Integrated treatment system and method for flue gas of glass kiln using petroleum coke as fuel

Abstract

The invention provides an integrated treatment system and method for flue gas of a glass kiln using petroleum coke as fuel, and belongs to the technical field of flue gas purification. The system comprises a second-stage waste heat boiler, a bypass heat exchanger, a first-stage desulfurization tower, a high-temperature electric dust remover, a second-stage desulfurization tower, composite ceramic fiber filter tube dust removal and denitration integrated equipment and an induced draft fan unit which are connected in sequence, the secondary waste heat boiler comprises a high-temperature section and a low-temperature section; the high-temperature section of the secondary waste heat boiler is connected with the bypass heat exchanger in parallel; the dust removal and denitration integrated equipment with the composite ceramic fiber filter tube comprises 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 is simple in structure, the high-temperature section can be replaced by the bypass heat exchanger when the high-temperature section breaks down, and the dedusting and denitration bins can be independently closed to achieve online maintenance when the dedusting and denitration bins break down.

Description

Technical Field

[0001] The disclosed embodiments 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 kiln using petroleum coke as fuel. Background Art

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

[0003] Disadvantages of traditional technology:

[0004] 1. Online maintenance is not possible: When the hot boiler fails, the SCR denitrification fails, the NID semi-dry desulfurization fails, or the bag filter fails, the kiln needs to be shut down for maintenance, which will affect the normal production of the kiln.

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

[0006] 3. The service life of the bag is 2 years: The general life of the kiln is more than 5 years. When the bag 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 glass kiln flue gas treatment system and method using petroleum coke as fuel, thereby solving the aforementioned problems existing in the prior art.

[0008] In order to achieve the above objectives, the technical solutions adopted by the embodiments of the present disclosure are as follows:

[0009] On the one hand, an embodiment of the present disclosure provides an integrated flue gas treatment system for a glass kiln whose fuel is petroleum coke, which is applied to a glass kiln whose fuel is petroleum coke powder. 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 comprises: a high-temperature section and a low-temperature section;

[0010] 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;

[0011] The composite ceramic fiber filter tube dust removal and denitrification integrated equipment includes a multi-stage series dust removal and denitrification bin, the gas pipeline of the secondary desulfurization tower is sequentially passed through the dust removal and denitrification bins at each stage, and an air inlet branch is arranged in each stage of the dust removal and denitrification bin, each air inlet branch is provided with a control valve, the air outlet of each stage of the dust removal and denitrification 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.

[0012] Exemplarily, the induced draft fan 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 pipe.

[0013] Exemplarily, the system further includes: a first slaked lime silo, which is disposed in a gas pipeline between the primary desulfurization tower and the high temperature section of a secondary waste heat boiler, and is used to provide slaked lime to the primary desulfurization tower.

[0014] Exemplarily, the system also includes: a spare baking soda silo and a second slaked lime silo which are sequentially arranged in the gas pipeline between the high-temperature electrostatic precipitator and the secondary desulfurization tower, for providing baking soda and slaked lime to the secondary desulfurization tower.

[0015] Exemplarily, the system also includes: a cyclone dust collector and a return silo, 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 silo, the gas outlet of the cyclone dust collector is sequentially penetrated into each dust removal and denitrification silo of the composite ceramic fiber filter tube dust removal and denitrification integrated equipment through a gas pipeline, and the discharge port of the return silo 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 provided in the flue gas duct, and a second gas flow rate sensor is provided 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 provided 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 provided 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 composite ceramic fiber filter tube dust removal and denitrification integrated equipment.

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

[0020] Exemplarily, the system further includes: a reflux pipe, which connects the secondary desulfurization tower with the primary desulfurization tower; the reflux pipe is arranged between the primary desulfurization tower and the secondary desulfurization tower, so that the flue gas from the secondary desulfurization tower refluxes to the primary desulfurization tower.

[0021] Another aspect of the present disclosure provides an integrated treatment method for glass furnace flue gas using petroleum coke as fuel, which is applied to the glass furnace flue gas treatment system as described above. The method comprises: a first stage:

[0022] Obtaining a first flue gas flow rate and a first sulfide concentration in the flue gas duct, and a 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, the first sulfide amount per unit time in the gas transmission pipeline at the front end of the primary desulfurization tower is determined, and the first preset sulfide amount per unit time after the flue gas flows through the primary desulfurization tower for desulfurization is combined to obtain the first amount of 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, the first desulfurization mode is adopted; wherein the first desulfurization mode is to use the first preset amount of addition at the front end of the primary desulfurization tower, that is, to add slaked lime at the maximum amount of addition; the desulfurization amount of the primary desulfurization tower is determined according to the slaked lime input flow rate;

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

[0026] Exemplarily, the method further includes:

[0027] Phase 2:

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

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

[0030] If not, the second amount of sulfides 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 second amount of sulfides to be reduced and the preset desulfurization amount to determine the desulfurizer of the corresponding flow rate.

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

[0032] If the second amount of sulfide to be reduced is between the first desulfurization amount and the second desulfurization amount, slaked lime is added in a fourth preset amount;

[0033] If the second amount of sulfide to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for each time exceeding t, a preset increment of slaked lime is added on the basis of the fourth preset amount;

[0034] If the second amount of sulfide to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for more than n times t, then after adding n times of preset increments of slaked lime on the basis of the fourth preset amount, additional preset amount of baking soda is added;

[0035] If the second amount of sulfide to be reduced is lower than the second desulfurization amount, the fifth preset amount of slaked lime is added.

[0036] Exemplarily, when the system includes a reflux pipe, when a preset amount of baking soda is added, the reflux pipe is opened at the same time.

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

[0038] The glass kiln flue gas treatment system proposed in the embodiment of the present disclosure solves the problem that each device in the traditional glass kiln flue gas desulfurization, dust removal and denitrification integrated system using petroleum coke powder as fuel cannot be maintained online. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 The embodiment of the present disclosure provides an integrated glass kiln flue gas treatment system using petroleum coke as fuel;

[0040] Figure 2 Another glass kiln fume integrated treatment system using petroleum coke as fuel is provided in an embodiment of the present disclosure;

[0041] Figure 3It is a schematic flow chart of an integrated method for treating flue gas from a glass kiln using 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 slaked lime silo; 4. High temperature electrostatic precipitator; 5. Secondary desulfurization tower; 51. Baking soda silo; 52. Second slaked lime silo; 6. Composite ceramic fiber filter tube dust removal and denitrification integrated equipment; 61. Cyclone dust collector; 62. Return silo; 7. Induced draft unit; 8. Chimney. DETAILED DESCRIPTION

[0044] In order to make the purpose, technical solution and advantages of the embodiment of the present disclosure more clear, the embodiment of the present disclosure is further described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation methods described here are only used to explain the embodiment of the present disclosure and are not used to limit the embodiment of the present disclosure.

[0045] Embodiment 1:

[0046] like Figure 1 As shown, the embodiment of the present disclosure proposes an integrated flue gas treatment system for a glass kiln using petroleum coke as fuel, the system comprising: 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 denitrification integrated equipment 6 and an induced draft unit 7; the secondary waste heat boiler 1 comprises: a high-temperature section 11 and a low-temperature section 12; the high-temperature section of the secondary waste heat boiler is connected in parallel with the bypass heat exchanger 2, and 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 3, the high-temperature electrostatic precipitator 4, the secondary The composite ceramic fiber filter tube dust removal and denitrification integrated equipment 6, the low-temperature section 12 of the secondary waste heat boiler and the induced draft unit 7; the composite ceramic fiber filter tube dust removal and denitrification integrated equipment 6 includes a multi-stage series dust removal and denitrification bin (not shown in the figure), the gas pipeline of the secondary desulfurization tower is sequentially passed through the dust removal and denitrification bins at each stage, and an air inlet branch is arranged in each stage of the dust removal and denitrification bin, each air inlet branch is provided with a control valve, the air outlet of each stage of the dust removal and denitrification 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 the air pipeline connected to the low-temperature section.

[0047] The various devices in the glass kiln fume treatment system of the disclosed embodiment are connected through corresponding pipelines, wherein the induced draft unit can be 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.

[0048] As an example of an induced draft unit, 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 pipe.

[0049] The glass kiln flue gas treatment system of the disclosed embodiment adopts dry desulfurization technology, wherein the composite ceramic fiber filter tube dust removal and denitrification integrated equipment is a composite ceramic tube dust removal and denitrification integrated equipment, which has multiple dust removal and denitrification; the specific process route is: kiln flue gas → waste heat boiler high temperature section → primary dry desulfurization → high temperature electrostatic precipitator → secondary dry desulfurization → composite ceramic fiber integrated equipment denitrification → waste heat boiler low temperature section → induced draft fan → chimney. Compared with the traditional glass kiln flue gas treatment integrated system, each device in the glass kiln flue gas treatment system of the disclosed embodiment can be repaired online on the one hand: when the high temperature section of the waste heat boiler fails, a bypass heat exchanger is provided to replace the high temperature section; when the composite ceramic fiber filter tube integration fails, the faulty chamber can be closed separately for maintenance; when the low temperature section of the waste heat boiler fails, the induced draft fan can be directly entered through the bypass; on the other hand, it has a long service life, especially the composite ceramic fiber integrated core equipment composite ceramic fiber filter tube has a service life of more than 5 years, which can meet the needs of the kiln period, and the equipment will not be shut down during the normal production of the kiln.

[0050] For glass kilns whose fuel is petroleum coke powder, the sulfur content is relatively high, and the general sulfur content is 3000mg / m3. Therefore, the current desulfurization method selected for glass kilns whose fuel is petroleum coke powder is semi-dry or wet. The flue gas treatment system of the glass kiln in the embodiment of the present disclosure adopts dry desulfurization. The core desulfurization equipment is a primary desulfurization tower, a high-temperature electrostatic precipitator and a secondary desulfurization tower. The desulfurization is carried out through a primary desulfurization + high-temperature electrostatic precipitator + secondary desulfurization process, and a pure dry flue gas purification process is adopted. The system of the embodiment of the present disclosure has low resistance, no smoke tail, no wastewater, and no secondary pollution. Taking into account the complexity of the flue gas composition after the combustion of petroleum coke powder fuel, especially the certain adhesion of particulate matter in the flue gas, a primary desulfurization tempering system is set in the primary desulfurization tower. The primary desulfurization and conditioning system has the performance of flue gas desulfurization and conditioning at the same time. It removes fluoride from the flue gas and destroys the adhesion of particulate matter in the flue gas, ensuring that the barbs of the high-temperature electrostatic precipitator barb wire are not corroded and damaged, so that the barb wire reaches the longest service life. The primary desulfurization and conditioning system uses slaked lime as a desulfurization and conditioning agent. Because the pure dry desulfurization efficiency can reach a desulfurization efficiency of more than 85%, only setting up a primary desulfurization cannot ensure that sulfur dioxide is removed to less than 50mg / m3, so a secondary desulfurization system is configured to ensure the emission index of sulfur dioxide. The injection point of the denitrification reducing agent is usually set at the front end of the composite ceramic fiber integration. Because the front end flue is short, the ammonia and flue gas are not mixed evenly, resulting in an increase in ammonia consumption and ammonia escape not meeting the standard. The injection point of the denitrification reducing agent in the embodiment of the present disclosure is set at the front end of the desulfurization tower in order to mix more evenly with the flue gas, reduce the use of the denitrification reducing agent, and ensure the ammonia escape index.

[0051] The glass kiln flue gas treatment system of the disclosed embodiment also includes: a first slaked lime silo, which is arranged in the 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.

[0052] In the disclosed embodiment, the first slaked lime silo is arranged at the front end of the primary desulfurization tower, and slaked lime is stored therein. The discharge port of the first slaked lime silo is provided with a pipeline, so that the first slaked lime silo is connected to the gas pipeline between the primary desulfurization tower and the high temperature section of the secondary waste heat boiler. The discharge port of the first slaked lime silo can also be provided with a control valve to control the discharge, mainly controlling the size of the discharge port opening. The larger the discharge port is opened, the more material is discharged per unit time, and the smaller the discharge port is opened, the less material is discharged per unit time. The control valve can be controlled by the control unit to realize automatic control of feeding.

[0053] The glass kiln flue gas treatment system of the disclosed embodiment also includes: a spare baking soda silo and a second slaked lime silo which are sequentially arranged between the high-temperature electrostatic precipitator and the secondary desulfurization tower, for providing baking soda and slaked lime to the secondary desulfurization tower.

[0054] In the system of the embodiment of the present disclosure, the spare baking soda silo and the second slaked lime silo are arranged at the front end of the secondary desulfurization tower, the spare baking soda silo stores baking soda, the second slaked lime silo stores slaked lime, the discharge ports of the spare baking soda silo and the second slaked lime silo are both provided with pipelines, the pipelines of the spare baking soda silo and the second slaked lime silo are respectively connected to the gas pipeline between the secondary desulfurization tower and the high-temperature electric precipitator, and the discharge ports of the spare baking soda silo and the second slaked lime silo can also be respectively provided with control valves to control the discharge. The control valve can be controlled by the control unit to realize automatic control of feeding.

[0055] A denitrification reducing agent injection point is arranged at the front end of the spare baking soda silo, that is, close to the rear end gas transmission pipeline of the high-temperature electrostatic precipitator, to inject the denitrification reducing agent.

[0056] The glass kiln flue gas treatment system of the disclosed embodiment 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.

[0057] The recovery port of the secondary desulfurization tower in the system of the embodiment of the present disclosure is close to the air inlet and located above the air inlet. The gas pipeline connected to the air outlet of the cyclone dust collector is arranged near the discharge port of each dust removal and denitration bin of the composite ceramic fiber filter tube dust removal and denitration integrated equipment, that is, below, each air inlet branch on the gas pipeline faces the discharge port of the corresponding dust removal and denitration bin, and the air outlet of each stage of the dust removal and denitration bin is away from the corresponding discharge port, that is, it is arranged above the corresponding dust removal and denitration bin, and the air outlet is connected to the gas 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 air outlet branch.

[0058] In the system of the embodiment of the present disclosure, each pipeline is provided with corresponding sensors according to actual conditions to detect the temperature, gas flow rate, sulfide concentration, nitride concentration, etc. in the pipeline, so that the flue gas finally discharged by the system can be purified to meet the requirements.

[0059] The flue gas discharged from the glass kiln enters the system of the embodiment of the present disclosure through the flue gas duct. The flue gas first enters the high temperature section of the secondary waste heat boiler through the flue gas duct. The first gas flow rate sensor, the first sulfide gas concentration detection sensor, and the first temperature sensor can be set near the high temperature section of the secondary waste heat boiler in the flue gas duct. The second gas flow rate sensor and the second temperature sensor are set in the gas 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 conditions, which is not limited to the above sensors.

[0060] The first gas flow rate sensor and the second gas flow rate sensor can be used to detect the gas flow rate after the flue gas passes through the high temperature section of the secondary waste heat boiler or the bypass heat exchanger. Generally speaking, the gas flow rate will be weakened, but if it encounters the high temperature section of the secondary waste heat boiler or the bypass heat exchanger, the gas flow rate may change significantly or not significantly. For example, the gas flow rate detected by the first gas flow rate sensor is v1, and the gas flow rate detected by the second gas flow rate sensor is v2, v1-v 2＝Δ v, Δ If v is between [a, b], the high temperature section of the secondary waste heat boiler or the bypass heat exchanger is considered normal. Δ v < a, or Δ v>b, it is preliminarily judged that the high temperature section of the secondary waste heat boiler or the bypass heat exchanger is faulty, and further judgment can be made in combination with the temperature. At this time, it is best to stop the high temperature section of the secondary waste heat boiler or the bypass heat exchanger. The gas flow rate can also be combined with the sulfide gas concentration to calculate the sulfide content per unit time to further determine the method of adding slaked lime.

[0061] Furthermore, the temperature of the high-temperature section of the secondary waste heat boiler or the pipes at both ends of the bypass heat exchanger can also be detected by the second temperature sensor to determine whether the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger is operating normally. If the detection temperature T of the second temperature sensor is lower than or equal to the preset temperature T0, the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger is normal. If T>T0, when the expected temperature is not reached, the high-temperature section or bypass of the secondary waste heat boiler is faulty, which can also be further verified in combination with the gas flow rate. At this time, the high-temperature section of the secondary waste heat boiler or the bypass heat exchanger needs to be closed for further inspection. The system of the embodiment of the present disclosure can also be provided with a nitride detection sensor in the pipeline at the rear end of the primary desulfurization tower. Those skilled in the art can set it according to actual conditions, which will not be elaborated here.

[0062] In the system of the embodiment of the present disclosure, 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; 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 composite ceramic fiber filter tube dust removal and denitrification integrated equipment.

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

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

[0065] That is to say, the air inlet and outlet of the dust removal and denitrification bin of the integrated composite ceramic fiber filter tube dust removal and denitrification equipment are both provided with gas flow rate sensors. The gas flow rate at the air inlet and outlet of each dust removal and denitrification bin can be used to determine whether the corresponding dust removal and denitrification bin is faulty. Temperature sensors can also be added to the air inlet and outlet of each dust removal and denitrification bin to determine whether the dust removal and denitrification bin is faulty alone or in combination with the airflow. The seventh gas flow rate sensor of the gas transmission pipeline between the integrated composite ceramic fiber filter tube dust removal and denitrification equipment and the low-temperature section of the secondary waste heat boiler and the eighth gas flow rate sensor at the rear end of the low-temperature section of the secondary waste heat boiler can be used to determine whether the low-temperature section is faulty. Temperature sensors can also be added to the front and rear ends of the low-temperature section respectively to determine whether the low-temperature section is faulty together with the gas flow rate sensor or alone. The judgment method can adopt the above-mentioned method, which will not be repeated here.

[0066] On the other hand, the embodiment of the present disclosure provides an integrated treatment method for glass kiln flue gas using petroleum coke as fuel, which is applied to the above-mentioned glass kiln flue gas treatment system. The desulfurization process is divided into two stages, namely the first stage and the second stage. The first stage includes: a first desulfurization mode and a second desulfurization mode, and the second stage includes: a third desulfurization mode and a fourth desulfurization mode. The method includes:

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

[0068] Step S1, obtaining a first flue gas flow rate and a first sulfide concentration in a flue gas duct, and a second flue gas flow rate in a gas transmission pipeline between a high temperature section and a primary 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, and the sulfide mainly refers to sulfur dioxide SO2.

[0070] Step S2, according to the second flue gas flow rate and the first sulfide concentration, determine the first sulfide amount per unit time in the gas pipeline at the front end of the primary desulfurization tower, combined with the first preset sulfide amount per unit time after the flue gas flows through the primary desulfurization tower for desulfurization, to obtain the first amount of 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 rear end of the primary desulfurization tower, there is a first preset sulfide amount. The actual content of sulfide at the front end of the primary desulfurization tower is subtracted from the first preset sulfide amount to obtain the first amount of sulfide to be reduced. The sulfide content 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 amount of desulfurization. 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 amount of slaked lime added per unit time. It can be determined based on the maximum amount of slaked lime added per unit time, and the flue gas flow rate can be ignored. The unit time can be 1h~10min, which can be set according to actual conditions. The first sulfide concentration mainly refers to the mass concentration C of sulfur dioxide SO2 s , in mg / m3, the second flue gas velocity v2, in m / h, the unit time can be confirmed according to the actual situation, combined with the pipe cross-sectional area s, s = π / 4 × D 2 , D is the inner diameter of the pipe, which can determine the flue gas flow rate Q per unit time in the pipe, in units of m3 / h, Q = s·v2, combined with the mass concentration of sulfur dioxide SO2 in the flue gas C s , the mass content of the first sulfide in the pipeline per unit time can be determined, m s =C s Q, that is, the emission, is in g / h. Based on the chemical reaction relationship between slaked lime Ca(OH)2 and sulfur dioxide, the amount of slaked lime added per unit time can be calculated. Theoretically, about 1.156 grams of Ca(OH)2 is required for each gram of SO2. The calculation process is not repeated here. The common amount of slaked lime added is 1.2 to 1.5 of that of sulfide, which can be adjusted according to actual conditions. If the first sulfide concentration is the volume concentration of sulfur dioxide C SO2 , the mass flow rate of sulfur dioxide can be calculated by combining the flue gas density ρ, unit kg / m3, and the flue gas flow rate Q, where the flue gas density ρ = P / RT. P is the absolute pressure of the pipeline (Pa), R is the specific gas constant (J / (kg·K)), which is approximately 287J / (kg·K) for air, but if the specific composition of the flue gas is known, use the corresponding mixed gas constant; T is the absolute temperature of the pipeline (K). The sulfide content in the pipeline is variable, so the amount of slaked lime added needs to be dynamically controlled to achieve the best desulfurization effect and the least cost investment. The amount of slaked lime added can be controlled by adjusting the discharge port opening of the control valve at the discharge port of the first slaked lime silo. The amount of sulfide actually reduced after desulfurization in the primary desulfurization tower can be determined based on the second sulfide concentration and the third flue gas flow rate in the pipeline after desulfurization in the primary desulfurization tower.

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

[0073] Because the desulfurization amount per unit time of the first-level desulfurization tower is determined by the amount of slaked lime input per unit time, at this time, the sulfide concentration is high and the flow rate is also high, resulting in a high sulfide content per unit time. The maximum amount of slaked lime is used. This situation is relatively rare. When the amount of the first sulfide to be reduced is not greater than the current maximum desulfurization amount per unit time of the first-level 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 current maximum desulfurization amount per unit time of the primary desulfurization tower, the second desulfurization mode is adopted; wherein, the second desulfurization mode is to add slaked lime using a second preset amount, and the second preset amount is less than the first preset amount.

[0075] The first desulfurization mode and the second desulfurization mode can be switched according to the actual situation. That is to say, the second desulfurization mode can cope with the amount of the first sulfide to be reduced that is not greater than the maximum desulfurization amount. After the flue gas passes through the first desulfurization tower, the concentration of sulfur dioxide is reduced. Combined with the current flue gas flow rate, the actual amount of sulfide is obtained. In the second stage, slaked lime can be added according to the actual situation.

[0076] Phase 2:

[0077] Step S5, obtaining the second sulfide concentration and the third flue gas flow rate of the flue gas after desulfurization in the primary desulfurization tower; wherein, according to the third flue gas flow rate and the second sulfide concentration, the second sulfide amount per unit time in the gas pipeline at the front end of the secondary desulfurization tower is determined, and combined with the second preset sulfide amount per unit time after the flue gas flows through the secondary desulfurization tower for desulfurization, the second sulfide amount to be reduced per unit time is obtained.

[0078] The second sulfide amount is the actual sulfide content in the pipeline after the flue gas flows through the primary desulfurization tower for desulfurization. The second preset sulfide amount is close to the final flue gas discharged. Therefore, step S3 supplements the desulfurization of the primary desulfurization tower to ensure that the sulfur dioxide SO2 content in the flue gas after desulfurization is 50mg / m 3 the following.

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

[0080] That is to say, the amount of the second sulfide to be reduced is small, and a low amount of slaked lime can be used to achieve a desulfurization effect that meets the requirements. The preset amount of slaked lime can be set according to the actual situation.

[0081] Step S7: if the second sulfide amount is greater than the first preset sulfide amount, the second sulfide amount to be reduced is relatively high, and the fourth desulfurization mode is adopted; the fourth desulfurization mode is to determine the corresponding relationship between the second sulfide amount to be reduced and the preset desulfurization amount, and to determine 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 causes the second sulfide amount to be greater than the first preset sulfide amount, and the second sulfide amount to be reduced is relatively high, then, according to the corresponding relationship between the second sulfide amount to be reduced and the preset desulfurization amount, the desulfurizer of 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 delivery flow rate.

[0083] The determining of the correspondence between the second amount of sulfide to be reduced and the preset desulfurization amount, and determining the addition of a corresponding amount of desulfurizer, comprises:

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

[0085] Step S72: if the second sulfide amount to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for more than the time t, then a preset increment Δm of slaked lime is added to the fourth preset amount. That is, the flow rate is gradually increased with the increase of time.

[0086] Step S73: if the second amount of sulfide to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for more than n times t, then after adding n preset increments of slaked lime on the basis of the fourth preset amount, an additional preset amount of baking soda is added.

[0087] Step S74: if the second amount of sulfide to be reduced is lower than the second desulfurization amount, slaked lime is added in a fifth preset amount.

[0088] The first to fourth fifth preset delivery amounts all refer to the delivery amount per unit time, and the unit can be g / h.

[0089] If the amount of the second sulfide to be reduced is high and lasts for a long time, it means that the concentration of sulfur dioxide in the flue gas from the primary desulfurization tower is high. Gradually increase the amount of slaked lime to achieve the purpose of rapid desulfurization; when the flue gas sulfide concentration is large and the cumulative time is long, it means that the flue gas adhesion is relatively large. In order to effectively reduce the flue gas sulfide concentration, baking soda can be added. Under normal circumstances, the amount of the second sulfide to be reduced will not be very high. Even if the amount of the second sulfide to be reduced reaches a high level, the addition of baking soda and slaked lime can ensure that the desulfurization meets the requirements. The main thing is how to control the addition of baking soda and slaked lime, which can save costs and meet emission standards, and can further destroy the adhesion of particulate matter in the flue gas.

[0090] The method further includes: if the difference in 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, the high temperature section is shut down, and the bypass heat exchanger is switched to operate;

[0091] If the difference between the flue gas flow velocity of each outlet branch of the composite ceramic fiber filter tube dust removal and denitrification integrated equipment and the flue gas flow velocity and / or temperature at the air inlet end is not within the corresponding preset threshold, the corresponding dust removal and denitrification bin of the composite ceramic fiber filter tube dust removal and denitrification integrated equipment is faulty, and the faulty dust removal and denitrification bin is closed;

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

[0093] When the induced draft unit is also connected to the dust removal and denitrification bins of the composite ceramic fiber filter tube dust removal and denitrification integrated equipment, after the low-temperature section of the secondary waste heat boiler fails, the low-temperature section is closed and the induced draft unit is switched to operate.

[0094] Embodiment 2:

[0095] Based on the first embodiment, Figure 2 As shown, the system may further include a return pipe between the primary desulfurization tower and the secondary desulfurization tower, so that the flue gas from the secondary desulfurization tower may return to the primary desulfurization tower.

[0096] Specifically, a reflux pipe can be added near the top or 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 provided on the reflux pipe near the gas outlet of the primary desulfurization tower to allow the flue gas from the secondary desulfurization tower to reflux to the primary desulfurization tower, thereby preventing the flue gas from the primary reflux tower from flowing directly to the secondary desulfurization tower.

[0097] The air inlet of the reflux pipe is connected to the top of the secondary desulfurization tower and is provided with a control valve. A one-way valve is provided near the air outlet of the reflux pipe and a Venturi structure may be provided. The air outlet of the reflux pipe is provided near the air outlet of the primary desulfurization tower or in 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, the reflux pipe can be opened.

[0099] Open the reflux pipe to allow the flue gas from 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 the particles in the flue gas and recycle the baking soda.

[0100] The above is only a preferred implementation of the embodiment of the present disclosure. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principles of the embodiment of the present disclosure. These improvements and modifications should also be considered as the protection scope of the embodiment 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; The composite ceramic fiber filter tube dust removal and denitrification integrated equipment includes a multi-stage parallel dust removal and denitrification bin, the gas pipeline of the secondary desulfurization tower is sequentially passed through the dust removal and denitrification bins at each stage, and an air inlet branch is arranged in each stage of the dust removal and denitrification bin, each air inlet branch is provided with a control valve, the air outlet of each stage of the dust removal and denitrification 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.

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, characterized in that The system further comprises: a first slaked lime silo, which is arranged 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.

4. The system according to claim 1, characterized in that The system also includes: a spare baking soda silo and a second slaked lime silo which are sequentially arranged in the gas pipeline between the high-temperature electrostatic precipitator and the secondary desulfurization tower, and are used to provide baking soda and slaked lime to the secondary desulfurization tower.

5. The system according to any one of claims 1 to 4, 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.

6. The system according to any one of claims 1 to 4, characterized in that: The system further comprises: a reflux pipeline, wherein 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 refluxes to the primary desulfurization tower.

7. An integrated treatment method for glass furnace flue gas using petroleum coke as fuel, applied to the glass furnace flue gas treatment system according to any one of claims 1 to 6, characterized in that: The method comprises: Phase 1: Obtaining a first flue gas flow rate and a first sulfide concentration in the flue gas duct, and a second flue gas flow rate in the gas transmission pipeline between the high temperature section and the primary desulfurization tower; According to the second flue gas flow rate and the first sulfide concentration, the first sulfide amount per unit time in the gas transmission pipeline at the front end of the primary desulfurization tower is determined, and the first preset sulfide amount per unit time after the flue gas flows through the primary desulfurization tower for desulfurization is combined to obtain the first amount of sulfide to be reduced per unit time; If the amount of the first sulfide to be reduced is greater than the maximum desulfurization amount of the primary desulfurization tower, the first desulfurization mode is adopted; wherein the first desulfurization mode is to use the first preset amount of addition at the front end of the primary desulfurization tower, that is, to add slaked lime at the maximum amount of addition; the desulfurization amount of the primary desulfurization tower is determined according to the slaked lime input flow rate; If the amount of the first sulfide to be reduced is not greater than the maximum desulfurization capacity of the primary desulfurization tower, the second desulfurization mode is adopted; wherein, the second desulfurization mode is to add slaked lime in a second preset amount.

8. The method according to claim 7, characterized in that The method further comprises: Phase 2: Obtain the second sulfide concentration and the third flue gas flow rate of the flue gas after desulfurization by the primary desulfurization tower; wherein, according to the third flue gas flow rate and the second sulfide concentration, determine the second sulfide amount per unit time in the gas transmission pipeline at the front end of the secondary desulfurization tower, and combine the second preset sulfide amount per unit time after the flue gas flows through the secondary desulfurization tower for desulfurization, to obtain the second sulfide amount to be reduced per unit time; Determine whether the second sulfide amount is less than or equal to the first preset sulfide amount. If so, the second sulfide amount to be reduced is low, and the third desulfurization mode is adopted; wherein the third desulfurization mode is to add slaked lime to the front end pipeline of the secondary desulfurization tower according to the third preset amount; If not, the second amount of sulfides 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 second amount of sulfides to be reduced and the preset desulfurization amount to determine the desulfurizer of the corresponding flow rate.

9. The method according to claim 8, characterized in that The determining of the correspondence between the second amount of sulfide to be reduced and the preset desulfurization amount to determine the desulfurization agent to be added with the corresponding flow rate includes: If the second amount of sulfide to be reduced is between the first desulfurization amount and the second desulfurization amount, slaked lime is added in a fourth preset amount; If the second amount of sulfide to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for each time exceeding t, a preset increment of slaked lime is added on the basis of the fourth preset amount; If the second amount of sulfide to be reduced continues to be between the first desulfurization amount and the second desulfurization amount for more than n times t, then after adding n times of preset increments of slaked lime on the basis of the fourth preset amount, additional preset amount of baking soda is added; If the second amount of sulfide to be reduced is lower than the second desulfurization amount, the fifth preset amount of slaked lime is added.

10. The method according to claim 9, characterized in that When the system includes a return line, When adding the preset amount of baking soda, open the reflux pipe at the same time.

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