CN113640468A - Multifunctional flue gas purification evaluation method - Google Patents

Multifunctional flue gas purification evaluation method Download PDF

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CN113640468A
CN113640468A CN202110924038.8A CN202110924038A CN113640468A CN 113640468 A CN113640468 A CN 113640468A CN 202110924038 A CN202110924038 A CN 202110924038A CN 113640468 A CN113640468 A CN 113640468A
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flue gas
temperature range
process temperature
gas purification
efficiency
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刘广涛
房豪杰
晏金炜
冯波
邓四化
赵开兴
连久翔
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Shanghai Institute of Electromechanical Engineering
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    • G—PHYSICS
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    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
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Abstract

本发明公开了一种多功能烟气净化评价方法，该方法通过污染物发生器组件供应污染物并随烟气进入加热器（1）中，开启引风机（5）使烟气流经加热器、干法反应器（2）、除尘器（3）的滤料（4）和引风机；污染物中包括酸性污染物时，化学药剂供应器组件向干法反应器中投加脱酸吸收剂干粉；污染物中包括氮氧化物时，化学药剂供应器组件向进入除尘器前的烟气中喷洒脱硝还原剂。本发明可以通过温度区间、过滤材料、药剂投加等工艺流程的控制和调节模拟不同工况下的烟气净化处理情况，实现各种条件下的试验，从而评价不同材料对除尘、脱酸、脱硝、脱除二噁英等污染物的实际净化效果，适用于冷态、热态等工况条件，结构简单，易于操作，成本低。

Figure 202110924038

The invention discloses a multifunctional flue gas purification evaluation method. The method supplies pollutants through a pollutant generator component and enters a heater (1) with the flue gas, and starts the induced draft fan (5) to make the flue gas flow through the heater. , dry process reactor (2), filter material (4) of dust collector (3) and induced draft fan; when the pollutants include acidic pollutants, the chemical agent supplier component adds deacidification absorbent into the dry process reactor Dry powder; when nitrogen oxides are included in the pollutants, the chemical supply unit sprays denitration reducing agent into the flue gas before entering the dust collector. The present invention can simulate the flue gas purification treatment situation under different working conditions through the control and adjustment of technological processes such as temperature interval, filter material, and chemical dosage, so as to realize the test under various conditions, so as to evaluate the effect of different materials on dust removal, deacidification, The actual purification effect of denitration, removal of dioxins and other pollutants is suitable for cold, hot and other working conditions, with simple structure, easy operation and low cost.

Figure 202110924038

Description

Multifunctional flue gas purification evaluation method
Technical Field
The invention relates to a flue gas purification simulation method, in particular to a multifunctional flue gas purification evaluation method.
Background
At present, incineration is the mainstream treatment process for treating domestic garbage and hazardous waste, biomass incineration power generation can realize resource utilization of agricultural and forestry waste, but the incineration process can generate substances containing particulate matters, HCl and SO2、NOxAnd harmful substances such as dioxin. The flue gas deacidification process in the prior art mainly comprises a dry method, a semi-dry method and a wet method, a bag-type dust remover is mainly adopted as a dust removal process, and the denitration process mainly comprises SNCR and SCR denitration technologies. The SNCR denitration technology is to spray ammonia water, urea solution and other amino reducing agents, reducing agents and NO into the temperature window of 850-1100 DEG CxThe reaction is carried out to remove the waste gas, and the denitration efficiency is between 30 and 60 percent; the SCR denitration technology is in O2And in the presence of a heterogeneous catalyst, using a reducing agent NH within a temperature window of 180 ℃ to 230 DEG C3NO in the smoke x Reduction to N2And H2O, the denitration efficiency can reach more than 80%. The technology for removing dioxin and heavy metal is mainly characterized in that activated carbon is sprayed into a flue gas pipeline before entering a dust collector, the activated carbon is used for adsorbing heavy metal and dioxin, after the activated carbon is sprayed into a flue, heavy metal pollutants such as dioxin, Hg and the like are adsorbed in the flue but are not saturated, then the activated carbon and the flue gas enter a bag type dust collector together and are adsorbed on the surface of a filter bag, and the activated carbon is in full contact with the flue gas passing through the surface of the filter bag, so that the aim of removing the heavy metal and the dioxin in the flue gas is fulfilled finally. The process is widely applied to the projects of household garbage incineration and dangerous waste incineration at present.
With the continuous progress of the technology, new treatment processes are emerging continuously, and treatment processes (such as catalytic ceramic filter tubes, catalytic cloth bags and the like) with integrated functions of dust removal, denitration and dioxin removal are beginning to be applied to the project of flue gas purification, partial waste incineration and dangerous waste incineration of a biomass power plant. However, the treatment effect of the new treatment process still remains in the theoretical analysis stage of the laboratory, the actual treatment effect is difficult to evaluate, and the evaluation cost is very high if the actual treatment effect is directly evaluated on the engineering project.
Chinese patent ZL201611219033.0 discloses a device and a method for detecting performance of a filter bag or a filter cartridge, and particularly discloses a device for detecting performance of the filter bag or the filter cartridge, which is composed of an automatic feeding system, a filter bag system, an ash removal system, a detection system and a control system, and the device is used for evaluating the dust removal effect of the filter bag or the filter cartridge. The device can only be carried out under the cold state condition, can not realize the simulation actual flue gas operating mode under the hot state condition, can not accurately evaluate the actual dust removal effect of filter bag or strain a section of thick bamboo.
Chinese patent CN201910215838.5 discloses a testing device and an evaluation method based on the denitration effect of a catalyst-loaded filter material, and specifically discloses a testing device composed of a flue gas bottle, a reducing agent gas bottle, a gas mixing chamber, and a denitration reaction chamber, wherein a denitration catalyst-loaded filter material is placed in the denitration reaction chamber. The concentration before and after the denitration reaction of the pollutant gas is detected and evaluated by the testing device. The thickness of the denitration catalyst load filter material in the evaluation device is 2.5-4.5mm, the denitration catalyst load filter material is only suitable for small-scale evaluation in a laboratory, and the test result cannot replace the denitration effect of a large-scale denitration catalyst load filter material in an actual project. Meanwhile, the test device is only suitable for the evaluation of denitration reaction and does not have evaluation functions of dedusting, deacidification, dioxin removal and the like.
Disclosure of Invention
The invention aims to provide a multifunctional flue gas purification evaluation method, which can simulate flue gas conditions under different working conditions, meet different test conditions by controlling and adjusting process flows such as a temperature interval, a filtering material, a medicament adding and the like, realize simulation of actual purification treatment of different flue gases, be used for evaluating flue gas purification effects and have high accuracy of evaluation results.
The invention is realized by the following steps:
a multifunctional flue gas purification evaluation method is realized based on a multifunctional flue gas purification evaluation device; the multifunctional flue gas purification evaluation device comprises a heater, a dry-process reactor, a dust remover, a filter material, an induced draft fan, a pollutant generator component and a chemical agent supplier component; the input end of the heater is provided with a flue gas supply pipeline, the output end of the pollutant generator assembly is connected to the input end of the heater, and the output end of the heater is connected with the input end of the dry-method reactor; the output end of the dry method reactor is connected with the air inlet of the dust remover, the filter material is arranged in the dust remover, and the air outlet of the dust remover is connected with the induced draft fan; the chemical agent supply assembly is respectively connected with the dry reactor and the dust remover;
the multifunctional flue gas purification evaluation method comprises the following steps: supplying pollutants through a pollutant generator assembly, enabling the pollutants to enter a heater along with flue gas, and starting an induced draft fan to enable the flue gas containing the pollutants to sequentially flow through the heater, a dry-process reactor, a filter material of a dust remover and the induced draft fan; when the pollutants comprise acidic pollutants, adding deacidification absorbent dry powder into the dry reactor by the chemical agent supplier component; when the pollutants comprise nitrogen oxides, the chemical agent supplier assembly sprays denitration reducing agents into the smoke before entering the dust remover.
The filter material is coated with a catalyst, the diameter of the filter material is 50-200mm, the length of the filter material is 0.5-6m, and the filter material is a catalyst ceramic tube or a catalyst cloth bag;
when the filter material is a catalyst ceramic tube, the process temperature interval of the catalyst ceramic tube comprises: at the temperature of 150 ℃ at 120-; when the filter material is a catalytic cloth bag, the process temperature interval of the catalytic cloth bag comprises: at a temperature of between 120 ℃ and 150 ℃, at a temperature of between 150 ℃ and 180 ℃ and at a temperature of between 180 ℃ and 220 ℃.
Supplying SO through pollutant generator assembly when evaluating desulfurization and dust removal efficiencyxAnd enters the heater along with the flue gas, and the induced draft fan is started to lead the SO contained in the flue gas to bexThe flue gas flows through a heater, a dry-method reactor, a filter material of a dust remover and a draught fan in sequence; chemical agent supplierThe component adds deacidification absorbent dry powder into the dry reactor; arranging a first inlet flue gas detector at the upstream of the air inlet of the dry reactor and detecting the obtained SOxIn a concentration of not more than 2000mg/m3A second inlet smoke detector is arranged at the upstream of the air inlet of the dust remover, and the concentration of the detected dust is not more than 60mg/m3；
The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency hydrated lime powder and slaked lime powder; wherein the sodium bicarbonate powder is mixed with SOxIn a molar ratio of 0.5-2, high-efficiency slaked lime powder and SOxIn a molar ratio of 0.8-3, slaked lime powder and SOxIn the range of 1 to 5;
when the filter material is a catalyst ceramic tube and the filtering air speed is 0.5-2.0m/min, the dust purification efficiency of the filter material is more than 99.93% for each process temperature interval; when the filter material is a catalytic cloth bag and the filtering air speed is 1.0m/min, the dust purification efficiency of the filter material is more than 99.94% in each process temperature interval;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is sodium bicarbonate powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 120 ℃ plus 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-95% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-99% in the process temperature range of 250-300 ℃; for the process temperature range of 350 ℃ and 400 ℃, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-99%;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is high-efficiency hydrated lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-60% for the process temperature range of 120 ℃ plus 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-90% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-99% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-95% in the process temperature range of 350-400 ℃;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is slaked lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 120 ℃ plus 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-50% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 15-50% in the process temperature range of 350-400 ℃.
When the HCl removal efficiency is evaluated, HCl is supplied by a pollutant generator assembly and enters a heater along with the flue gas, and an induced draft fan is started to enable the flue gas containing the HCl to sequentially flow through the heater, a dry-process reactor, a filter material of a dust remover and the induced draft fan; adding deacidification absorbent dry powder into the dry reactor by a chemical agent supplier component; arranging a first inlet flue gas detector at the upstream of the gas inlet of the dry reactor and detecting that the concentration of HCl obtained does not exceed 20000mg/m3；
The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency hydrated lime powder and hydrated lime powder, wherein the molar ratio of the sodium bicarbonate powder to HCl is 0.5-1.5, the molar ratio of the high-efficiency hydrated lime powder to HCl is 0.6-2, and the molar ratio of the hydrated lime powder to HCl is 1-3;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is sodium bicarbonate powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-96% for a process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is high-efficiency hydrated lime powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-85% for a process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%;
when the filter material is a catalyst ceramic tube and the deacidification absorbent dry powder is slaked lime powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-70% for the process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 35-70%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-60%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-50%.
Evaluation of NOxFor efficiency of removal, NO is supplied through pollutant generator assemblyxAnd enters a heater along with the flue gas, and a draught fan is started to lead NO to be containedxThe flue gas flows through a heater, a dry-method reactor, a filter material of a dust remover and a draught fan in sequence, and the dry-method reactor is not started; spraying ammonia water serving as a denitration reducing agent into the flue gas before entering the dust remover by the chemical agent supplier component to ensure that the molar ratio of the ammonia nitrogen in the flue gas is 0.5-3; arranging a first inlet flue gas detector upstream of the inlet of the dry reactor and detecting the resulting NOxThe concentration of (A) is not more than 800mg/m3；
When the filter material is a catalyst ceramic tube, the NO of the multifunctional flue gas purification evaluation device is increased by 150 ℃ in the process temperature range of 120 DEG CxThe removal efficiency is 10-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 30-95%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 250 ℃ and 300 DEG CxThe removal efficiency is 50-98%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 350 ℃ and 400 DEG CxThe removal efficiency is 55-98%.
When the filter material is a catalytic cloth bag, the NO of the multifunctional flue gas purification evaluation device is increased by 150 ℃ in the process temperature range of 120 DEG CxThe removal efficiency is 10-40%; for the process temperature range of 150 ℃ and 180 ℃, multiple functions are realizedNO of flue gas purification evaluation devicexThe removal efficiency is 30-80%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 40-95%.
When the dioxin removal efficiency is evaluated, supplying dioxin through a pollutant generator assembly and entering a heater along with flue gas for heating, and starting an induced draft fan to enable the flue gas containing the dioxin to sequentially flow through the heater, a dry reactor, a filter material of a dust remover and the induced draft fan, wherein the dry reactor is not started; a first inlet flue gas detector is arranged at the upstream of an air inlet of the dry reactor, and the concentration of dioxin obtained by sampling the first inlet flue gas detector and analyzing the sample in a laboratory is not more than 100ngTEQ/Nm3；
When the filter material is a catalytic ceramic tube, the removal efficiency of dioxin in the process temperature range of 120-150 ℃ is 60-70%, wherein the decomposition efficiency of gaseous dioxin is 65%; for the process temperature range of 180 ℃ and 220 ℃, the dioxin removal efficiency of the filter material is 70-80%, wherein the decomposition efficiency of gaseous dioxin is 75%; for the process temperature range of 250-300 ℃, the dioxin removal efficiency of the filter material is 85-95%, wherein the decomposition efficiency of gaseous dioxin is 85%; for the process temperature range of 350-400 ℃, the dioxin removal efficiency of the filter material is 85-99.6%, wherein the decomposition efficiency of gaseous dioxin is 90%;
when the filter material is a catalytic cloth bag, the dioxin removal efficiency of the filter material is 50-60% for the process temperature interval of 120-150 ℃; for the process temperature range of 150 ℃ and 180 ℃, the dioxin removal efficiency of the filter material is 60-70%; the removal efficiency of dioxin in the filter material is 70-80% for the process temperature range of 180-220 ℃.
Evaluation of NOxIn the case of influence on efficiency of dioxin removal, NO is supplied through pollutant generator modulexAnd dioxin are heated by the heater along with the flue gas, and the induced draft fan is started to lead the NO to be containedxAnd the flue gas of the dioxin sequentially flows through a heater, a dry reactor, a filter material of a dust remover and an induced draft fan, and the dry reactor is not started; the chemical agent supply assembly sprays denitration reducing agent ammonia water into the flue gas before entering the dust remover; under the working condition that the ammonia nitrogen molar ratio in the flue gas is not changedA first inlet flue gas detector is arranged at the upstream of an air inlet of the dry reactor, and the concentration of dioxin obtained by sampling and laboratory analysis by the first inlet flue gas detector is 5-10ngTEQ/Nm3NO detected by the first inlet smoke detectorxThe concentration is 400-1200mg/m3；
The filter material is a catalyst ceramic tube, and the dioxin removal efficiency is 40-55% for each process temperature interval of 120-150 ℃; for each process temperature range of 180 ℃ and 220 ℃, the dioxin removal efficiency is 50-65%; for each process temperature range of 250 ℃ and 300 ℃, the dioxin removal efficiency is 60-85 percent; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 70-89%.
When the influence of HCl on the dioxin removal efficiency is evaluated, HCl and dioxin are supplied through a pollutant generator assembly and enter a heater along with flue gas for heating, and an induced draft fan is started to enable the flue gas containing HCl and dioxin to sequentially flow through the heater, a dry method reactor, a filter material of a dust remover and the induced draft fan; adding deacidification absorbent dry powder into the dry reactor by a chemical agent supplier component; a first inlet flue gas detector is arranged at the upstream of an air inlet of the dry reactor, and the concentration of dioxin obtained by sampling and laboratory analysis of the first inlet flue gas detector is 5-10ngTEQ/Nm3The concentration of HCl detected by the first inlet flue gas detector is 500-3；
The filter material is a catalyst ceramic tube; when the dry powder of the deacidification absorbent is slaked lime powder, the molar ratio of the slaked lime powder to HCl is 1, when the dry powder of the deacidification absorbent is sodium bicarbonate powder, the molar ratio of the sodium bicarbonate powder to HCl is 1, and when the dry powder of the deacidification absorbent is high-efficiency slaked lime powder, the molar ratio of the high-efficiency slaked lime powder to HCl is 1.5; the removal efficiency of the dioxin is 20-40% in the process temperature range of 120 ℃ plus 150 ℃; the removal efficiency of the dioxin is 20-60% for the process temperature range of 180 ℃ and 220 ℃; the process temperature range is 250 ℃ and 300 ℃, and the dioxin removal efficiency is 20-80%; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 30-90%.
Evaluation of SOxIn the case of influence on efficiency of dioxin removal, SO is supplied from a pollutant generator modulexAnd dioxanHeating quartz and flue gas in a heater, starting a draught fan to make SOxAnd the flue gas of the dioxin sequentially flows through a heater, a dry-process reactor, a filter material of a dust remover and an induced draft fan; adding deacidification absorbent dry powder into the dry reactor by a chemical agent supplier component; a first inlet flue gas detector is arranged at the upstream of an air inlet of the dry reactor, and the concentration of dioxin obtained by sampling and laboratory analysis of the first inlet flue gas detector is 5-10ngTEQ/Nm3The SO detected by the first inlet flue gas detectorxThe concentration of (b) is 200-2000mg/m3；
The filter material is a catalyst ceramic tube; when the dry powder of the desulfurization absorbent is high-efficiency hydrated lime powder, the high-efficiency hydrated lime powder is mixed with SOxIs 2, when the dry powder of the desulfurization absorbent is sodium bicarbonate, the sodium bicarbonate is mixed with SOxIs 1.5, when the dry powder of the desulphurization absorbent is slaked lime powder, the slaked lime powder and SOxIs 3;
the removal efficiency of dioxin is 10-30% in the process temperature range of 120 ℃ plus 150 ℃; the process temperature range is 180 ℃ and 220 ℃, and the dioxin removal efficiency is 20-50%; the process temperature range is 250 ℃ and 300 ℃, and the dioxin removal efficiency is 30-70%; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 40-80%.
When the pressure difference was evaluated:
under the cold state condition, starting the induced draft fan, enabling the flue gas to sequentially flow through the heater, the dry-process reactor, the filter material of the dust remover and the induced draft fan, and not starting the heater; setting pressure difference sensors on an air inlet flue and an air outlet flue of the dust remover, measuring pressure difference through the pressure difference sensors under the condition that the filtering air speed is not changed, wherein the pressure difference range of different filter materials is 300-1200 pa; changing the filtering wind speed, and measuring the pressure difference of the filter material at the filtering wind speed of 0.5-3 m/min by a pressure difference sensor, wherein the pressure difference range is 300-2500 pa; under the condition of unchanged air volume, adding 50g of dry powder into the flue gas in batches, and measuring the pressure difference of an air inlet and an air outlet of a dust remover through a pressure difference sensor, wherein the pressure difference range is 500-;
under the thermal state condition, adding 50g of dry powder into the flue gas in batches, starting an induced draft fan, and enabling the flue gas containing the dry powder to sequentially flow through a heater, a dry reactor, a filter material of a dust remover and the induced draft fan and be heated by the heater; in each process temperature interval, the differential pressure of the air inlet and the air outlet of the dust remover is measured by a differential pressure sensor, and the differential pressure range is 500-.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention can adjust different process temperature intervals due to the heater, so as to meet the simulation requirements of integrated removal of pollutants such as deacidification, denitration, dioxin removal and the like under different process temperature intervals, explore the removal efficiency of the pollutants in different temperature intervals, and ensure that the simulation environment is consistent with the actual purification treatment process, thereby ensuring that the evaluation result is more accurate and having higher reference significance.
2. The invention is provided with the replaceable filter material, the volume of the filter material is consistent with the actual purification treatment process, the integrated removal efficiency of different filter material materials to pollutants such as deacidification, denitration and dioxin removal in the corresponding process temperature interval can be truly simulated, and the filter material is used for accurately evaluating the flue gas purification effect of the filter material so as to meet the test evaluation requirements of new materials.
3. According to the invention, different pollutants can be added, and corresponding chemical reducing agents are added according to different pollutants, so that the flue gas conditions under different working conditions can be simulated according to the flue gas characteristics of different industries, a flue gas purification simulation test and a multi-pollutant system purification simulation test under various conditions are realized, comprehensive detection evaluation close to the actual working conditions is obtained, and support is provided for the industrial application of the chemical reducing agents.
The invention can simulate the flue gas purification treatment conditions under different working conditions by controlling and adjusting the process flows of temperature intervals, filtering materials, medicament addition and the like, and realize tests under various conditions, thereby evaluating the actual purification effects of different materials on pollutants such as dust removal, deacidification, denitration, dioxin removal and the like, being suitable for the working conditions such as cold state, hot state and the like, and having simple structure, easy operation and low cost.
Drawings
FIG. 1 is a front view of the multi-functional flue gas purification evaluation device of the present invention.
In the figure, 1 a heater, 2 a dry reactor, 3 a dust remover, 4 filter materials, 5 an induced draft fan, 6 a first pollutant generator, 7 a second pollutant generator, 8 a deacidification agent supplier, 9 a denitration reducing agent supplier, 101 a first inlet flue gas detector, 102 a second inlet flue gas detector, 11 an outlet flue gas detector and 12 a differential pressure sensor.
Detailed Description
The invention is further described with reference to the following figures and specific examples.
Referring to fig. 1, a multifunctional flue gas purification evaluation device comprises a heater 1, a dry reactor 2, a dust remover 3, a filter material 4, an induced draft fan 5, a pollutant generator component, a chemical agent supplier component, a first inlet flue gas detector 101, a second inlet flue gas detector 102, an outlet flue gas detector 11 and a differential pressure sensor 12; the input end of the heater 1 is a flue gas supply pipeline, the output end of the pollutant generator component is connected to the input end of the heater 1, and the output end of the heater 1 is connected with the input end of the dry reactor 2; the output end of the dry method reactor 2 is connected with the air inlet of the dust remover 3, at least one filter material 4 is arranged in the dust remover 3, the filter material 4 is positioned between the air inlet of the dust remover 3 and the air purifying chamber, and the air outlet of the air purifying chamber of the dust remover 3 is connected with the induced draft fan 5; the chemical agent supply assembly is respectively connected with the dry reactor 2 and the dust remover 3, the first inlet flue gas detector 101 is arranged at the upstream of the air inlet of the dry reactor 2, the second inlet flue gas detector 102 is arranged at the upstream of the air inlet of the dust remover 3, and the outlet flue gas detector 11 is arranged at the downstream of the air outlet of the air purifying chamber of the dust remover 3; the differential pressure sensor 12 is installed on the air inlet flue and the air outlet flue of the dust remover 3.
The chemical agent supply assembly comprises a deacidification absorbent supply device 8 and a denitration reducing agent supply device 9; a deacidification absorbent supplier 8 is connected to the dry reactor 2, and a denitration reducing agent supplier 9 is connected to an upstream pipeline of an air inlet of the dust remover 3. The deacidification absorbent supplier 8 is used for supplying the dry deacidification absorbent powder to the dry reactor 2 so as to meet the reactions of desulfurization, deacidification and the like. The denitration reducing agent supplier 9 is used for spraying denitration reducing agents such as ammonia water and the like on the flue gas before entering the dust remover 3 so as to meet the removal reaction of the filter material 4 in the dust remover 3 on various pollutants.
The filter material 4 is coated with a catalyst, the filter material 4 can adopt a catalyst ceramic tube or a catalyst cloth bag, and the number of the filter materials 4 is 1-8. The diameter of the filter material 4 is 50-200mm, preferably 150 mm; the length of the filter material 4 is 0.5-6m, preferably 3 m. The type of the catalyst can be selected according to the actual process treatment requirement, so that the pollutants can be subjected to deacidification, dust removal and denitration integration under the action of the catalyst.
Preferably, the pollutant generator assembly comprises a plurality of pollutant generators, such as a first pollutant generator 6 and a second pollutant generator 7, and the output ends of the first pollutant generator 6 and the second pollutant generator 7 are connected to the input end of the heater 1. The number of the pollutant generators can be adjusted according to the type of pollutants in the actual evaluation requirement, and the pollutant generators are used for providing SO with a certain concentration2、NOxHCl, dioxin, and the like.
A multifunctional flue gas purification evaluation method is based on the multifunctional flue gas purification evaluation device to realize the evaluation of the purification effect of the flue gas containing pollutants; the multifunctional flue gas purification evaluation method comprises the following steps: supplying pollutants through a pollutant generator assembly, enabling the pollutants to enter the heater 1 along with the smoke, and starting the induced draft fan 5 to enable the smoke containing the pollutants to sequentially flow through the heater 1, the dry-process reactor 2, the filter material 4 of the dust remover 3 and the induced draft fan 5; when acidic contaminants are included in the contaminants, the chemical supply assembly feeds the deacidified absorbent dry powder into the dry reactor 2. Whether the dry reactor 2 is started can be determined according to whether the flue gas contains acidic pollutants; when the dry reactor 2 is started, acid pollutants in the flue gas are subjected to acid-base neutralization reaction in the dry reactor 2, and when the dry reactor 2 is not started, the flue gas only flows through the dry reactor 2. When the pollutants include nitrogen oxides, the chemical agent supplier component sprays denitration reducing agents into the flue gas before entering the dust remover 3. Whether the heater 1 is started or not can be determined according to the evaluation conditions of a cold state and a hot state, when the evaluation is carried out under the cold state condition, the heater 1 is not started, the flue gas only flows through the heater 1, when the evaluation is carried out under the hot state condition, the heater 1 is started, and the flue gas is heated to a process temperature interval required by the evaluation through the heater 1 when flowing through the heater 1.
When the filter material 4 is a catalyst ceramic tube, the process temperature interval of the catalyst ceramic tube comprises: at the temperature of 150 ℃ at 120-; when the filter material 4 is a catalytic cloth bag, the process temperature interval of the catalytic cloth bag comprises: at a temperature of between 120 ℃ and 150 ℃, at a temperature of between 150 ℃ and 180 ℃ and at a temperature of between 180 ℃ and 220 ℃.
The range of the air quantity of the induced draft fan 5 is 50-3000m3And/h, negative pressure is provided to control the flow direction and flow speed of the flue gas, and the air volume range of the induced draft fan 5 can be adjusted according to actual evaluation requirements.
When the desulfurization and dust removal efficiency is evaluated by adopting the multifunctional flue gas purification evaluation method, SO is supplied by the pollutant generator componentxAnd enters the heater 1 along with the flue gas, and the draught fan 5 is started to lead the SO contained in the flue gas to bexThe flue gas flows through a heater 1, a dry-method reactor 2, a filter material 4 of a dust remover 3 and a draught fan 5 in sequence; adding deacidified absorbent dry powder into the dry reactor 2 through a deacidified absorbent feeder 8 of the chemical agent feeder component; SO detected by the first inlet flue gas detector 101xConcentration C of1Not more than 2000mg/m3The second inlet flue gas detector 102 detects the obtained dust concentration as F1(ii) a SO detected by the outlet flue gas detector 11xIs C in a concentration of2(ii) a The dust concentration detected by the outlet flue gas detector 11 is F2. Efficiency of desulfurization etaAThe calculation formula of (2) is as follows: etaA=(C1-C2)/C1100% and dust purification efficiency etaBThe calculation formula of (2) is as follows: etaB=(F1-F2)/F1*100%。
The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency hydrated lime powder and slaked lime powder. The main component of the high-efficiency hydrated lime powder is calcium hydroxide, and compared with hydrated lime, the high-efficiency hydrated lime powder has the characteristics of higher purity, larger specific surface area and larger pore volume, the purity of the high-efficiency hydrated lime powder is more than 95 percent, and the specific surface area of the high-efficiency hydrated lime powder is more than 50m2Perg, pore volume of high-efficiency hydrated lime powder is more than 0.3cm3(ii)/g; xiaoxiao (medicine for eliminating cough and asthma)The purity of the lime is about 85 percent, and the specific surface area of the slaked lime is less than 15m2(g) the pore volume of the slaked lime is less than 0.1cm3(ii) in terms of/g. Preferably, the sodium bicarbonate powder is mixed with SOxIn a molar ratio of 0.5-2, high-efficiency slaked lime powder and SOxIn a molar ratio of 0.8-3, slaked lime powder and SOxIn the range of 1 to 5.
When the filter material 4 is a catalyst ceramic tube and the filtering air speed is 0.5-2.0m/min, the dust purification efficiency of the filter material 4 is more than 99.93% for each process temperature interval. Wherein, when the filtering wind speed is 0.5m/min, the dust purification efficiency of the filter material 4 is more than 99.99 percent; when the filtering wind speed is 1 m/min, the dust purification efficiency of the filter material 4 is more than 99.96 percent; when the filtering wind speed is 1.5 m/min, the dust purification efficiency of the filter material 4 is more than 99.95 percent; when the filtering wind speed is 2 m/min, the dust purification efficiency of the filter material 4 is more than 99.93 percent.
When the filter material 4 is a catalytic cloth bag and the filtering air speed is 0.5-2.0m/min, the dust purification efficiency of the filter material 4 is more than 99.94% for each process temperature interval. Wherein, when the filtering wind speed is 0.5m/min, the dust purification efficiency of the filter material 4 is more than 99.99 percent; when the filtering wind speed is 1 m/min, the dust purification efficiency of the filter material 4 is more than 99.97 percent; when the filtering wind speed is 1.5 m/min, the dust purification efficiency of the filter material 4 is more than 99.96 percent; when the filtering wind speed is 2 m/min, the dust purification efficiency of the filter material 4 is more than 99.94 percent.
Under the condition that the filtering wind speed of the filter material 4 and the retention time of the flue gas in the dry-method reactor 2 are unchanged:
when the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is sodium bicarbonate powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 120 ℃ plus 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-95% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-99% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-99% in the process temperature range of 350-400 ℃.
Wherein, sodium bicarbonate powder and SO are mixedxWhen the molar ratio of (A) to (B) is in the range of 0.5, the molar ratio of (B) to (C) is within the range ofThe process temperature range is 120-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-40% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% in the process temperature range of 350-400 ℃.
When sodium bicarbonate powder is mixed with SOxWhen the molar ratio is 1, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-60% for the process temperature range of 120-150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 80-90% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 85-98% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 85-98% in the process temperature range of 350-400 ℃.
When sodium bicarbonate powder is mixed with SOxWhen the molar ratio is 2, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 60-70% for the process temperature range of 120-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 85-95% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 90-99% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 90-99% in the process temperature range of 350-400 ℃.
When the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is high-efficiency hydrated lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-60% for the process temperature range of 120 ℃ and 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-90% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-99% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-95% in the process temperature range of 350-400 ℃.
Wherein the high-efficiency slaked lime powder is mixed with SOxWhen the molar ratio is in the range of 0.8, the process temperature range is 120 ℃ plus 150 ℃, and the multifunctional flue gas purification evaluation deviceThe desulfurization efficiency is 20-30%; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% for the process temperature range of 180 ℃ and 220 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-60% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional smoke purification evaluation device is 50-60% in the process temperature range of 350-400 ℃.
When the hydrated lime powder is efficiently mixed with SOxWhen the molar ratio is 2, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% for the process temperature range of 120-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 70-80% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 80-98% in the process temperature range of 250 ℃ and 300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 75-95% in the process temperature range of 350-400 ℃.
When the hydrated lime powder is efficiently mixed with SOxWhen the molar ratio is 3, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 50-60% for the process temperature range of 120-150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 80-90% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 90-99% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 80-95% in the process temperature range of 350-400 ℃.
When the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is slaked lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 120 ℃ plus 150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-50% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 15-50% in the process temperature range of 350-400 ℃.
Wherein, when slaked lime powder is mixed with SOxWhen the molar ratio is 1, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-30% for the process temperature range of 120-; for the process temperature interval 180-22The desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-30% at 0 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-25% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 15-25% in the process temperature range of 350-400 ℃.
When slaked lime powder and SOxWhen the molar ratio is 3, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-50% for the process temperature range of 120-150 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-50% for the process temperature range of 180 ℃ and 220 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 30-40% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-30% in the process temperature range of 350-400 ℃.
When slaked lime powder and SOxWhen the molar ratio is 5, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 60-70% for the process temperature range of 120-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 60-70% for the process temperature range of 180-; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% in the process temperature range of 250-300 ℃; the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 40-50% in the process temperature range of 350-400 ℃.
When the HCl removal efficiency is evaluated by adopting a multifunctional flue gas purification evaluation method, HCl is supplied by a pollutant generator assembly and enters a heater 1 along with the flue gas, and an induced draft fan 5 is started, so that the flue gas containing the HCl sequentially flows through the heater 1, a dry-method reactor 2, a filter material 4 of a dust remover 3 and the induced draft fan 5; adding deacidified absorbent dry powder into the dry reactor 2 through a deacidified absorbent feeder 8 of the chemical agent feeder component; the first inlet flue gas detector 101 detects the resulting concentration D of HCl1Not more than 20000mg/m3And the concentration of HCl detected by the outlet flue gas detector 11 is D2. HCl removal efficiency etaDThe calculation formula of (2) is as follows: etaD=(D1-D2)/D1*100%。
The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency hydrated lime powder and slaked lime powder. Preferably, the molar ratio of the sodium bicarbonate powder to the HCl ranges from 0.5 to 1.5, the molar ratio of the high-efficiency slaked lime powder to the HCl ranges from 0.6 to 2, and the molar ratio of the slaked lime powder to the HCl ranges from 1 to 3.
Under the condition that the filtering wind speed of the filter material 4 and the retention time of the flue gas in the dry-method reactor 2 are unchanged:
when the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is sodium bicarbonate powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-96% for the process temperature range of 120 ℃ plus 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%.
Wherein, when the molar ratio of the sodium bicarbonate powder to the HCl is 0.5, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-40% for the process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-50%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%.
When the molar ratio of the sodium bicarbonate powder to the HCl is 1, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-95% for a process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%.
When the molar ratio of the sodium bicarbonate powder to the HCl is in the range of 1.5, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 88-96% for the process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%.
When the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is high-efficiency hydrated lime powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-85% for the process temperature range of 120 ℃ plus 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%.
Wherein, when the molar ratio range of the high-efficiency hydrated lime powder to the HCl is 0.6, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-50% for the process temperature range of 120-; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%.
When the molar ratio of the high-efficiency hydrated lime powder to the HCl is within 1.5, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 60-80% for the process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 85-99%.
When the molar ratio of the high-efficiency hydrated lime powder to the HCl is within 2, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 70-85% for the process temperature range of 120-; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 90-99%.
When the filter material 4 is a catalyst ceramic tube and the deacidification absorbent dry powder is slaked lime powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-70% for the process temperature range of 120 ℃ plus 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 35-70%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-60%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-50%.
Wherein, when the molar ratio of the slaked lime powder to the HCl is 1, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-40% for the process temperature range of 120 ℃ and 150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 35-45%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-30%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 20-30%.
When the molar ratio of the slaked lime powder to the HCl is within 2 percent, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60 percent for the process temperature range of 120-150 ℃; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-50%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-40%.
When the molar ratio of the slaked lime powder to the HCl is within 3, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 60-70% for the process temperature range of 120-; for the process temperature range of 180 ℃ and 220 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 60-70%; for the process temperature range of 250 ℃ and 300 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-60%; for the process temperature range of 350 ℃ and 400 ℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 40-50%.
Method for evaluating NO by adopting multifunctional flue gas purification evaluation methodxFor efficiency of removal, NO is supplied through pollutant generator assemblyxAnd enters the heater 1 along with the flue gas, and the induced draft fan 5 is started to lead NO to be containedxThe flue gas flows through a heater 1, a dry-method reactor 2, a filter material 4 of a dust remover 3 and a draught fan 5 in sequence, and the dry-method reactor 2 is not started; spraying a denitration reducing agent into the flue gas before entering the dust remover 3 through a denitration reducing agent supplier 9 of the chemical agent supplier assembly, wherein the denitration reducing agent is preferably ammonia water, so that the molar ratio of ammonia nitrogen in the flue gas is in the range of 0.5-3; NO detected by the first inlet flue gas detector 101xConcentration E of1Not more than 800mg/m3NO detected by the outlet flue gas detector 11xAt a concentration of E2。NOxRemoval efficiency etaEThe calculation formula of (2) is as follows: etaE=(E1-E2)/E1*100%。
Under the condition that the filtering wind speed of the filter material 4 is unchanged:
when the filter material 4 is a catalyst ceramic tube, the NO of the multifunctional flue gas purification evaluation device is increased by 150 ℃ for the process temperature range of 120-xThe removal efficiency is 10-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 30-95%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 250 ℃ and 300 DEG CxThe removal efficiency is 50-98%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 350 ℃ and 400 DEG CxThe removal efficiency is 55-98%.
Wherein, when the ammonia nitrogen molar ratio in the flue gas is 0.5, the NO of the multifunctional flue gas purification evaluation device is 150 ℃ for the process temperature range of 120-xThe removal efficiency is 10-20%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 30-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 250 ℃ and 300 DEG CxThe removal efficiency is50-60 percent; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 350 ℃ and 400 DEG CxThe removal efficiency is 55-70%.
When the ammonia nitrogen molar ratio in the flue gas is 1, the NO of the multifunctional flue gas purification evaluation device is determined for the process temperature range of 120 ℃ plus 150 DEG CxThe removal efficiency is 20-30%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 75-90%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 250 ℃ and 300 DEG CxThe removal efficiency is 85-95%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 350 ℃ and 400 DEG CxThe removal efficiency is 85-98%.
When the ammonia nitrogen molar ratio in the flue gas is 3, the NO of the multifunctional flue gas purification evaluation device is determined for the process temperature range of 120 ℃ plus 150 DEG CxThe removal efficiency is 30-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 85-95%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 250 ℃ and 300 DEG CxThe removal efficiency is 90-98%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 350 ℃ and 400 DEG CxThe removal efficiency is 90-98%.
When the filter material 4 is a catalytic cloth bag, the temperature of the process temperature range is 120 ℃ plus 150 ℃, and the NO of the multifunctional flue gas purification evaluation devicexThe removal efficiency is 10-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 150 ℃ and 180 DEG CxThe removal efficiency is 30-80%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 40-95%.
Wherein, when the ammonia nitrogen molar ratio in the flue gas is 0.5, the NO of the multifunctional flue gas purification evaluation device is 150 ℃ for the process temperature range of 120-xThe removal efficiency is 10-20%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 150 ℃ and 180 DEG CxThe removal efficiency is 30-50%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 40-60%.
When the ammonia nitrogen molar ratio in the flue gas is 1, the ammonia nitrogen molar ratio is adjusted to the working conditionNO of multifunctional flue gas purification evaluation device within the process temperature range of 120 ℃ and 150 DEG CxThe removal efficiency is 20-30%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 150 ℃ and 180 DEG CxThe removal efficiency is 40-70%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 80-90%.
When the ammonia nitrogen molar ratio in the flue gas is 3, the NO of the multifunctional flue gas purification evaluation device is determined for the process temperature range of 120 ℃ plus 150 DEG CxThe removal efficiency is 30-40%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 150 ℃ and 180 DEG CxThe removal efficiency is 60-80%; NO of the multifunctional flue gas purification evaluation device for the process temperature range of 180 ℃ and 220 DEG CxThe removal efficiency is 85-95%.
When the dioxin removal efficiency is evaluated by adopting a multifunctional flue gas purification evaluation method, dioxin is supplied by a pollutant generator assembly and enters a heater 1 along with flue gas for heating, an induced draft fan 5 is started, so that the flue gas containing the dioxin flows through the heater 1, a dry method reactor 2, a filter material 4 of a dust remover 3 and the induced draft fan 5 in sequence, and the dry method reactor 2 is not started; the concentration H of dioxin detected by the first inlet flue gas detector 1011Not more than 100ngTEQ/Nm3The concentration of dioxin detected by the outlet flue gas detector 11 is H2. Efficiency η of dioxin removalHThe calculation formula of (2) is as follows: etaH=(H1-H2)/H1*100%。
Under the condition that the filtering wind speed of the filter material 4 is unchanged:
when the filter material 4 is a catalytic ceramic tube, the removal efficiency of dioxin in the filter material 4 is 60-70% for the process temperature interval of 120-150 ℃, wherein the decomposition efficiency of gaseous dioxin is 65%; for the process temperature range of 180 ℃ and 220 ℃, the dioxin removal efficiency of the filter material 4 is 70-80%, wherein the decomposition efficiency of gaseous dioxin is 75%; for the process temperature range of 250 ℃ and 300 ℃, the dioxin removal efficiency of the filter material 4 is 85-95%, wherein the decomposition efficiency of gaseous dioxin is 85%; for the process temperature range of 350 ℃ and 400 ℃, the dioxin removal efficiency of the filter material 4 is 85-99.6%, wherein the decomposition efficiency of gaseous dioxin is 90%.
When the filter material 4 is a catalytic cloth bag, the dioxin removal efficiency of the filter material 4 is 50-60% for the process temperature interval of 120-150 ℃; for the process temperature range of 150 ℃ and 180 ℃, the dioxin removal efficiency of the filter material 4 is 60-70%; the removal efficiency of dioxin in the filter material 4 is 70-80% for the process temperature range of 180-220 ℃.
Method for evaluating NO by adopting multifunctional flue gas purification evaluation methodxIn the case of influence on efficiency of dioxin removal, NO is supplied through pollutant generator modulexAnd dioxin enter the heater 1 along with the flue gas for heating, and the draught fan 5 is started to lead the NO to be containedxAnd the flue gas of the dioxin sequentially flow through a heater 1, a dry reactor 2, a filter material 4 of a dust remover 3 and a draught fan 5, and the dry reactor 2 is not started; spraying a denitration reducing agent into the flue gas before entering the dust remover 3 through a denitration reducing agent supplier 9 of the chemical agent supplier assembly, wherein the denitration reducing agent is preferably ammonia water, so that the molar ratio range of ammonia nitrogen in the flue gas is 1; under the working condition that the ammonia nitrogen molar ratio in the flue gas is not changed, the concentration J of the dioxin detected by the first inlet flue gas detector 1011Is 5-10ngTEQ/Nm3NO detected by the first inlet flue gas detector 101xConcentration J3Is 400-1200mg/m3And the concentration of dioxin detected by the outlet flue gas detector 11 is J2. Efficiency η of dioxin removalJThe calculation formula of (2) is as follows: etaJ=(J1-J2)/J1*100%。
The filter material 4 affects mutually in the processes of decomposing the dioxin and denitrating, when the filter material 4 is a catalyst ceramic tube, the dioxin removal efficiency is 40-55% for each process temperature interval of 120 ℃ plus one material at 150 ℃; for each process temperature range of 180 ℃ and 220 ℃, the dioxin removal efficiency is 50-65%; for each process temperature range of 250 ℃ and 300 ℃, the dioxin removal efficiency is 60-85 percent; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 70-89%. .
Wherein, for the process temperature range of 120 ℃ and 150 ℃, when NO is usedxConcentration J of3Is 400mg/m3The dioxin removal efficiency is 55 percent; when NO is presentxConcentration J of3Is 800mg/m3The dioxin removal efficiency is 50 percent; when in useNOxConcentration J of3Is 1200mg/m3The dioxin removal efficiency was 40%.
For the process temperature range of 180 ℃ and 220 ℃, when NO is generatedxConcentration J of3Is 400mg/m3The dioxin removal efficiency is 65%; when NO is presentxConcentration J of3Is 800mg/m3The dioxin removal efficiency is 60 percent; when NO is presentxConcentration J of3Is 1200mg/m3The dioxin removal efficiency was 50%.
At a process temperature range of 250 ℃ and 300 ℃, when NO is generatedxConcentration J of3Is 400mg/m3The dioxin removal efficiency is 85 percent; when NO is presentxConcentration J of3Is 800mg/m3The dioxin removal efficiency is 70 percent; when NO is presentxConcentration J of3Is 1200mg/m3The dioxin removal efficiency was 60%.
For the process temperature range of 350 ℃ and 400 ℃, when NO is generatedxConcentration J of3Is 400mg/m3The dioxin removal efficiency is 89%; when NO is presentxConcentration J of3Is 800mg/m3The dioxin removal efficiency is 80 percent; when NO is presentxConcentration J of3Is 1200mg/m3The dioxin removal efficiency was 70%.
When a multifunctional flue gas purification evaluation method is adopted to evaluate the influence of HCl on the dioxin removal efficiency, HCl and dioxin are supplied by a pollutant generator component and enter a heater 1 along with flue gas for heating, and an induced draft fan 5 is started to enable the flue gas containing HCl and dioxin to sequentially flow through the heater 1, a dry method reactor 2, a filter material 4 of a dust remover 3 and the induced draft fan 5; adding deacidified absorbent dry powder into the dry reactor 2 through a deacidified absorbent feeder 8 of the chemical agent feeder component; concentration L of dioxin detected by first inlet flue gas detector 1011Is 5-10ngTEQ/Nm3The concentration L of HCl detected by the first inlet flue gas detector 1013Is 500-12000mg/m3The concentration of dioxin detected by the outlet flue gas detector 11 is L2. Efficiency η of dioxin removalLThe calculation formula of (2) is as follows: etaL=(L1-L2)/L1*100%。
The filter material 4 is mutually influenced in the processes of decomposing dioxin and deacidifying, the filter material 4 is a catalyst ceramic tube, and when the dry powder of the deacidification absorbent is slaked lime powder, the molar ratio of the slaked lime powder to HCl is 1; when the dry powder of the deacidification absorbent is sodium bicarbonate powder, the molar ratio of the sodium bicarbonate powder to the HCl is 1, and when the dry powder of the deacidification absorbent is high-efficiency hydrated lime powder, the molar ratio of the high-efficiency hydrated lime powder to the HCl is 1.5. The removal efficiency of the dioxin is 20-40% in the process temperature range of 120 ℃ plus 150 ℃; the removal efficiency of the dioxin is 20-60% for the process temperature range of 180 ℃ and 220 ℃; the process temperature range is 250 ℃ and 300 ℃, and the dioxin removal efficiency is 20-80%; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 30-90%.
Wherein, for the process temperature range of 120 ℃ and 150 ℃, when the concentration L of HCl is higher than that of the HCl3Is 500mg/m3The dioxin removal efficiency is 50 percent; when the concentration of HCl L is3Is 2000mg/m3The dioxin removal efficiency is 40 percent; when the concentration of HCl L is3Is 5000 mg/m3The dioxin removal efficiency is 30 percent; when the concentration of HCl L is3Is 12000mg/m3The dioxin removal efficiency was 20%.
At a process temperature range of 180 ℃ and 220 ℃, when the concentration L of HCl is higher than that of HCl3Is 500mg/m3The dioxin removal efficiency is 60 percent; when the concentration of HCl L is3Is 2000mg/m3The dioxin removal efficiency is 50 percent; when the concentration of HCl L is3Is 5000 mg/m3The dioxin removal efficiency is 40 percent; when the concentration of HCl L is3Is 12000mg/m3The dioxin removal efficiency was 20%.
At a process temperature range of 250 ℃ and 300 ℃, when the concentration L of HCl is higher than that of the3Is 500mg/m3The dioxin removal efficiency is 80 percent; when the concentration of HCl L is3Is 2000mg/m3The dioxin removal efficiency is 60 percent; when the concentration of HCl L is3Is 5000 mg/m3The dioxin removal efficiency is 30 percent; when the concentration of HCl L is3Is 12000mg/m3The dioxin removal efficiency was 20%.
For the process temperature range of 350 ℃ and 400 ℃, when the HCl is adoptedConcentration L3Is 500mg/m3The dioxin removal efficiency is 90 percent; when the concentration of HCl L is3Is 2000mg/m3The dioxin removal efficiency is 80 percent; when the concentration of HCl L is3Is 5000 mg/m3The dioxin removal efficiency is 50 percent; when the concentration of HCl L is3Is 12000mg/m3The dioxin removal efficiency was 30%.
SO evaluation by adopting the multifunctional flue gas purification evaluation methodxIn the case of influence on efficiency of dioxin removal, SO is supplied from a pollutant generator modulexAnd dioxin enter the heater 1 along with the flue gas to be heated, and the draught fan 5 is started to lead the SO to be containedxAnd the flue gas of the dioxin sequentially flow through a heater 1, a dry method reactor 2, a filter material 4 of a dust remover 3 and a draught fan 5; adding deacidified absorbent dry powder into the dry reactor 2 through a desulphurization absorbent feeder 8 of the chemical agent feeder assembly; the concentration S of dioxin detected by the first inlet flue gas detector 1011Is 5-10ngTEQ/Nm3The SO detected by the first inlet flue gas detector 101xConcentration Y of1200-2000mg/m3The concentration of dioxin detected by the outlet flue gas detector 11 is S2. Efficiency η of dioxin removalsThe calculation formula of (2) is as follows: etas=(S1-S2)/S1*100%。
The filter material 4 is mutually influenced in the processes of decomposing dioxin and desulfurizing, the filter material 4 is a catalyst ceramic tube, and when the desulfurizing absorbent dry powder is high-efficiency hydrated lime powder, the high-efficiency hydrated lime powder and SOxIs 2, when the dry powder of the desulfurization absorbent is sodium bicarbonate, the sodium bicarbonate is mixed with SOxIs 1.5, when the dry powder of the desulphurization absorbent is slaked lime powder, the slaked lime powder and SOxIs 3.
The removal efficiency of dioxin is 10-30% in the process temperature range of 120 ℃ plus 150 ℃; the process temperature range is 180 ℃ and 220 ℃, and the dioxin removal efficiency is 20-50%; the process temperature range is 250 ℃ and 300 ℃, and the dioxin removal efficiency is 30-70%; the process temperature range is 350 ℃ and 400 ℃, and the dioxin removal efficiency is 40-80%.
Wherein, forThe process temperature range is 120 ℃ and 150 ℃ when SO is generatedxConcentration Y of1Is 200mg/m3The dioxin removal efficiency is 30 percent; when SOxConcentration Y of1Is 1000mg/m3The dioxin removal efficiency is 20 percent; when SOxConcentration Y of1Is 2000mg/m3The dioxin removal efficiency was 10%.
For the process temperature range of 180 ℃ and 220 ℃, when the concentration Y of SOx is equal to1Is 200mg/m3The dioxin removal efficiency is 50 percent; when SOxConcentration Y of1Is 1000mg/m3The dioxin removal efficiency is 40 percent; when SOxConcentration Y of1Is 2000mg/m3The dioxin removal efficiency was 20%.
At a process temperature range of 250 ℃ and 300 ℃, when SO is appliedxConcentration Y of1Is 200mg/m3The dioxin removal efficiency is 70 percent; when SOxConcentration Y of1Is 1000mg/m3The dioxin removal efficiency is 50 percent; when SOxConcentration Y of1Is 2000mg/m3The dioxin removal efficiency was 30%.
At a process temperature range of 350 ℃ and 400 ℃, when SO is appliedxConcentration Y of1Is 200mg/m3The dioxin removal efficiency is 80 percent; when SOxConcentration Y of1Is 1000mg/m3The dioxin removal efficiency is 60 percent; when being SOxConcentration Y of1Is 2000mg/m3The dioxin removal efficiency was 40%.
The method for evaluating the pressure difference of different filter materials 4 under the cold condition comprises the following steps: a pressure difference sensor 12 is arranged on a gas inlet flue and a gas outlet flue of a dust remover 3 through communicating pipelines and is used for detecting the gas pressure difference in the gas inlet flue and the gas outlet flue of the dust remover 3, a filter material 4 is arranged in the dust remover 3, an induced draft fan 5 is started, a heater 1, a dry method reactor 2, the filter material 4 of the dust remover 3 and the induced draft fan 5 are started, and the heater 1 is not started; under the condition that the air volume is unchanged, namely the filtering air speed is unchanged (the filtering air speed is preferably 1.0 m/min), the differential pressure is measured by the differential pressure sensor 12, and the differential pressure range of different filtering materials 4 is 300-1200 Pa.
The method for evaluating the pressure difference of the filter material 4 at different filter wind speeds under the cold condition comprises the following steps: a filter material 4 is arranged in the dust remover 3, an induced draft fan 5, a heater 1, the dry method reactor 2, the filter material 4 of the dust remover 3 and the induced draft fan 5 are started, and the heater 1 is not started; the air quantity of the draught fan 5 is changed, the pressure difference of the filter material 4 at the filtering air speed of 0.5-3 m/min is measured through the pressure difference sensor 12, and the pressure difference range is 300-2500 pa. Wherein the pressure difference range when the filtering wind speed is 0.5m/min is 300-800 pa; the pressure difference range when the filtering wind speed is 1.0m/min is 500-1200 Pa; the pressure difference range when the filtering wind speed is 1.5 m/min is 800-; the pressure difference range when the filtering wind speed is 2 m/min is 900-2000 pa; the pressure difference range when the filtering wind speed is 3 m/min is 1000-2500 Pa.
The method for evaluating the pressure difference of different dust loads under cold conditions (i.e. normal temperature conditions without heating) is as follows: a filter material 4 is arranged in the dust remover 3, an induced draft fan 5, a heater 1, the dry method reactor 2, the filter material 4 of the dust remover 3 and the induced draft fan 5 are started, and the heater 1 is not started; under the condition of constant air volume (preferably 1.0 m/min), 50g of dry powder is added into the flue gas in batches, the pressure difference of an air inlet and an air outlet of the dust remover 3 is measured by the pressure difference sensor 12, the pressure difference data changing along with the time and the dry powder adding amount is recorded, and the pressure difference range is 500-3500 pa. Wherein, the pressure difference range when the dry powder adding amount is 0g is 500-1200Pa, the pressure difference range when the dry powder adding amount is 2g is 700-1500Pa, the pressure difference range when the dry powder adding amount is 5g is 1000-2200Pa, the pressure difference range when the dry powder adding amount is 10g is 1200-2300Pa, the pressure difference range when the dry powder adding amount is 20g is 1500-2800Pa, and the pressure difference range when the dry powder adding amount is 50g is 1800-3500 Pa.
The method for evaluating the pressure difference of different dust loads under the thermal state condition comprises the following steps: a filter material 4 is arranged in the dust remover 3, 50g of dry powder is added into the flue gas in batches, an induced draft fan 5 is started, the flue gas containing the dry powder sequentially flows through a heater 1, a dry reactor 2, the filter material 4 of the dust remover 3 and the induced draft fan 5, and the flue gas is heated by the heater 1; under the condition of constant air volume (preferably 1.0 m/min), the differential pressure of the air inlet and the air outlet of the dust remover 3 is measured by the differential pressure sensor 12 in each process temperature interval, and the differential pressure data changing along with the time and the dry powder adding amount is recorded, wherein the differential pressure range is 500-3600 pa. Wherein, the pressure difference range when the dry powder adding amount is 0g is 500-1200Pa, the pressure difference range when the dry powder adding amount is 2g is 800-1600Pa, the pressure difference range when the dry powder adding amount is 5g is 1000-2300Pa, the pressure difference range when the dry powder adding amount is 10g is 1300-2400Pa, the pressure difference range when the dry powder adding amount is 20g is 1600-2900Pa, and the pressure difference range when the dry powder adding amount is 50g is 1900-3600 Pa.
The working principle of the multifunctional flue gas purification evaluation device is as follows:
a pollutant generator component is arranged in the front section flue of the heater 1 to ensure that SOx、NOxAfter being measured by a standard gas bottle, the pollutants are injected into a flue; a draught fan 5 provides negative pressure, smoke containing pollutants is led into a heater 1 and is heated to a set temperature through the heater 1, namely a process temperature interval of a filter material 4, the heated smoke is led into a dry-method reactor 2, acid removal absorbent dry powder is sprayed from the lower part of the dry-method reactor 2 by an acid removal absorbent dry powder supplier 8, the acid removal absorbent dry powder and acid substances flow in the same direction from bottom to top in the dry-method reactor 2 and simultaneously generate acid-base neutralization reaction to play a role in deacidification, the smoke and the acid removal absorbent dry powder are discharged from the top of the dry-method reactor 2 and enter a dust remover 3, the smoke enters from the bottom of the dust remover 3, the smoke enters from the outside of the filter material 4 when flowing from bottom to top and flows out from a central hole, and finally enters a gas purifying chamber at the top of the dust remover 3, dust is filtered and removed by the filter material 4, and NO is filtered by the filter material 4xThe catalyst is removed by reduction reaction in the presence of the catalyst. The dust remover 3 can use the compressed air pulse blowback to clear away the dust attached to the surface of the filter material 4, and the fly ash is concentrated at the bottom of the dust remover 3, thus being convenient for cleaning. In the flue before entering the dust remover 3, the denitration reducing agent ammonia water is sprayed in through the denitration reducing agent supplier 9, the ammonia water and the flue gas are fully mixed and then enter the dust remover 3, and the integration of deacidification, dust removal and denitration is realized through a catalyst ceramic filter tube or a catalytic cloth bag in a set process temperature interval. The first inlet flue gas detector 101 and the second inlet flue gas detector 102 may detect the original concentration of the pollutants; an outlet flue gas detector 11 is arranged in the rear section flue of the dust remover 3, and can detect the emission concentration of pollutants. The draught fan 5 discharges the purified flue gas through a chimney or purifies the purified flue gasAnd conveying the flue gas to a subsequent treatment process.
The multifunctional flue gas purification evaluation method can detect the differential pressure and the dust treatment efficiency of the catalytic ceramic filter tube or the catalytic cloth bag under the cold state and the hot state conditions.
The multifunctional flue gas purification evaluation method can carry out test detection in a process temperature range of 120-400 ℃ under a thermal state condition, respectively carry out detection and evaluation on the removal efficiency of the catalytic ceramic filter tube and the catalytic cloth bag in process temperature ranges of 120-plus-150 ℃, 180-plus-220 ℃, 250-plus-300 ℃ and 350-plus-400 ℃, and examine the removal efficiency of different deacidification agents at different temperatures by selecting sodium bicarbonate powder, high-efficiency hydrated lime and slaked lime as deacidification agents. Investigation of NO at different temperature intervalsxThereby comprehensively evaluating the catalytic ceramic filter tube and the catalytic cloth bag. Other forms of filter material 4 are also suitable.
The multifunctional flue gas purification evaluation method can detect the dioxin removal efficiency of the catalytic ceramic filter tube or the catalytic cloth bag under the thermal state condition, and the dioxin standard gas is added into the flue gas, and the flue gas before and after purification is respectively sampled by the first inlet flue gas detector 101 and the first outlet flue gas detector 11 and is analyzed in a laboratory, so that the dioxin removal efficiency of the filter material 4 is evaluated. Meanwhile, the flue gas temperature can be changed, and the dioxin removal efficiency can be evaluated in different process temperature intervals. Alternatively, NO can be injectedx、SOxAnd one pollutant in HCl changes the concentration of dioxin, the mechanism of the influence of each pollutant on the removal of the dioxin is explored, and the synergistic removal effect of each pollutant and the dioxin is evaluated.

Claims (10)

1.一种多功能烟气净化评价方法，其特征是：该多功能烟气净化评价方法基于多功能烟气净化评价装置实现；所述的多功能烟气净化评价装置包括加热器（1）、干法反应器（2）、除尘器（3）、滤料（4）、引风机（5）、污染物发生器组件和化学药剂供应器组件；加热器（1）的输入端烟气供应管道，污染物发生器组件的输出端连接至加热器（1）的输入端，加热器（1）的输出端与干法反应器（2）的输入端连接；干法反应器（2）的输出端与除尘器（3）的进气口连接，滤料（4）安装在除尘器（3）内，除尘器（3）的出气口与引风机（5）连接；化学药剂供应器组件分别与干法反应器（2）和除尘器（3）连接；1. A multifunctional flue gas purification evaluation method, characterized in that: the multifunctional flue gas purification evaluation method is realized based on a multifunctional flue gas purification evaluation device; the multifunctional flue gas purification evaluation device comprises a heater (1) , dry reactor (2), dust collector (3), filter material (4), induced draft fan (5), pollutant generator assembly and chemical agent supplier assembly; the input end of the heater (1) is supplied with flue gas Pipe, the output end of the pollutant generator assembly is connected to the input end of the heater (1), and the output end of the heater (1) is connected with the input end of the dry process reactor (2); The output end is connected with the air inlet of the dust collector (3), the filter material (4) is installed in the dust collector (3), and the air outlet of the dust collector (3) is connected with the induced draft fan (5); the chemical agent supply components are respectively Connected with the dry process reactor (2) and the dust collector (3); 所述的多功能烟气净化评价方法是：通过污染物发生器组件供应污染物并随烟气进入加热器（1）中，开启引风机（5），使含有污染物的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）；当污染物中包括酸性污染物时，化学药剂供应器组件向干法反应器（2）中投加脱酸吸收剂干粉；当污染物中包括氮氧化物时，化学药剂供应器组件向进入除尘器（3）前的烟气中喷洒脱硝还原剂。The multifunctional flue gas purification evaluation method is as follows: supplying pollutants through a pollutant generator component and entering the heater (1) with the flue gas, turning on the induced draft fan (5), and causing the flue gas containing pollutants to flow through in sequence. Heater (1), dry process reactor (2), filter material (4) and induced draft fan (5) of dust collector (3); when the pollutants include acidic pollutants, the chemical agent The deacidification absorbent dry powder is added into the reactor (2); when the pollutants include nitrogen oxides, the chemical agent supplier component sprays the denitration reducing agent into the flue gas before entering the dust collector (3). 2.根据权利要求1所述的多功能烟气净化评价方法，其特征是：所述的滤料（4）上涂覆有催化剂，滤料（4）的直径为50-200mm，长度为0.5-6m，滤料（4）为触媒陶瓷管或催化布袋；2. The multifunctional flue gas purification evaluation method according to claim 1, characterized in that: the filter material (4) is coated with a catalyst, the diameter of the filter material (4) is 50-200mm, and the length is 0.5 mm -6m, the filter material (4) is a catalyst ceramic tube or a catalyst cloth bag; 所述的滤料（4）为触媒陶瓷管时，触媒陶瓷管的工艺温度区间包括：120-150℃、180-220℃、250-300℃和350-400℃；滤料（4）为催化布袋时，催化布袋的工艺温度区间包括：120-150℃、150-180℃和180-220℃。When the filter material (4) is a catalyst ceramic tube, the process temperature range of the catalyst ceramic tube includes: 120-150°C, 180-220°C, 250-300°C and 350-400°C; the filter material (4) is a catalyst When bagging, the process temperature range of catalytic bagging includes: 120-150°C, 150-180°C and 180-220°C. 3.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价脱硫及除尘效率时，通过污染物发生器组件供应SOx并随烟气进入加热器（1）中，开启引风机（5），使含有的SOx烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）；化学药剂供应器组件向干法反应器（2）中投加脱酸吸收剂干粉；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101）并检测得到的SOx的浓度不超过2000mg/m3，在除尘器（3）进气口的上游设置第二入口烟气检测器（102）并检测得到的粉尘的浓度不超过60mg/m3；3. The multifunctional flue gas purification evaluation method according to claim 2, characterized in that: when evaluating desulfurization and dust removal efficiency, SO x is supplied through the pollutant generator assembly and enters the heater (1) with the flue gas, and is turned on. The induced draft fan (5) makes the SOx flue gas contained in it flow through the heater (1), the dry process reactor (2), the filter material (4) of the dust collector (3) and the induced draft fan (5) in turn; chemical agents The feeder assembly adds the deacidification absorbent dry powder into the dry process reactor (2); a first inlet flue gas detector (101) is arranged upstream of the air inlet of the dry process reactor (2) to detect the SO x obtained The concentration of dust does not exceed 2000mg/m 3 , a second inlet smoke detector (102) is set upstream of the air inlet of the dust collector (3), and the concentration of the detected dust does not exceed 60mg/m 3 ; 所述的脱酸吸收剂干粉为碳酸氢钠粉末、高效熟石灰粉末、消石灰粉末中的一种；其中，碳酸氢钠粉末与SOx的摩尔比范围为0.5-2，高效熟石灰粉末与SOx的摩尔比范围为0.8-3，消石灰粉末与SOx的摩尔比范围为1-5；The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency slaked lime powder, and slaked lime powder; wherein, the molar ratio range of sodium bicarbonate powder and SO x is 0.5-2, and the molar ratio of high-efficiency slaked lime powder and SO x is 0.5-2. The molar ratio range is 0.8-3, and the molar ratio range of slaked lime powder to SO x is 1-5; 当所述的滤料（4）为触媒陶瓷管且过滤风速为0.5-2.0m/min时，对于各工艺温度区间，滤料（4）的粉尘净化效率均大于99.93%；当滤料（4）为催化布袋且过滤风速为1.0m/min时，对于各工艺温度区间，滤料（4）的粉尘净化效率均大于99.94%；When the filter material (4) is a catalytic ceramic tube and the filtration wind speed is 0.5-2.0m/min, the dust purification efficiency of the filter material (4) is greater than 99.93% for each process temperature range; when the filter material (4) ) is a catalytic cloth bag and the filtration wind speed is 1.0m/min, for each process temperature range, the dust purification efficiency of the filter material (4) is greater than 99.94%; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为碳酸氢钠粉末时，对于工艺温度区间120-150℃，多功能烟气净化评价装置的脱硫效率为20-70%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的脱硫效率为30-95%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的脱硫效率为40-99%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的脱硫效率为40-99%；When the filter material (4) is a catalytic ceramic tube, and the dry powder of the deacidification absorbent is sodium bicarbonate powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for the process temperature range of 120-150°C. %; For the process temperature range of 180-220°C, the desulfurization efficiency of the multi-functional flue gas purification and evaluation device is 30-95%; for the process temperature range of 250-300°C, the desulfurization efficiency of the multi-functional flue gas purification and evaluation device is 40-99% %; For the process temperature range of 350-400℃, the desulfurization efficiency of the multi-functional flue gas purification evaluation device is 40-99%; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为高效熟石灰粉末时，对于工艺温度区间120-150℃，多功能烟气净化评价装置的脱硫效率为20-60%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的脱硫效率为40-90%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的脱硫效率为50-99%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的脱硫效率为50-95%；When the filter material (4) is a catalytic ceramic tube, and the deacidification absorbent dry powder is high-efficiency slaked lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-60% for the process temperature range of 120-150°C ; For the process temperature range of 180-220°C, the desulfurization efficiency of the multi-functional flue gas purification and evaluation device is 40-90%; for the process temperature range of 250-300°C, the desulfurization efficiency of the multi-functional flue gas purification and evaluation device is 50-99% ; For the process temperature range of 350-400 °C, the desulfurization efficiency of the multi-functional flue gas purification evaluation device is 50-95%; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为消石灰粉末时，对于工艺温度区间120-150℃，多功能烟气净化评价装置的脱硫效率为20-70%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的脱硫效率为20-70%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的脱硫效率为20-50%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的脱硫效率为15-50%。When the filter material (4) is a catalytic ceramic tube, and the dry powder of the deacidification absorbent is slaked lime powder, the desulfurization efficiency of the multifunctional flue gas purification evaluation device is 20-70% for a process temperature range of 120-150°C; For the process temperature range of 180-220 °C, the desulfurization efficiency of the multi-functional flue gas purification evaluation device is 20-70%; for the process temperature range of 250-300 °C, the desulfurization efficiency of the multi-functional flue gas purification evaluation device is 20-50%; For the process temperature range of 350-400 °C, the desulfurization efficiency of the multi-functional flue gas purification evaluation device is 15-50%. 4.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价HCl脱除效率时，通过污染物发生器组件供应HCl并随烟气进入加热器（1），开启引风机（5），使含有HCl的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）；化学药剂供应器组件向干法反应器（2）中投加脱酸吸收剂干粉；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101）并检测得到的HCl的浓度不超过20000mg/m3；4. The multifunctional flue gas purification evaluation method according to claim 2, characterized in that: when evaluating the HCl removal efficiency, HCl is supplied through the pollutant generator assembly and enters the heater (1) with the flue gas, and the induced draft fan is turned on. (5), so that the flue gas containing HCl flows through the heater (1), the dry process reactor (2), the filter material (4) of the dust collector (3) and the induced draft fan (5) in turn; the chemical agent supplier component Add the deacidification absorbent dry powder into the dry process reactor (2); set a first inlet flue gas detector (101) upstream of the air inlet of the dry process reactor (2), and the detected HCl concentration does not exceed 20000mg/m 3 ; 所述的脱酸吸收剂干粉为碳酸氢钠粉末、高效熟石灰粉末、消石灰粉末中的一种，其中，碳酸氢钠粉末与HCl的摩尔比范围为0.5-1.5，高效熟石灰粉末与HCl的摩尔比范围为0.6-2，消石灰粉末与HCl的摩尔比范围为1-3；The deacidification absorbent dry powder is one of sodium bicarbonate powder, high-efficiency slaked lime powder, and slaked lime powder, wherein the molar ratio of sodium bicarbonate powder to HCl ranges from 0.5 to 1.5, and the molar ratio of high-efficiency slaked lime powder to HCl is in the range of 0.5-1.5. The range is 0.6-2, and the molar ratio of slaked lime powder to HCl is in the range of 1-3; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为碳酸氢钠粉末，对于工艺温度区间120-150℃，多功能烟气净化评价装置的HCl脱除效率为30-96%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的HCl脱除效率为40-99%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的HCl脱除效率为50-99%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的HCl脱除效率为50-99%；When the filter material (4) is a catalyst ceramic tube, and the deacidification absorbent dry powder is sodium bicarbonate powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-150°C for the process temperature range of 120-150°C 96%; for the process temperature range of 180-220 °C, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 40-99%; for the process temperature range of 250-300 °C, the HCl removal efficiency of the multi-functional flue gas purification evaluation device The efficiency is 50-99%; for the process temperature range of 350-400 °C, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 50-99%; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为高效熟石灰粉末，对于工艺温度区间120-150℃，多功能烟气净化评价装置的HCl脱除效率为40-85%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的HCl脱除效率为50-99%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的HCl脱除效率为50-99%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的HCl脱除效率为50-99%；When the filter material (4) is a catalyst ceramic tube, and the dry powder of the deacidification absorbent is high-efficiency slaked lime powder, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 40-85 for a process temperature range of 120-150°C. %; For the process temperature range of 180-220℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 250-300℃, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 50-99%; for the process temperature range of 350-400 ℃, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 50-99%; 当所述的滤料（4）为触媒陶瓷管，且脱酸吸收剂干粉为消石灰粉末，对于工艺温度区间120-150℃，多功能烟气净化评价装置的HCl脱除效率为30-70%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的HCl脱除效率为35-70%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的HCl脱除效率为20-60%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的HCl脱除效率为20-50%。When the filter material (4) is a catalytic ceramic tube, and the dry powder of the deacidification absorbent is slaked lime powder, the HCl removal efficiency of the multifunctional flue gas purification evaluation device is 30-70% for a process temperature range of 120-150°C ; For the process temperature range of 180-220 °C, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 35-70%; for the process temperature range of 250-300 °C, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 20-60%; for the process temperature range of 350-400 ℃, the HCl removal efficiency of the multi-functional flue gas purification evaluation device is 20-50%. 5.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价NOx脱除效率时，通过污染物发生器组件供应NOx并随烟气进入加热器（1），开启引风机（5），使含有NOx的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5），干法反应器（2）不启用；化学药剂供应器组件向进入除尘器（3）前的烟气中喷洒脱硝还原剂氨水，使烟气中氨氮摩尔比范围为0.5-3；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101）并检测得到的NOx的浓度不超过800mg/m3；5. The multifunctional flue gas purification evaluation method according to claim 2, characterized in that: when evaluating the NOx removal efficiency, NOx is supplied through the pollutant generator assembly and enters the heater (1) with the flue gas, and is turned on The induced draft fan (5) makes the flue gas containing NOx flow through the heater (1), the dry process reactor (2), the filter material (4) and the induced draft fan (5) of the dust collector (3) in sequence, and the dry process The reactor (2) is not activated; the chemical agent supplier component sprays ammonia water, a denitrification reducing agent, into the flue gas before entering the dust collector (3), so that the molar ratio of ammonia to nitrogen in the flue gas is in the range of 0.5-3; 2) A first inlet smoke detector (101) is arranged upstream of the air inlet, and the detected NOx concentration does not exceed 800 mg/m 3 ; 当所述的滤料（4）为触媒陶瓷管，对于工艺温度区间120-150℃，多功能烟气净化评价装置的NOx脱除效率为10-40%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的NOx脱除效率为30-95%；对于工艺温度区间250-300℃，多功能烟气净化评价装置的NOx脱除效率为50-98%；对于工艺温度区间350-400℃，多功能烟气净化评价装置的NOx脱除效率为55-98%；When the filter material (4) is a catalytic ceramic tube, the NOx removal efficiency of the multifunctional flue gas purification evaluation device is 10-40% for the process temperature range of 120-150°C; for the process temperature range of 180-220°C , the NO x removal efficiency of the multi-functional flue gas purification evaluation device is 30-95%; for the process temperature range of 250-300 ℃, the NO x removal efficiency of the multi-functional flue gas purification evaluation device is 50-98%; The temperature range is 350-400℃, and the NOx removal efficiency of the multi-functional flue gas purification evaluation device is 55-98%; 当所述的滤料（4）为催化布袋，对于工艺温度区间120-150℃，多功能烟气净化评价装置的NOx脱除效率为10-40%；对于工艺温度区间150-180℃，多功能烟气净化评价装置的NOx脱除效率为30-80%；对于工艺温度区间180-220℃，多功能烟气净化评价装置的NOx脱除效率为40-95%。When the filter material (4) is a catalytic cloth bag, the NOx removal efficiency of the multi-functional flue gas purification evaluation device is 10-40% for a process temperature range of 120-150°C; for a process temperature range of 150-180°C, The NOx removal efficiency of the multifunctional flue gas purification evaluation device is 30-80%; for the process temperature range of 180-220 °C, the NOx removal efficiency of the multifunctional flue gas purification evaluation device is 40-95%. 6.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价二噁英脱除效率时，通过污染物发生器组件供应二噁英并随烟气进入加热器（1）加热，开启引风机（5），使含有二噁英的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5），干法反应器（2）不启用；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101），第一入口烟气检测器（101）取样并经实验室分析得到的二噁英的浓度不超过100ngTEQ/Nm3；6. The multifunctional flue gas purification evaluation method according to claim 2, characterized in that: when evaluating the dioxin removal efficiency, the dioxin is supplied through the pollutant generator assembly and enters the heater (1) with the flue gas Heating, turn on the induced draft fan (5), so that the flue gas containing dioxin flows through the heater (1), the dry process reactor (2), the filter material (4) and the induced draft fan (5) of the dust collector (3) in turn. ), the dry process reactor (2) is not activated; a first inlet flue gas detector (101) is set upstream of the air inlet of the dry process reactor (2), and the first inlet flue gas detector (101) takes samples and passes through the The concentration of dioxin obtained by laboratory analysis does not exceed 100ngTEQ/Nm 3 ; 当所述的滤料（4）为触媒陶瓷管时，对于工艺温度区间120-150℃，滤料（4）的二噁英脱除效率为60-70%，其中，气态二噁英的分解效率为65%；对于工艺温度区间180-220℃，滤料（4）的二噁英脱除效率为70-80%，其中，气态二噁英的分解效率为75%；对于工艺温度区间250-300℃，滤料（4）的二噁英脱除效率为85-95%，其中，气态二噁英的分解效率为85%；对于工艺温度区间350-400℃，滤料（4）的二噁英脱除效率为85-99.6%，其中，气态二噁英的分解效率为90%；When the filter material (4) is a catalyst ceramic tube, the dioxin removal efficiency of the filter material (4) is 60-70% for a process temperature range of 120-150°C, wherein the decomposition of gaseous dioxins The efficiency is 65%; for the process temperature range of 180-220°C, the dioxin removal efficiency of the filter material (4) is 70-80%, of which the decomposition efficiency of gaseous dioxins is 75%; for the process temperature range of 250 -300 °C, the dioxin removal efficiency of the filter material (4) is 85-95%, of which the decomposition efficiency of gaseous dioxins is 85%; for the process temperature range of 350-400 °C, the filter material (4) The removal efficiency of dioxin is 85-99.6%, of which the decomposition efficiency of gaseous dioxin is 90%; 当所述的滤料（4）为催化布袋，对于工艺温度区间120-150℃，滤料（4）的二噁英脱除效率为50-60%；对于工艺温度区间150-180℃，滤料（4）的二噁英脱除效率为60-70%；对于工艺温度区间180-220℃，滤料（4）的二噁英脱除效率为70-80%。When the filter material (4) is a catalytic cloth bag, the dioxin removal efficiency of the filter material (4) is 50-60% for a process temperature range of 120-150°C; for a process temperature range of 150-180°C, the filter The dioxin removal efficiency of the material (4) is 60-70%; for the process temperature range of 180-220°C, the dioxin removal efficiency of the filter material (4) is 70-80%. 7.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价NOx对二噁英脱除效率的影响时，通过污染物发生器组件供应NOx和二噁英并随烟气进入加热器（1）加热，开启引风机（5），使含有NOx和二噁英的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5），干法反应器（2）不启用；化学药剂供应器组件向进入除尘器（3）前的烟气中喷洒脱硝还原剂氨水；在烟气中氨氮摩尔比不变的工况下，在干法反应器（2）的进气口上游设置第一入口烟气检测器（101），第一入口烟气检测器（101）取样并经实验室分析得到的二噁英的浓度为5-10ngTEQ/Nm3，第一入口烟气检测器（101）检测得到的NOx浓度为400-1200mg/m3；7. The multifunctional flue gas purification evaluation method according to claim 2 is characterized in that: when evaluating the influence of NOx on the dioxin removal efficiency, NOx and dioxins are supplied through the pollutant generator assembly and followed by The flue gas enters the heater (1) for heating, and the induced draft fan (5) is turned on, so that the flue gas containing NOx and dioxin flows through the heater (1), the dry process reactor (2), and the dust collector (3) in sequence. The filter material (4) and the induced draft fan (5) are not activated in the dry process reactor (2); the chemical agent supplier component sprays ammonia water, a denitration reducing agent, into the flue gas before entering the dust collector (3); in the flue gas Under the condition that the molar ratio of ammonia and nitrogen remains unchanged, a first inlet smoke detector (101) is arranged upstream of the air inlet of the dry process reactor (2), and the first inlet smoke detector (101) is sampled and tested in the laboratory The concentration of dioxin obtained by analysis is 5-10ngTEQ/Nm 3 , and the concentration of NOx detected by the first inlet smoke detector (101) is 400-1200 mg/m 3 ; 所述的滤料（4）为触媒陶瓷管，对于各工艺温度区间120-150℃，二噁英脱除效率为40-55%；对于各工艺温度区间180-220℃，二噁英脱除效率为50-65%；对于各工艺温度区间250-300℃，二噁英脱除效率为60-85%；对于工艺温度区间350-400℃，二噁英脱除效率为70-89%。The filter material (4) is a catalyst ceramic tube. For each process temperature range of 120-150°C, the dioxin removal efficiency is 40-55%; for each process temperature range of 180-220°C, the dioxin removal efficiency is 40-55%. The efficiency is 50-65%; for each process temperature range of 250-300°C, the dioxin removal efficiency is 60-85%; for the process temperature range of 350-400°C, the dioxin removal efficiency is 70-89%. 8.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价HCl对二噁英脱除效率的影响时，通过污染物发生器组件供应HCl和二噁英并随烟气进入加热器（1）加热，开启引风机（5），使含有HCl和二噁英的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）；化学药剂供应器组件向干法反应器（2）中投加脱酸吸收剂干粉；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101），第一入口烟气检测器（101）取样并经实验室分析得到的二噁英的浓度为5-10ngTEQ/Nm3，第一入口烟气检测器（101）检测得到的HCl的浓度为500-12000mg/m3；8. The multifunctional flue gas purification evaluation method according to claim 2, characterized in that: when evaluating the influence of HCl on the dioxin removal efficiency, supply HCl and dioxin through the pollutant generator assembly and follow the flue gas. Enter the heater (1) for heating, turn on the induced draft fan (5), so that the flue gas containing HCl and dioxin flows through the filter material of the heater (1), the dry process reactor (2), and the dust collector (3) in turn. (4) and the induced draft fan (5); the chemical agent supplier component adds the deacidification absorbent dry powder into the dry process reactor (2); the first inlet smoke is arranged upstream of the air inlet of the dry process reactor (2). gas detector (101), the concentration of dioxin obtained by the first inlet smoke detector (101) is 5-10ngTEQ/Nm 3 by sampling and laboratory analysis, and the first inlet smoke detector (101) detects and obtains The concentration of HCl is 500-12000mg/m 3 ; 所述的滤料（4）为触媒陶瓷管；脱酸吸收剂干粉为消石灰粉末时，消石灰粉末与HCl的摩尔比为1，脱酸吸收剂干粉为碳酸氢钠粉末时，碳酸氢钠粉末与HCl的摩尔比为1，脱酸吸收剂干粉为高效熟石灰粉末时，高效熟石灰粉末与HCl的摩尔比为1.5；对于工艺温度区间120-150℃，二噁英脱除效率为20-40%；对于工艺温度区间180-220℃，二噁英脱除效率为20-60%；对于工艺温度区间250-300℃，二噁英脱除效率为20-80%；对于工艺温度区间350-400℃，二噁英脱除效率为30-90%。The filter material (4) is a catalyst ceramic tube; when the deacidification absorbent dry powder is slaked lime powder, the molar ratio of slaked lime powder to HCl is 1, and when the deacidification absorbent dry powder is sodium bicarbonate powder, the sodium bicarbonate powder and the The molar ratio of HCl is 1, and when the deacidification absorbent dry powder is high-efficiency slaked lime powder, the molar ratio of high-efficiency slaked lime powder to HCl is 1.5; for the process temperature range of 120-150 °C, the dioxin removal efficiency is 20-40%; For the process temperature range of 180-220°C, the dioxin removal efficiency is 20-60%; for the process temperature range of 250-300°C, the dioxin removal efficiency is 20-80%; for the process temperature range of 350-400°C , the dioxin removal efficiency is 30-90%. 9.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价SOx对二噁英脱除效率的影响时，通过污染物发生器组件供应SOx和二噁英并随烟气进入加热器（1）加热，开启引风机（5），使含有SOx和二噁英的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）；化学药剂供应器组件向干法反应器（2）中投加脱酸吸收剂干粉；在干法反应器（2）的进气口上游设置第一入口烟气检测器（101），第一入口烟气检测器（101）取样并经实验室分析得到的二噁英的浓度为5-10ngTEQ/Nm3，第一入口烟气检测器（101）检测得到的SOx的浓度为200-2000mg/m3；9. The multifunctional flue gas purification evaluation method according to claim 2 is characterized in that: when evaluating the influence of SO x on the dioxin removal efficiency, SO x and dioxin are supplied through the pollutant generator assembly and accompanied by The flue gas enters the heater (1) for heating, and the induced draft fan (5) is turned on, so that the flue gas containing SO x and dioxins flows through the heater (1), the dry process reactor (2), and the dust collector (3) in sequence. filter material (4) and induced draft fan (5); the chemical agent supply component adds the deacidification absorbent dry powder into the dry process reactor (2); a third An inlet smoke detector (101), the concentration of dioxin obtained by the first inlet smoke detector (101) and analyzed by the laboratory is 5-10ngTEQ/Nm 3 , the first inlet smoke detector (101 ) The detected SO x concentration is 200-2000 mg/m 3 ; 所述的滤料（4）为触媒陶瓷管；脱硫吸收剂干粉为高效熟石灰粉末时，高效熟石灰粉末与SOx的摩尔比为2，脱硫吸收剂干粉为碳酸氢钠时，碳酸氢钠与SOx的摩尔比为1.5，脱硫吸收剂干粉为消石灰粉末时，消石灰粉末与SOx的摩尔比为3；The filter material (4) is a catalyst ceramic tube; when the desulfurization absorbent dry powder is high-efficiency slaked lime powder, the molar ratio of the high-efficiency slaked lime powder to SO x is 2, and when the desulfurization absorbent dry powder is sodium bicarbonate, sodium bicarbonate and SO The molar ratio of x is 1.5, and when the dry powder of the desulfurization absorbent is slaked lime powder, the molar ratio of slaked lime powder to SO x is 3; 对于工艺温度区间120-150℃，二噁英脱除效率为10-30%；对于工艺温度区间180-220℃，二噁英脱除效率为20-50%；对于工艺温度区间250-300℃，二噁英脱除效率为30-70%；对于工艺温度区间350-400℃，二噁英脱除效率为40-80%。For the process temperature range of 120-150°C, the dioxin removal efficiency is 10-30%; for the process temperature range of 180-220°C, the dioxin removal efficiency is 20-50%; for the process temperature range of 250-300°C , the dioxin removal efficiency is 30-70%; for the process temperature range of 350-400 ℃, the dioxin removal efficiency is 40-80%. 10.根据权利要求2所述的多功能烟气净化评价方法，其特征是：评价压差时：10. The multifunctional flue gas purification evaluation method according to claim 2 is characterized in that: when evaluating the differential pressure: 在冷态条件下，启动引风机（5），使烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5），加热器（1）不启动；在除尘器（3）的进气口烟道和出气口烟道上设置压差传感器（12），在过滤风速不变的条件下，通过压差传感器（12）测定压差，不同滤料（4）的压差范围为300-1200pa；改变过滤风速，通过压差传感器（12）测定滤料（4）在过滤风速0.5-3 m/min时的压差，压差范围为300-2500pa；在风量不变的条件下，向烟气中分批投加共50g干粉，通过压差传感器（12）测定除尘器（3）进出气口的压差，压差范围为500-3500pa；Under cold conditions, start the induced draft fan (5), so that the flue gas flows through the heater (1), the dry process reactor (2), the filter material (4) of the dust collector (3) and the induced draft fan (5) in sequence , the heater (1) does not start; a differential pressure sensor (12) is set on the air inlet flue and the air outlet flue of the dust collector (3). Measure the pressure difference, the pressure difference range of different filter materials (4) is 300-1200pa; change the filtering wind speed, measure the pressure difference of the filter material (4) when the filtering wind speed is 0.5-3 m/min through the differential pressure sensor (12), The pressure difference range is 300-2500pa; under the condition of constant air volume, add a total of 50g dry powder to the flue gas in batches, and measure the pressure difference between the inlet and outlet of the dust collector (3) through the pressure difference sensor (12). 500-3500pa; 在热态条件下，向烟气中分批投加共50g干粉，启动引风机（5），使含有干粉的烟气依次流经加热器（1）、干法反应器（2）、除尘器（3）的滤料（4）和引风机（5）并通过加热器（1）加热；在各工艺温度区间内，通过压差传感器（12）测定除尘器（3）进出气口的压差，压差范围为500-3600pa。Under hot conditions, add a total of 50g of dry powder to the flue gas in batches, start the induced draft fan (5), and make the flue gas containing dry powder flow through the heater (1), the dry process reactor (2), and the dust collector in sequence. The filter material (4) and the induced draft fan (5) of (3) are heated by the heater (1); in each process temperature range, the pressure difference between the inlet and outlet of the dust collector (3) is measured by the differential pressure sensor (12). The differential pressure range is 500-3600pa.
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