a method for integrated treatment of flue gas of a glass furnace with petroleum coke as fuel, which is applied to the above-mentioned glass furnace flue gas treatment system. The method includes: The first stage:

[0022] Obtain the first flue gas flow rate and the first sulfide concentration of the flue gas pipeline, and the second flue gas flow rate in the gas transmission pipeline between the high-temperature section and the primary desulfurization tower;

[0023] According to the second flue gas flow rate and the first sulfide concentration, determine the amount of the first sulfide per unit time in the gas transmission pipeline at the front end of the primary desulfurization tower, and combine the amount of the first preset sulfide per unit time after the flue gas is desulfurized by passing through the primary desulfurization tower to obtain the amount of the first sulfide to be reduced per unit time;

[0024] If the amount of the first sulfide to be reduced is greater than the maximum desulfurization amount of the primary desulfurization tower, adopt the first desulfurization mode; wherein, the first desulfurization mode is to add slaked lime at the front end of the primary desulfurization tower with the first preset dosage, that is, the maximum dosage; the desulfurization amount of the primary desulfurization tower is determined according to the input flow rate of slaked lime;

[0025] If the amount of the first sulfide to be reduced is not greater than the maximum desulfurization amount of the primary desulfurization tower, adopt the second desulfurization mode; wherein, the second desulfurization mode is to add slaked lime with the second preset dosage.

[0026] Exemplarily, the method further includes:

[0027] The second stage:

[0028] Obtain the second sulfide concentration and the third flue gas flow rate after the flue gas is desulfurized by the primary desulfurization tower; wherein, according to the third flue gas flow rate and the second sulfide concentration, determine the amount of the second sulfide per unit time in the gas transmission pipeline at the front end of the secondary desulfurization tower, and combine the amount of the second preset sulfide per unit time after the flue gas is desulfurized by passing through the secondary desulfurization tower to obtain the amount of the second sulfide to be reduced per unit time;

[0029] Determine whether the amount of the second sulfide is less than or equal to the first preset sulfide amount. If so, the amount of the second sulfide to be reduced is low, and the third desulfurization mode is adopted; wherein, the third desulfurization mode is to add slaked lime into the pipeline at the front end of the secondary desulfurization tower according to the third preset dosage.

[0030] If not, the amount of the second sulfide to be reduced is high, and the fourth desulfurization mode is adopted; the fourth desulfurization mode is to determine the corresponding relationship between the amount of the second sulfide to be reduced and the preset desulfurization amount to determine the dosage of the desulfurizer with the corresponding flow rate.

[0031] Exemplarily, the determining the corresponding relationship between the amount of the second sulfide to be reduced and the preset desulfurization amount to determine the dosage of the desulfurizer with the corresponding flow rate includes:

[0032] If the amount of the second sulfide to be reduced is between the first desulfurization amount and the second desulfurization amount, add slaked lime according to the fourth preset dosage.

[0033] If the amount of the second sulfide to be reduced continuously remains between the first desulfurization amount and the second desulfurization amount for every time t exceeded, add slaked lime with a preset increment once on the basis of the fourth preset dosage.

[0034] If the amount of the second sulfide to be reduced continuously remains between the first desulfurization amount and the second desulfurization amount for more than n times of time t, after adding slaked lime with n times of preset increments on the basis of the fourth preset dosage, additionally add baking soda with the preset dosage.

[0035] If the amount of the second sulfide to be reduced is less than the second desulfurization amount, add slaked lime according to the fifth preset dosage.

[0036] Exemplarily, when the system includes a reflux pipeline, the reflux pipeline is opened together when additionally adding baking soda with the preset dosage.

[0037] The beneficial effects of the embodiments of the present disclosure are:

[0038] The glass furnace flue gas treatment system proposed by the embodiments of the present disclosure solves the problem that in the traditional integrated flue gas desulfurization, dust removal and denitration system of a glass furnace using petroleum coke powder as fuel, each device cannot be repaired online. Description of the Drawings

[0039] Figure 1 is an integrated flue gas treatment system of a glass furnace with petroleum coke as fuel provided by an embodiment of the present disclosure;

[0040] Figure 2 is another integrated flue gas treatment system of a glass furnace with petroleum coke as fuel provided by an embodiment of the present disclosure;

[0041] Figure 3It is a schematic flow diagram of a method for integrated treatment of glass furnace flue gas with petroleum coke as fuel provided by an embodiment of the present disclosure.

[0042] In the figure:

[0043] 1. Secondary waste heat boiler; 11. High-temperature section; 12. Low-temperature section; 2. Bypass heat exchanger; 3. Primary desulfurization tower; 31. First hydrated lime silo; 4. High-temperature electrostatic precipitator; 5. Secondary desulfurization tower; 51. Baking soda silo; 52. Second hydrated lime silo; 6. Composite ceramic fiber filter tube dust removal and denitration integrated equipment; 61. Cyclone dust collector; 62. Return bin; 7. Induced draft fan unit; 8. Chimney. Specific embodiments

[0044] In order to make the objectives, technical solutions and advantages of the embodiments of the present disclosure clearer, the following further describes the embodiments of the present disclosure in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to explain the embodiments of the present disclosure and are not used to limit the embodiments of the present disclosure.

[0045] Embodiment 1:

[0046] As Figure 1 shown, on the one hand, an embodiment of the present disclosure provides an integrated treatment system for glass furnace flue gas with petroleum coke as fuel. The system includes: a secondary waste heat boiler 1, a bypass heat exchanger 2, a primary desulfurization tower 3, a high-temperature electrostatic precipitator 4, a secondary desulfurization tower 5, a composite ceramic fiber filter tube dust removal and denitration integrated equipment 6, and an induced draft fan unit 7; the secondary waste heat boiler 1 includes: a high-temperature section 11 and a low-temperature section 12; the intake end of the parallel connection of the high-temperature section of the secondary waste heat boiler and the bypass heat exchanger 2 is used to connect to the flue gas pipeline, and the exhaust end is sequentially connected to the primary desulfurization tower 3, the high-temperature electrostatic precipitator 4, the secondary desulfurization tower 5, the composite ceramic fiber filter tube dust removal and denitration integrated equipment 6, the low-temperature section 12 of the secondary waste heat boiler, and the induced draft fan unit 7; the composite ceramic fiber filter tube dust removal and denitration integrated equipment 6 includes multiple series-connected dust removal and denitration bins (not marked in the figure), the gas transmission pipeline of the secondary desulfurization tower sequentially passes through each dust removal and denitration bin, and an intake branch is provided in each dust removal and denitration bin. Control valves are provided on each intake branch, an outlet branch is connected to the outlet of each dust removal and denitration bin, control valves are provided on each outlet branch, and each outlet branch is arranged on the gas transmission pipe connecting the low-temperature section.

[0047] In the glass furnace flue gas treatment system of the embodiment of the present disclosure, each device is connected through corresponding pipelines. Among them, the induced draft fan unit can be connected to the gas transmission pipeline between the composite ceramic fiber filter tube dust removal and denitration integrated equipment and the low-temperature section through a bypass pipeline.

[0048] As an example of the induced draft fan set, the induced draft fan set includes: at least one induced draft fan. When there are multiple induced draft fans, the induced draft fans are connected in parallel with each other, and each induced draft fan is also connected to the gas pipeline between the composite ceramic fiber filter tube dust removal and denitration integrated equipment and the low temperature section through a bypass pipeline.

[0049] The glass furnace flue gas treatment system of the embodiments of the present disclosure adopts a dry desulfurization technology. Among them, the composite ceramic fiber filter tube dust removal and denitration integrated equipment is a composite ceramic tube dust removal and denitration integrated equipment, which has multiple dust removals and denitrations; the specific process route is: furnace flue gas → high temperature section of the waste heat boiler → primary dry desulfurization → high temperature electrostatic precipitator → secondary dry desulfurization → denitration of the composite ceramic fiber integrated equipment → low temperature section of the waste heat boiler → induced draft fan → chimney. Compared with the traditional glass furnace flue gas treatment integrated system, on the one hand, each device in the glass furnace flue gas treatment system of the embodiments of the present disclosure can be overhauled online: when the high temperature section of the waste heat boiler fails, a bypass heat exchanger is provided to replace the work of the high temperature section; when the composite ceramic fiber filter tube integrated equipment fails, the faulty chamber can be separately closed for overhaul; when the low temperature section of the waste heat boiler fails, it can directly enter the induced draft fan through the bypass; on the other hand, it has a long service life. In particular, the service life of the composite ceramic fiber filter tube, the core equipment of the composite ceramic fiber integrated equipment, is more than 5 years, which can meet the requirements of the furnace kiln period, and there will be no equipment shutdown during the normal production of the furnace.

[0050] For glass furnaces with petroleum coke powder as fuel, the sulfur content is relatively high, and the general sulfur content is 3000mg / m3. Therefore, for glass furnaces with petroleum coke powder as fuel, the selected desulfurization method is semi-dry or wet. The glass furnace flue gas treatment system of the embodiments of the present disclosure adopts dry desulfurization, and the core desulfurization equipment is the primary desulfurization tower, high temperature electrostatic precipitator and secondary desulfurization tower. The desulfurization is through the primary desulfurization + high temperature electrostatic precipitation + secondary desulfurization process, and a pure dry flue gas purification process is adopted. The system of the embodiments of the present disclosure has low resistance, no smoky tail, no waste water and no secondary pollution. Considering the complexity of the flue gas components after the combustion of petroleum coke powder fuel, especially the adhesion of particulate matter in the flue gas, a primary desulfurization conditioning system is provided in the primary desulfurization tower. The primary desulfurization conditioning system has both the performance of flue gas desulfurization and conditioning. While removing fluoride in the flue gas, it destroys the adhesion of particulate matter in the flue gas, ensures that the spikes of the spike lines in the high temperature electrostatic precipitator are not corroded and damaged, and enables the spike lines to reach the longest service life. The primary desulfurization conditioning system uses slaked lime as the desulfurization conditioning agent. Because the desulfurization efficiency of the pure dry desulfurization can reach more than 85%, only setting the primary desulfurization cannot ensure that sulfur dioxide is removed to 50mg / m 3Therefore, a secondary desulfurization system is configured to ensure the emission index of sulfur dioxide. The injection point of the denitration reducing agent is usually set at the front end of the integrated composite ceramic fiber. Since the front-end flue is short, the mixing of ammonia and flue gas is uneven, resulting in an increase in ammonia consumption and non-compliance with ammonia escape standards. In the embodiment of the present disclosure, the injection point of the denitration reducing agent is set at the front end of the desulfurization tower to mix more evenly with the flue gas, reduce the usage amount of the denitration reducing agent, and ensure the ammonia escape index.

[0051] The flue gas treatment system of the glass furnace in the embodiment of the present disclosure further includes: a first hydrated lime silo, and a gas transmission pipeline disposed between the primary desulfurization tower and the high-temperature section of the secondary waste heat boiler, for supplying hydrated lime to the primary desulfurization tower.

[0052] In the embodiment of the present disclosure, the first hydrated lime silo is disposed at the front end of the primary desulfurization tower and stores hydrated lime. A pipeline is provided at the discharge port of the first hydrated lime silo to connect the first hydrated lime silo to the gas transmission pipeline between the primary desulfurization tower and the high-temperature section of the secondary waste heat boiler. A control valve may also be provided at the discharge port of the first hydrated lime silo to control the discharge, mainly controlling the opening size of the discharge port. When the discharge port is opened large, the discharge per unit time is more; when the discharge port is opened small, the discharge per unit time is less. The control valve can be controlled by a control unit to achieve automatic control of feeding.

[0053] The flue gas treatment system of the glass furnace in the embodiment of the present disclosure further includes: a standby sodium bicarbonate silo and a second hydrated lime silo disposed in sequence between the high-temperature electrostatic precipitator and the secondary desulfurization tower, for supplying sodium bicarbonate and hydrated lime to the secondary desulfurization tower.

[0054] In the system of the embodiment of the present disclosure, the standby sodium bicarbonate silo and the second hydrated lime silo are disposed at the front end of the secondary desulfurization tower. The standby sodium bicarbonate silo stores sodium bicarbonate, and the second hydrated lime silo stores hydrated lime. Pipelines are provided at the discharge ports of the standby sodium bicarbonate silo and the second hydrated lime silo, and the pipelines of the standby sodium bicarbonate silo and the second hydrated lime silo are respectively connected to the gas transmission pipeline between the secondary desulfurization tower and the high-temperature electrostatic precipitator. Control valves may also be respectively provided at the discharge ports of the standby sodium bicarbonate silo and the second hydrated lime silo to control the discharge. The control valves can be controlled by a control unit to achieve automatic control of feeding.

[0055] At the front end of the standby sodium bicarbonate silo, that is, at the rear-end gas transmission pipeline close to the high-temperature electrostatic precipitator, an injection point for the denitration reducing agent is provided to inject the denitration reducing agent.

[0056] The flue gas treatment system of the embodiment of the present disclosure further includes: a cyclone dust collector and a return bin. The inlet of the cyclone dust collector is communicated with the outlet of the secondary desulfurization tower. The discharge port of the cyclone dust collector is communicated with the inlet of the return bin. The gas outlet of the cyclone dust collector passes through each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment in sequence through a gas transmission pipeline. The discharge port of the return bin is communicated with the recovery port of the secondary desulfurization tower.

[0057] In the system of the embodiment of the present disclosure, the recovery port of the secondary desulfurization tower is close to the air inlet and above the air inlet. The gas transmission pipeline communicated with the gas outlet of the cyclone dust collector is arranged at the position close to the discharge port, that is, below, of each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment. Each air inlet branch on the gas transmission pipeline faces the discharge port of the corresponding dust removal and denitration bin. The gas outlet of each stage of dust removal and denitration bin is far from the corresponding discharge port, that is, arranged above the corresponding dust removal and denitration bin. The gas outlet is communicated with the gas transmission pipeline between the composite ceramic fiber filter tube dust removal and denitration integrated equipment and the low-temperature section of the secondary waste heat boiler through the corresponding gas outlet branch.

[0058] In the system of the embodiment of the present disclosure, corresponding sensors are arranged on each pipeline according to actual situations to detect the temperature, gas flow rate, sulfide concentration, nitride concentration, etc. in the pipeline, so that the flue gas finally discharged from the system meets the purification requirements.

[0059] The flue gas discharged from the glass furnace enters the system of the embodiment of the present disclosure through a flue gas pipeline. The flue gas first enters the high-temperature section of the secondary waste heat boiler through the flue gas pipeline. A first gas flow rate sensor, a first sulfide gas concentration detection sensor, a first temperature sensor, etc. can be arranged at the position close to the high-temperature section of the secondary waste heat boiler in the flue gas pipeline. A second gas flow rate sensor and a second temperature sensor are arranged in the gas transmission pipeline between the high-temperature section of the secondary waste heat boiler and the primary desulfurization tower. Those skilled in the art can set corresponding detection equipment according to actual situations, not limited to the above sensors, etc.

[0060] The first gas flow rate sensor and the second gas flow rate sensor can be used to detect the gas flow rate of the flue gas after passing through the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger. Generally speaking, the gas flow rate will decrease, but in the case of the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger, the gas flow rate may change significantly or insignificantly. For example, the gas flow rate detected by the first gas flow rate sensor is v 1 , and the gas flow rate detected by the second gas flow rate sensor is v 2 , v 1 - v 2＝Δ v, Δ v is between [a, b], and the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger is regarded as normal. If Δ v < a, orΔ When v > b, it is initially judged that there is a fault in the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger. Further judgment can be made in combination with the temperature. At this time, it is best to stop the operation of the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger. The gas flow rate can also be used to calculate the content of sulfide per unit time in combination with the sulfide gas concentration to further determine the feeding method of slaked lime.

[0061] Furthermore, it is also possible to separately judge whether the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger is operating normally by detecting the temperatures at both ends of the pipeline of the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger by the second temperature sensor. If the detected temperature T of the second temperature sensor is less than or equal to the preset temperature T 0 , the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger is normal. If T > T 0 , when the expected temperature is not reached, the high-temperature section of the secondary waste heat boiler or the bypass is faulty. It can also be further verified in combination with the gas flow rate. At this time, it is necessary to close the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger for further inspection. In the system of the embodiment of the present disclosure, a nitride detection sensor can also be provided in the pipeline at the rear end of the first desulfurization tower. Those skilled in the art can set it according to the actual situation and will not be elaborated here.

[0062] In the system of the embodiment of the present disclosure, a second sulfide gas concentration detection sensor is provided in the pipeline between the smoke outlet of the first desulfurization tower and the high-temperature electrostatic precipitator; a third gas flow rate sensor is provided in the pipeline between the high-temperature electrostatic precipitator and the second desulfurization tower; a fourth gas flow rate sensor and a third sulfide gas concentration detection sensor are provided in the pipeline between the smoke outlet of the second desulfurization tower and the composite ceramic fiber filter tube dust removal and denitration integrated device.

[0063] The third gas flow rate sensor and the fourth gas flow rate sensor, in combination with the inner diameter of the pipeline, are mainly used to calculate the gas flow rate in the pipeline and, in combination with the sulfide gas concentration, determine the content of sulfide per unit time to judge which desulfurization method to adopt.

[0064] In the system of the embodiment of the present disclosure, a fifth gas flow rate sensor and a sixth gas flow rate sensor are respectively provided in each intake branch and each outlet branch of the composite ceramic fiber filter tube dust removal and denitration integrated device; a seventh gas flow rate sensor is provided in the gas transmission pipeline between the composite ceramic fiber filter tube dust removal and denitration integrated device and the low-temperature section of the secondary waste heat boiler; an eighth gas flow rate sensor is provided at the outlet end of the low-temperature section of the secondary waste heat boiler.

[0065] That is to say, gas flow sensors are provided at both the inlet and outlet of the dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated device. Whether the corresponding dust removal and denitration bin is faulty can be judged by the gas flow rates at the inlet and outlet of each dust removal and denitration bin. Temperature sensors can also be added at the inlet and outlet of each dust removal and denitration bin to judge whether the dust removal and denitration bin is faulty alone or in combination with the gas flow. The seventh gas flow sensor on the gas transmission pipeline between the composite ceramic fiber filter tube dust removal and denitration integrated device and the low-temperature section of the secondary waste heat boiler and the eighth gas flow sensor at the rear end of the low-temperature section of the secondary waste heat boiler can be used to judge whether the low-temperature section is faulty. Temperature sensors can also be added at the front and rear ends of the low-temperature section to judge whether the low-temperature section is faulty together with the gas flow sensor or alone. The judgment method can adopt the above method and will not be elaborated here.

[0066] Another aspect of the embodiments of the present disclosure provides a method for integrated treatment of glass furnace flue gas with petroleum coke as fuel, which is applied to the above-mentioned glass furnace flue gas treatment system. The desulfurization process is divided into two stages, namely the first stage and the second stage. The first stage includes: the first desulfurization mode and the second desulfurization mode, and the second stage includes: the third desulfurization mode and the fourth desulfurization mode. The method includes:

[0067] As Figure 3 shown, the first stage:

[0068] Step S1: Obtain the first flue gas flow rate and the first sulfide concentration of the flue gas pipeline, and the second flue gas flow rate in the gas transmission pipeline between the high-temperature section and the first-stage desulfurization tower.

[0069] In this method, it can be considered that after the flue gas flows through the high-temperature section of the secondary waste heat boiler, the components and corresponding concentrations of the flue gas do not change significantly. Sulfide mainly refers to sulfur dioxide SO 2 .

[0070] Step S2: Determine the amount of the first sulfide per unit time in the gas transmission pipeline at the front end of the first-stage desulfurization tower according to the second flue gas flow rate and the first sulfide concentration, and combine it with the amount of the first preset sulfide per unit time after the flue gas is desulfurized by the first-stage desulfurization tower to obtain the amount of the first sulfide to be reduced per unit time.

[0071] According to the second flue gas flow rate and the first sulfide concentration, the actual content of sulfide at the front end of the primary desulfurization tower can be determined. After desulfurization at the back end of the primary desulfurization tower, there is a first preset amount of sulfide. The difference between the actual content of sulfide at the front end of the primary desulfurization tower and the first preset amount of sulfide gives the amount of the first sulfide to be reduced. The content of sulfide per unit time is related to its concentration, flow rate, and pipeline size. Here, the pipeline size is known, and other factors are ignored. The amount of slaked lime entering the primary desulfurization tower determines the desulfurization amount. Factors such as desulfurization efficiency can be considered to determine the current desulfurization amount of the primary desulfurization tower. The current maximum desulfurization amount only needs to consider the maximum feeding amount of slaked lime per unit time, which can be determined according to the maximum feeding amount of slaked lime per unit time, and the flue gas flow rate can be ignored. The unit time can be from 1h to 10min and can be set according to the actual situation. The first sulfide concentration mainly refers to the mass concentration C 2 of sulfur dioxide SO s , with the unit of mg / m3, and the second flue gas flow rate v 2 , with the unit that can be m / h. The unit time can be confirmed according to the actual situation. Combining with the cross-sectional area s of the pipeline, s = π / 4×D 2 , where D is the inner diameter of the pipeline, the flue gas flow rate Q per unit time of the pipeline can be determined, with the unit of m3 / h, Q = s·v 2 . Combining with the mass concentration C 2 of sulfur dioxide SO s in the flue gas, the mass content of the first sulfide in the pipeline per unit time, m s = C s ·Q, which is also the emission amount, with the unit of g / h. According to the chemical reaction relationship between slaked lime Ca(OH) 2 and sulfur dioxide, the feeding amount of slaked lime per unit time can be calculated. Theoretically, about 1.156 grams of Ca(OH) 2 is required for every gram of SO 2 . The calculation process is not elaborated here. The common feeding amount of slaked lime is 1.2 to 1.5 times that of sulfide and can be adjusted according to the actual situation. If the first sulfide concentration is the volume concentration C SO2, the mass flow rate of sulfur dioxide can be calculated by combining the flue gas density ρ (in kg / m³) and the flue gas flow rate Q. Among them, the flue gas density ρ = P / RT. P is the absolute pressure in the pipeline (in Pa), R is the specific gas constant (in J / (kg·K)), which is approximately 287 J / (kg·K) for air, but if the specific composition of the flue gas is known, the corresponding mixed gas constant is used; T is the absolute temperature in the pipeline (in K). The content of sulfides in the pipeline is variable, so it is necessary to dynamically control the feeding amount of slaked lime to achieve the best desulfurization effect and the least cost input. The opening of the discharge port can be controlled by adjusting the control valve at the discharge port of the first slaked lime silo to control the feeding amount of slaked lime. The actual amount of sulfides decreased after desulfurization in the primary desulfurization tower can be determined according to the second sulfide concentration in the pipeline and the third flue gas flow rate after desulfurization in the primary desulfurization tower.

[0072] Step S3: If the amount of the first sulfide to be reduced is greater than the maximum desulfurization amount per unit time of the primary desulfurization tower, the first desulfurization mode is adopted; among them, the first desulfurization mode is to add slaked lime at the front end of the primary desulfurization tower with the first preset feeding amount, that is, the maximum feeding amount.

[0073] Since the desulfurization amount per unit time of the primary desulfurization tower is determined according to the feeding amount of slaked lime per unit time, at this time, the sulfide concentration is high and the flow rate is also high, resulting in a high content of sulfides per unit time. Adding slaked lime with the maximum feeding amount is relatively rare. When the amount of the first sulfide to be reduced is not greater than the maximum desulfurization amount per unit time of the primary desulfurization tower, switch to the second desulfurization mode.

[0074] Step S4: If the amount of the first sulfide to be reduced is not greater than the maximum desulfurization amount per unit time of the primary desulfurization tower, the second desulfurization mode is adopted; among them, the second desulfurization mode is to add slaked lime with the second preset feeding amount, and the second preset feeding amount is less than the first preset feeding amount.

[0075] The first desulfurization mode and the second desulfurization mode can be switched according to the actual situation. That is to say, adopting the second desulfurization mode can handle the amount of the first sulfide to be reduced that is not greater than the maximum desulfurization amount. After the flue gas is desulfurized by the primary desulfurization tower, the concentration of sulfur dioxide decreases. Combining the current flue gas flow rate, the actual amount of sulfides is obtained, and slaked lime can be added according to the actual situation in the second stage.

[0076] The second stage:

[0077] Step S5: Obtain the second sulfide concentration and the third flue gas flow rate after the flue gas is desulfurized by the primary desulfurization tower; among them, according to the third flue gas flow rate and the second sulfide concentration, determine the amount of the second sulfide per unit time in the gas transmission pipeline at the front end of the secondary desulfurization tower, and combine the amount of the second preset sulfide per unit time after the flue gas flows through the secondary desulfurization tower to obtain the amount of the second sulfide to be reduced per unit time.

[0078] The amount of the second sulfide is the actual sulfide content in the pipeline after the flue gas passes through the primary desulfurization tower for desulfurization. The second preset amount of sulfide is the flue gas close to the final emission. Therefore, the supplement of the desulfurization of the primary desulfurization tower in step S3 is to ensure that the sulfur dioxide SO 2 content in the desulfurized flue gas is below 50 mg / m 3 or less.

[0079] Step S6: Determine whether the amount of the second sulfide is less than or equal to the first preset dosage. If so, the amount of the second sulfide to be reduced is relatively low, and the third desulfurization mode is adopted. Among them, the third desulfurization mode is to add slaked lime to the pipeline at the front end of the secondary desulfurization tower according to the third preset dosage.

[0080] That is to say, the amount of the second sulfide to be reduced is relatively small, and a low dosage of slaked lime can be completely used to achieve the required desulfurization effect. The addition of slaked lime at each preset dosage can be set according to the actual situation.

[0081] Step S7: If the amount of the second sulfide is greater than the first preset amount of sulfide, the amount of the second sulfide to be reduced is relatively high, and the fourth desulfurization mode is adopted. The fourth desulfurization mode is to judge the corresponding relationship between the amount of the second sulfide to be reduced and the preset desulfurization amount, and then determine to inject the desulfurizer with the corresponding flow rate.

[0082] When the amount of the first sulfide to be reduced in step S3 is greater than the current maximum desulfurization amount of the primary desulfurization tower, after the desulfurization treatment in step 3, the actual sulfide content is still relatively high, which results in the amount of the second sulfide being greater than the first preset amount of sulfide, and the amount of the second sulfide to be reduced is relatively high. Then, according to the corresponding relationship between the amount of the second sulfide to be reduced and the preset desulfurization amount, the desulfurizer with the corresponding flow rate is determined. At this time, there is a corresponding relationship between the preset desulfurization amount per unit time and the slaked lime injection flow rate.

[0083] The judgment of the corresponding relationship between the amount of the second sulfide to be reduced and the preset desulfurization amount, and the determination of injecting the corresponding amount of desulfurizer includes:

[0084] Step S71: If the amount of the second sulfide to be reduced is between the first desulfurization amount and the second desulfurization amount, add slaked lime according to the fourth preset dosage.

[0085] Step S72: If the amount of the second sulfide to be reduced continuously stays between the first desulfurization amount and the second desulfurization amount and exceeds the time t each time, add slaked lime with a preset increment Δm on the basis of the fourth preset dosage. That is, the flow rate is gradually increased with the increase of time.

[0086] Step S73: If the amount of the second sulfide to be reduced continuously stays between the first desulfurization amount and the second desulfurization amount and exceeds n times of time t, after adding slaked lime with n times of preset increments on the basis of the fourth preset dosage, add baking soda with the preset dosage.

[0087] Step S74: If the second sulfide amount to be reduced is lower than the second desulfurization amount, add slaked lime at the fifth preset dosage.

[0088] The first to fifth preset dosages all refer to the dosage per unit time, and the unit can be g / h.

[0089] A relatively high second sulfide amount to be reduced and a long duration indicate a relatively high sulfur dioxide concentration in the flue gas coming out of the primary desulfurization tower. Gradually increase the slaked lime dosage to achieve the purpose of rapid desulfurization. When the sulfide concentration in the flue gas is relatively high and the cumulative time is relatively long, it indicates that the adhesiveness of the flue gas is relatively high. To effectively reduce the sulfide concentration in the flue gas, baking soda can be added. Generally, the second sulfide amount to be reduced will not be very high. Even if the second sulfide amount to be reduced reaches a relatively high level, adding baking soda and slaked lime can ensure that the desulfurization meets the requirements. The main thing is how to control the dosage of baking soda and slaked lime, which can not only save costs but also meet the emission standards, and can further damage the adhesiveness of the particulate matter in the flue gas.

[0090] The method further includes: If the difference in the flue gas flow rate and / or temperature at both ends of the high-temperature section of the secondary waste heat boiler is not within the corresponding preset threshold, the high-temperature section of the secondary waste heat boiler fails, close the high-temperature section, and switch to the bypass heat exchanger for operation;

[0091] If the difference in the flue gas flow rate and / or temperature between the inlet end and the outlet branches of each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment is not within the corresponding preset threshold, the corresponding dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment fails, and close the faulty dust removal and denitration bin;

[0092] If the difference in the flue gas flow rate and / or temperature between the outlet end of the low-temperature section of the secondary waste heat boiler and the outlet branches of each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment is not within the corresponding preset threshold, the low-temperature section of the secondary waste heat boiler fails;

[0093] When the induced draft fan unit is also connected to each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment, after the low-temperature section of the secondary waste heat boiler fails, close the low-temperature section and switch the induced draft fan unit for operation.

[0094] Embodiment 2:

[0095] Based on Embodiment 1, as Figure 2 shown, the system can also add a reflux pipeline between the primary desulfurization tower and the secondary desulfurization tower, so that the flue gas of the secondary desulfurization tower can be refluxed to the primary desulfurization tower.

[0096] Specifically, a reflux pipeline can be added near or at the top of the secondary desulfurization tower to the vicinity of the gas outlet of the primary desulfurization tower. A one-way valve can be installed at the reflux pipeline near the gas outlet of the primary desulfurization tower, so that the flue gas of the secondary desulfurization tower can flow back to the primary desulfurization tower, preventing the flue gas of the primary reflux tower from directly flowing to the secondary desulfurization tower.

[0097] The intake of the reflux pipeline is connected to the secondary desulfurization tower near the top and is provided with a control valve. A one-way valve is installed near the outlet of the reflux pipeline, and a Venturi structure can be set. The outlet of the reflux pipeline is arranged near the gas outlet of the primary desulfurization tower or on the gas pipeline between the primary desulfurization tower and the high-temperature electrostatic precipitator.

[0098] In step S73, when adding a preset amount of baking soda additionally, the reflux pipeline can be opened.

[0099] Opening the reflux pipeline allows the flue gas of the secondary desulfurization tower to flow back to the primary desulfurization tower. The flue gas may contain unreacted baking soda. While the flue gas disperses and dilutes the flue gas at the outlet of the primary desulfurization tower, it can further destroy the adhesion of particulate matter in the flue gas and can also recycle the baking soda.

[0100] The above are only the preferred embodiments of the present disclosure. It should be noted that for those of ordinary skill in the art, without departing from the principles of the embodiments of the present disclosure, several improvements and refinements can be made, and these improvements and refinements should also be regarded as the protection scope of the embodiments of the present disclosure.

Claims

1. An integrated fume treatment system for a glass kiln using petroleum coke as fuel, which is applied to a glass kiln using petroleum coke powder as fuel, and is characterized in that: The system comprises: A secondary waste heat boiler, a bypass heat exchanger, a primary desulfurization tower, a high-temperature electrostatic precipitator, a secondary desulfurization tower, a composite ceramic fiber filter tube dust removal and denitrification integrated equipment, and an induced draft unit; the secondary waste heat boiler includes: a high-temperature section and a low-temperature section; After the high temperature section of the secondary waste heat boiler is connected in parallel with the bypass heat exchanger, the air inlet end is used to connect to the flue gas duct, and the exhaust end is sequentially connected to the primary desulfurization tower, the high temperature electrostatic precipitator, the secondary desulfurization tower, the composite ceramic fiber filter tube dust removal and denitrification integrated equipment, the low temperature section of the secondary waste heat boiler and the induced draft unit; when the high temperature section of the secondary waste heat boiler fails, the bypass heat exchanger replaces the high temperature section of the waste heat boiler to work; The composite ceramic fiber filter tube dust removal and denitration integrated equipment comprises a multi-stage parallel dust removal and denitration bin, the gas pipeline of the secondary desulfurization tower is sequentially arranged in the dust removal and denitration bins of each stage, and an air inlet branch is arranged in each dust removal and denitration bin, each air inlet branch is provided with a control valve, the air outlet of each dust removal and denitration bin is connected to an air outlet branch, each air outlet branch is provided with a control valve, and each air outlet branch is arranged in a gas pipeline connected to the low temperature section; The system further comprises: A first slaked lime silo is provided in a gas pipeline between the primary desulfurization tower and the high temperature section of the secondary waste heat boiler, and is used to provide slaked lime to the primary desulfurization tower; A spare baking soda silo and a second slaked lime silo are sequentially arranged in the gas transmission pipeline between the high-temperature electric precipitator and the secondary desulfurization tower, and are used to provide baking soda and slaked lime to the secondary desulfurization tower; A reflux pipe, one end of which is close to the gas outlet of the primary desulfurization tower, and the reflux pipe is arranged between the primary desulfurization tower and the secondary desulfurization tower, so that the flue gas of the secondary desulfurization tower refluxes to the primary desulfurization tower; The unreacted baking soda in the flue gas disperses and dilutes the flue gas at the outlet of the primary desulfurization tower, while further destroying the adhesion of the particles in the flue gas.

2. The system according to claim 1, characterized in that The induced draft unit includes: at least one induced draft fan. When it includes multiple induced draft fans, the induced draft fans are connected in parallel with each other, and each induced draft fan is also connected to the gas pipeline between the composite ceramic fiber filter tube dust removal and denitrification integrated equipment and the low temperature section through a bypass pipeline.

3. The system according to claim 1 or 2, characterized in that: The system also includes: a cyclone dust collector and a return bin, the inlet of the cyclone dust collector is connected to the outlet of the secondary desulfurization tower, the discharge port of the cyclone dust collector is connected to the inlet of the return bin, the gas outlet of the cyclone dust collector is sequentially penetrated through the various dust removal and denitrification bins of the composite ceramic fiber filter tube dust removal and denitrification integrated equipment through a gas pipeline, and the discharge port of the return bin is connected to the recovery port of the secondary desulfurization tower.

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