CN220589535U - Waste incineration flue gas treatment system - Google Patents
Waste incineration flue gas treatment system Download PDFInfo
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Abstract
本实用新型提供了一种垃圾焚烧烟气处理系统，采用高比表面积、高孔容的熟石灰作为脱硫剂，并采用高温干法脱硫、触媒陶瓷纤维管反应器及后处理装置的搭配使用，在一定温度范围即可将污染物高效处理干净，以更短的工艺流程达到垃圾焚烧烟气超净排放要求，具有高效、稳定、运行费用低等性能优越性，经处理后干净烟气可较传统方法多回收大量烟气余热，且有效对后续余热回收装置提供保护，大大减少换热面被粉尘(尤其是黏性粉尘)堵塞覆盖的风险，提升换热效率，实现了垃圾焚烧飞灰减排及资源化利用。
The utility model provides a waste incineration flue gas treatment system, which uses hydrated lime with high specific surface area and high pore volume as the desulfurization agent, and adopts the combination of high-temperature dry desulfurization, catalyst ceramic fiber tube reactor and post-processing device to achieve a certain temperature at a certain temperature. The pollutants can be treated efficiently within the scope, and the ultra-clean emission requirements of waste incineration flue gas can be achieved with a shorter process flow. It has the performance advantages of high efficiency, stability, and low operating costs. After treatment, the clean flue gas can be produced more than traditional methods. It recovers a large amount of flue gas waste heat and effectively protects the subsequent waste heat recovery device, greatly reducing the risk of the heat exchange surface being blocked and covered by dust (especially sticky dust), improving heat exchange efficiency, and achieving waste incineration fly ash emission reduction and resource utilization.
Description
The present application claims a chinese prior application, application number: 2021217725282, priority of day 2021, month 7 and 30; all of which are included as part of the present utility model.
Technical Field
The utility model belongs to the field of environmental protection, relates to a garbage incineration flue gas treatment system, and particularly relates to a garbage incineration treatment system capable of efficiently recovering heat.
Background
Along with the development of cities, the total amount of household garbage is continuously increased, the existing treatment mode of the household garbage is mainly incineration, but the flue gas in the incineration process inevitably contains fly ash, and the fly ash generated by the incineration of the household garbage contains harmful substances such as dioxin and is classified as dangerous waste by the country due to the particularity of the household garbage. The moisture content of the waste incineration flue gas is large and generally reaches 20% -30%; the smoke contains toxic and harmful components, and contains various trace metals such as Pb, hg, cr and the like; the smoke contains complex components, SOx, dust, NOx and the like, and contains more acid gases such as HCl, HF and the like; strong cancerogenic substances such as dioxin, furan and the like exist; the dust has fine particle size, high viscosity, and strong polishing and impact properties.
The traditional waste incineration tail gas treatment process flow is longer, and adopts the processes of SNCR+semi-dry deacidification+dry deacidification+active carbon jet adsorption+bag dust collector+SGH (steam heating) +SCR+GGH (flue gas reheating), and the specific process steps are as follows: 1) The flue gas from the garbage incinerator firstly removes part of nitrogen oxides in the incinerator through SNCR, and then exchanges heat through a waste heat boiler/economizer and an air preheater, so that the temperature of the outlet flue gas is 230-250 ℃; 2) The flue gas at the outlet of the waste heat boiler enters a rotary spray semi-dry deacidification tower for deacidification, the deacidification outlet temperature is about 155 ℃, and slaked lime is directly sprayed on a flue to remove redundant SO (sulfur dioxide) X The method comprises the steps of carrying out a first treatment on the surface of the 3) The flue gas after deacidification is added with activated carbon to adsorb heavy metals and dioxin in the flue gas; 4) The flue gas after being sprayed and absorbed by the activated carbon enters a bag type dust collector for dust removal; 5) The flue gas from the bag dust removal is heated to about 200 ℃ through SGH saturated steam and mixed with the sprayed ammonia gas, and then enters a medium-low temperature denitration SCR reactor to remove nitrogen oxides in the flue gas; 6) And the flue gas from the SCR system is subjected to GGH heat exchange with the flue gas before entering the SCR system, and the temperature of the flue gas after heat exchange is higher than the dew point and is pumped to a chimney by an induced draft fan for emission.
The above process has the following disadvantages: 1) The method has the advantages that the standard emission is finished in a mode of cooling, deacidifying and dedusting before heating and denitrating, the equipment flow is long, the heat of the flue gas cannot be utilized and is wasted, the flue gas is required to be additionally heated, and the defects of high operation cost (energy consumption, resistance, equipment maintenance and the like) and high equipment investment exist; 2) Because the flue gas temperature is lower, the middle-low temperature catalyst is unstable to operate and is easily blocked by ABS and sticky dust, the denitration efficiency is reduced, the front-stage deactivated catalyst has to be replaced frequently, the operation cost is increased, and the continuous operation of the incinerator is influenced; 3) The activated carbon is used for adsorbing dioxin, so that pollutants are captured from a gaseous state to a solid state, the use cost of the activated carbon is high, the adsorbed saturated activated carbon is required to be treated as hazardous waste, and a large amount of activated carbon has potential safety hazards such as spontaneous combustion; 4) The produced amount of the fly ash is large, the concentration of pollutants such as heavy metal, dioxin and the like in the fly ash is high, the fly ash is required to be used as hazardous waste for chelating and landfill disposal, and the disposal cost is extremely high.
The technology has high investment cost, low dioxin removal efficiency and large demand of activated carbon; in order to ensure the denitration efficiency and the service life of the SCR reactor at low temperature, the inlet SO is required to be strictly controlled 2 The concentration of the catalyst is higher than 180 ℃ and the catalyst can normally operate, so that a large amount of heat energy is consumed to heat the flue gas, the cloth bag and the catalyst are required to be replaced regularly, and the operation cost and the maintenance cost of the system are high.
The Chinese patent application with the application number of 201811485748.X discloses a flue gas purification system and a flue gas purification process, which adopt a technology of 'high-temperature TMSCR (titanium cotton catalytic filter element integrated purification), gas purification, dry injection, SDA deacidification (rotary spray semi-dry desulfurization), cloth bag dust remover and active carbon fixed bed adsorption' for garbage incineration flue gas treatment. However, with this technique, the following problems still remain: 1. after dust in the flue gas is filtered out by the titanium cotton filter element, the rear end is connected with a dry method and a semi-dry method desulfurization process, more dust desulfurization byproducts are injected, and then the dust is collected and removed by a cloth bag, so that dust components are collected, and the post-treatment cost is high; 2. the flue gas temperature is low during dry desulfurization and deacidification, and the desulfurization and deacidification treatment efficiency is low; 3. the titanium cotton filter core adopts titanium alloy as raw material, has low heat resistance, is generally below 300 ℃ and has high cost.
Therefore, a flue gas treatment system which can efficiently remove harmful substances such as dioxin, nitrogen oxides, sulfur oxides, heavy metals and the like in the flue gas of the garbage incineration, can recover heat to the maximum extent, and has the advantages of simple operation, energy conservation, emission reduction and low cost is urgently needed.
Disclosure of Invention
In order to solve the problems, the utility model provides a waste incineration flue gas treatment system, which adopts slaked lime with high specific surface area and high pore volume as an enhanced calcium-based adsorbent, adopts a high-temperature dry desulfurization method, a catalyst ceramic fiber tube reactor and a post-treatment device to be matched for use, can efficiently treat pollutants cleanly in a certain temperature range, meets the requirements of ultra-clean discharge of waste incineration flue gas with a shorter process flow, has the advantages of high efficiency, stability, low operation cost and the like, can recycle a large amount of flue gas waste heat after treatment compared with the traditional method, effectively protects a subsequent waste heat recovery device, greatly reduces the risk of blocking and covering a heat exchange surface by dust (especially viscous dust), improves the heat exchange efficiency, and realizes the emission reduction and resource utilization of waste incineration fly ash.
In one aspect, the utility model provides a garbage incineration flue gas treatment system, which mainly comprises a dry desulfurization device, an ammonia spraying system and a catalytic ceramic fiber tube reactor which are connected in sequence; the dry desulfurization device can spray a calcium-based desulfurizing agent, the calcium-based desulfurizing agent is slaked lime powder, and the specific surface area is more than or equal to 38m 2 Per gram, pore volume is not less than 0.20cm 3 /g。
The dry desulfurization device provided by the utility model can directly carry out high-temperature desulfurization on high-temperature flue gas (370-420 ℃) discharged from the garbage incinerator, and the desulfurized high-temperature flue gas is mixed with sprayed ammonia water and then directly enters the catalyst ceramic fiber tube integrated reactor, so that a large amount of dust (containing heavy metals and dioxin) and desulfurization byproducts are removed at one time.
The garbage incinerator according to the present utility model refers to any incinerator that can be used for garbage incineration, such as a grate furnace, a circulating-bed incinerator, etc. The flue gas treatment system for the garbage incinerator can be used for treating the flue gas by any flue gas burnt by the garbage incinerator.
The dry desulfurization device provided by the utility model is used for desulfurizing HCl and SO in the flue gas X The acid gas is removed to meet the ultra-low emission requirement, the viscous smoke is quenched and tempered, the ceramic fiber tube in the subsequent process section is protected, and the service life is prolonged.
BET surface area of ordinary slaked lime less than 18m 2 The calcium-based desulfurizing agent adopted by the utility model is high-efficiency calcium-based desulfurizing agent slaked lime powder with high pore volume and high specific surface area, and the specific surface area is more than or equal to 38m 2 Per gram, pore volume is not less than 0.20cm 3 The purity of the slaked lime powder is more than or equal to 93 percent, the passing rate of the slaked lime with the granularity of 800 meshes is more than or equal to 95 percent, and the slaked lime is an enhanced calcium-based adsorbent, can provide more contact area for acid gas, can adsorb more acid gas pollutants under the condition of the same slaked lime dosage, and has higher purityThe activity and absorption efficiency of the catalyst are not needed by a grinding system, the fly ash production amount is small, and no waste water is produced.
Researches prove that the high-efficiency calcium-based desulfurizing agent with high pore volume and high specific surface area has highest deacidification and desulfurization efficiency in a high-temperature range of 350-450 ℃, can achieve more than 99% adsorption effect on high-concentration acidic pollutants, and has lower sensitivity on the influence of water content and other gases in flue gas.
The flue gas from the incinerator contains basically acidic pollutants, such as the concentration of acidic pollutants such as SO 2 Or generally greater than 800mg/Nm 3 By controlling the dry desulfurization device to be introduced in the high temperature range of 350-450 ℃, the ultrahigh adsorption effect of the high-efficiency calcium-based desulfurizing agent with high pore volume and high specific surface area can be fully utilized, and the ultrahigh deacidification efficiency can be realized.
The catalyst ceramic fiber tube has high-precision filtering capability and very good high-temperature resistance, can directly treat high-temperature flue gas after dry desulfurization, simultaneously realize dust removal, denitration and dioxin removal of the flue gas, has small temperature loss (less than 20 ℃), shortens the process flow, reduces the occupied area, improves the running stability and the operation portability of the device, reduces the investment cost and the running cost, improves the waste heat recovery efficiency and the recovery quantity of the treated clean flue gas, and has high recovery benefit.
Therefore, the dry desulfurization device suitable for high-temperature desulfurization and the composite ceramic fiber tube reactor suitable for high-temperature removal of a large amount of dust (containing heavy metals and dioxin) and desulfurization byproducts are perfectly combined, and the device is particularly suitable for high-efficiency purification treatment and high-efficiency heat energy recovery of waste incineration flue gas.
The utility model creatively adopts the high-temperature dry desulfurization and catalyst ceramic fiber tube reactor combination of the high-efficiency calcium-based desulfurizing agent with high pore volume and high specific surface area in the waste incineration industry, controls the smoke extraction temperature in the waste incinerator to be in the range of 350-450 ℃, can treat pollutants as clean as possible at the front end, meets the requirement of ultra-clean discharge of the waste incineration smoke with a shorter process flow, has higher waste heat recovery efficiency in the middle cooling stage, solves the difficult problem of high-efficiency recovery and utilization of the waste heat after removing the pollutants in the high-temperature section, and achieves the purposes of energy conservation and consumption reduction.
Further, the catalyst ceramic fiber pipe reactor comprises a ceramic fiber pipe body and catalyst catalysts, wherein the catalyst catalysts are distributed on the ceramic fiber pipe body.
Further, the ceramic fiber pipe body consists of ceramic fibers; the catalyst is distributed on the ceramic fibers of the ceramic fiber pipe body from inside to outside.
Further, the catalyst is a vanadium-titanium or vanadium-titanium-tungsten catalyst.
The catalyst ceramic fiber tube adopted by the utility model is formed by pressing and drying a ceramic fiber (with the diameter of about 2-3 microns) grinding tool with high porosity and low density, and the basic material of the catalyst ceramic fiber tube is composed of aluminum silicate fibers and inorganic adhesive, is not easy to react with chemical substances, can resist high temperature of 750 ℃ under the condition of not containing a catalyst, and can resist high temperature of 420 ℃ under the condition of attaching the catalyst.
The ceramic fiber pipe is independently developed and produced by the applicant, and an utility model patent CN110354912A is applied for a preparation process of the ceramic fiber pipe.
The ceramic fiber of the ceramic fiber pipe is formed by molding and drying a grinding tool after wiredrawing at a high temperature of more than 1000 ℃, the porosity reaches 65-85%, the air permeability is high, the resistance in the operation process is low, the pores are many, and a large amount of catalyst can be responsible for on the ceramic fiber, so that the higher denitration and dioxin removal effect is realized, the cost is low, and only lower electricity consumption is needed.
The ceramic fiber tube catalyst is a vanadium-titanium catalyst, is uniformly distributed on the ceramic fiber tube body from inside to outside, has high denitration and dioxin removal efficiency, and has activity which is not easy to be adversely affected.
The catalyst ceramic fiber tube comprises a ceramic fiber filter tube with a catalyst, a bin, an ash bucket and a steel structure support, wherein the bin, the ash bucket and the steel structure support are the same as a cloth bag dust collector with a traditional structure, the basic principle of dust removal of the ceramic fiber filter tube is that the ceramic fiber filter tube is based on a high-porosity structure, a ceramic fiber gap with the diameter of 2-3 microns is subjected to surface filtration, dust cakes are formed on the surface of the ceramic fiber tube, when reflection pulse ash removal is carried out, the dust cakes attached to the surface can be stripped, but dust which is permeated to the ceramic fiber filter tube for one millimeter deep can not be removed, the dust can be prevented from further permeating the inside of the ceramic fiber filter tube, and the filtration efficiency is improved.
The removal principle of dioxin and denitration is based on a mixing technology of two effective base materials: the ceramic fiber filter tube and the vanadium-based catalyst are sprayed with ammonia water or urea at the inlet of the catalyst ceramic fiber filter tube, and under the action of the catalyst, dioxin and NO x The dioxin is decomposed and removed, the dioxin removal rate of the whole system reaches 99.7 percent, and the dioxin emission in the flue gas reaches the standard (0.1 TED-ng/m 3 ) The nitrogen oxide removal efficiency reaches more than 95 percent. The catalyst is uniformly distributed in the ceramic fiber filter tube, so that the contact area is larger, and the residence time and the removal efficiency are maximized.
Wherein, denitration catalysis mechanism:
4NO+4NH 3 +O 2 ---4N 2 +6H 2 O；4NO+2(NH 2 ) 2 CO+O 2 ---4N 2 +4H 2 O+2CO 2
dioxin removal mechanism:
C 12 HnCl 8-n O 2 +(9+0.5n)O 2 ＝(n-4)H 2 O+12CO 2 +(8-n)HCl
therefore, after the high-temperature flue gas is treated by the catalyst ceramic fiber tube, a large amount of dust (containing heavy metals and dioxin) and desulfurization byproducts are intercepted by the high-precision filtering capacity of the catalyst ceramic fiber tube and are sprayed to the outside of the dust hopper by pulse; the flue gas after the dust removal of the catalyst ceramic fiber tube passes through the filter tube and is fully contacted with catalyst catalysts distributed in the tube, and at the stage, gaseous dioxin is catalytically decomposed into harmless substances, and nitrogen oxides are catalytically reduced.
The denitration temperature of the traditional waste incineration tail gas treatment process is below 220 ℃, sulfur dioxide is easy to react with ammonia in the flue gas to generate ammonium sulfate and ammonium bisulfate due to various reasons at low temperature, and the substance is a sticky substance which is easy to adhere to the active surface of a catalyst, so that the contact specific surface area of the catalyst is reduced, and the denitration efficiency is reduced. The viscous substance can be gradually decomposed at 280 deg.C, and can be completely decomposed at 320 deg.C or above, and the catalyst can be recovered.
Meanwhile, the SCR catalyst needs to operate at relatively clean flue gas and at a proper reaction temperature (250-320), the traditional process is limited by the temperature resistance of bag dust removal, the flue gas can only be heated to 180-200 ℃ after being subjected to bag dust removal (140 ℃) for denitration, and a large amount of steam is consumed.
Further, the system also comprises a superheater, wherein an inlet of the superheater is connected with the garbage incinerator, and an outlet of the superheater is connected with the dry desulfurization device.
Further, the superheater comprises a convection evaporator, a high-temperature superheater, a medium-temperature superheater and a low-temperature superheater which are sequentially connected; and the outlet of the low-temperature superheater is connected with a dry desulfurization device.
Further, the device also comprises an economizer, and the outlet of the catalytic ceramic fiber tube reactor is connected with the inlet of the economizer.
The economizer is a device which is arranged at the lower part of a tail flue of a boiler and is used for recovering the waste heat of discharged smoke, and heats boiler feed water into a heating surface of saturated water under the pressure of a steam drum.
The initial temperature of the flue gas generated in the garbage incinerator can reach thousands of degrees, after heat is recovered through an evaporator and a superheater and cooled, the temperature of the flue gas is reduced to about 370-400 ℃ and is led to a flue for purification treatment, after the flue gas is treated through a dry desulfurization device and a catalytic ceramic fiber tube reactor, the flue gas Wen Sun is very small and is less than 20 ℃, and the flue gas is directly led back to an economizer at about 350-390 ℃ to continuously recover the heat until the temperature of the flue gas is reduced to 20 ℃ above an acid dew point, so that the heat in the flue gas is fully recovered, and the energy is further saved and the consumption is reduced.
Further, the device also comprises an after-treatment device.
Further, the post-treatment device comprises an activated carbon spraying device and a bag-type dust remover.
Further, the active carbon spraying device is connected with the bag-type dust remover; the outlet of the coal economizer is connected with the inlet of the active carbon spraying device, and the outlet of the active carbon spraying device is connected with the inlet of the bag-type dust collector.
The flue gas discharged from the outlet of the economizer can be further adsorbed and removed by adding a post-treatment device to the trace heavy metals which are possibly separated out during cooling and the regenerated small amount of dioxins. The post-treatment device can adopt a combination of an active carbon spraying device and a bag-type dust remover, and the collected dust is discharged from a discharge hole of the bag-type dust remover. Compared with the fly ash collected by the traditional garbage incineration treatment process, the fly ash collected by the part is greatly reduced, so that the emission reduction and the resource utilization of the fly ash are realized.
In still another aspect, the utility model provides a method for treating waste incineration flue gas, which is characterized by comprising the following steps:
1) The flue gas is led out from the coal economizer of the garbage incinerator and enters a dry desulfurization device, and acidic pollutants (HCl, HF and SO) in the flue gas are removed by spraying a calcium-based desulfurizing agent 2 )；
2) Spraying ammonia water into the flue gas obtained in the step 1), mixing the flue gas with the ammonia water, and then feeding the mixture into a catalytic ceramic fiber tube reactor to remove dust, heavy metals, nitrogen oxides and dioxin; the dioxin is catalytically decomposed, and the nitrogen oxides are catalytically reduced;
3) The flue gas obtained in the step 2) enters an economizer to recycle heat;
4) The flue gas after heat exchange recovered by the economizer is further removed heavy metal or regenerated dioxin precipitated by cooling through a post-treatment device, and dust is collected;
5) Is discharged outside through a chimney.
Further, when the flue gas in the step 1) is led out from the economizer of the garbage incineratorThe temperature of (2) is 370-400 ℃; the calcium-based desulfurizing agent is slaked lime powder with specific surface area more than or equal to 38m 2 Per gram, pore volume is not less than 0.20cm 3 /g。
Further, in the step 2), the temperature of the flue gas in the catalytic ceramic fiber tube reactor is 350-390 ℃ and the flow rate of the flue gas is 0.8-1.2 m/min.
Further, the flue gas in the step 3) enters an economizer to exchange heat for recovering heat, the temperature of the flue gas before heat exchange is 330-370 ℃, and the temperature of the flue gas after heat exchange is 20 ℃ above the acid dew point.
The temperatures given herein are not meant to be limiting, and for example, the temperature at which the economizer is drawn may be anywhere in the vicinity of 370-400 ℃, such as 360.1 ℃, … 361.5 ℃, … 362.3 ℃, … 400.5.5 ℃, … 411.2 ℃, … 420.1.1 ℃, etc., and temperatures in the vicinity of the temperature ranges described herein are all within the scope of the present utility model.
The traditional method mainly adopts a rotary spray semi-dry method to carry out desulfurization, a great amount of moisture takes away the latent heat of the flue gas, and after the pollutants of the waste incineration flue gas are removed, the flue gas temperature is too low, the waste heat utilization efficiency of the tail gas is very low, and the tail gas is difficult to recycle. Because the temperature of the flue gas at the boiler outlet is 230-250 ℃ in the traditional method, the flue gas enters the tail gas treatment system for treatment, and the temperature of the treated tail gas is only 140-150 ℃, so that the heat of the flue gas at 240-140 ℃ is difficult to recycle.
The utility model adopts the full-dry process, and can treat the flue gas cleanly in a high temperature section, so that the flue gas can be directly subjected to waste heat utilization in a relatively high temperature section, the flue gas is led out of the economizer for treatment at 370-400 ℃, the temperature of the flue gas is reduced to about 350 ℃ after the treatment, and then the flue gas is led back to the economizer for waste heat utilization, and the flue gas is discharged when the temperature of the flue gas is reduced by 120 ℃ or lower, so that the utilization temperature section of the flue gas is wider, and the heat utilization efficiency is higher. Meanwhile, the corrosion influence of clean flue gas on equipment can be reduced to the minimum, and the waste heat recovery efficiency can be further improved without dust.
According to the utility model, wen Sunxiao (< 20 ℃) of the high-temperature section dry desulfurization and catalyst ceramic fiber filter cartridge is adopted, the waste heat recovery is carried out on the treated clean flue gas, the heat recovery of the flue gas in the whole temperature section of 100-350 ℃ can be almost covered, the recovery benefit is high, meanwhile, the influence of blockage, corrosion and the like of the heat exchange surface of an air preheater or a subsequent heat exchange device can be reduced by the clean flue gas, the heat exchange efficiency is improved, the operation and maintenance cost of the device is reduced, and the purposes of energy conservation and consumption reduction are achieved.
Further, the post-treatment device in the step 4) is an activated carbon injection device and a bag-type dust remover; the temperature of the flue gas in the post-treatment device is 140 ℃, and heavy metals in dust collected by the bag-type dust collector can be recycled.
The rear end cloth bag only needs to collect the sprayed activated carbon powder and a small amount of substances such as heavy metal and dioxin absorbed at a low temperature Duan Xichu, the collected substances are purer, and the post-treatment cost is lower.
According to the emission index requirement of GB18485-2014 'pollution control Standard for household garbage incineration', for main pollutants: the particle is less than or equal to 20mg/m 3 Nitrogen oxides (NOx) are less than or equal to 250mg/m 3 Sulfur dioxide (SO) 2 )≤80mg/m 3 Hydrogen chloride (HCl) is less than or equal to 50mg/m 3 Dioxin is less than or equal to 0.1ng TEQ/m 3 。
By adopting the garbage incineration flue gas treatment system provided by the utility model, the emission indexes of main pollutants can be satisfied: the particle is less than or equal to 5mg/m 3 Nitrogen oxides (NOx) are less than or equal to 50mg/m 3 Sulfur dioxide (SO) 2 )≤35mg/m 3 Hydrogen chloride (HCl) is less than or equal to 1mg/m 3 Dioxin is less than or equal to 0.01ngTEQ/m 3 The particulate matters, nitrogen oxides and sulfur dioxide can meet the national ultra-low emission requirements on main flue gas pollutants of coal-fired power plants, and the dioxin is far lower than the emission concentration of the dioxin in the EU waste incineration pollutant emission standard DIRECTIVE _2000, so that high environmental benefits are brought.
According to GB18485-2014 "pollution control standards for household refuse incineration", 3.5 incinerator slag is defined as: residues directly discharged from a hearth after the household garbage is burnt, and ash residues discharged by a superheater and an economizer; incineration fly ash is defined as: the fume purifying system captures matters and bottom ash settled at the bottom of a flue and a chimney, wherein the incineration fly ash is managed according to dangerous waste, and the household garbage incinerator slag (excluding the incineration fly ash) can directly enter a household garbage landfill for disposal in GB 16889-2008 pollution control Standard of the household garbage landfill 6.1.
In the flue gas treatment system provided by the utility model, flue gas is directly led out from a proper temperature window between the economizers, and is led back to the economizers after being treated, the collected ash slag is essentially consistent with the slag, and the flue gas can directly enter a household garbage landfill for disposal or can be recycled after being inspected to be qualified without being treated by dangerous waste.
Compared with the traditional waste incineration tail gas treatment process, incineration fly ash is collected at a low temperature section after waste heat recovery and utilization, dioxin treatment mainly depends on spraying a large amount of activated carbon for adsorption and collection, the heavy metal content and the regenerated dioxin content in the fly ash are high, the waste incineration tail gas must be treated as hazardous waste, the treatment cost is extremely high, and the excessive risk of the possibility of dioxin in the discharged tail gas still exists.
The treatment system is characterized in that ash in the flue gas is trapped in a large amount (trapping efficiency is more than or equal to 99%) in advance by combining a dry deacidification and catalyst ceramic fiber filter tube process at a high temperature section, the property of the ash is consistent with that of the slag, the ash can directly enter a household garbage landfill for disposal or can be recycled through identification, the ash is prevented from being treated as dangerous waste, gaseous dioxin in the flue gas is oxidized and decomposed into harmless substances by a catalyst attached to the upper surface when passing through the catalyst ceramic fiber tube, the flue gas is led back to an economizer for waste heat utilization after the high temperature treatment, the tail end of the flue gas is further adsorbed and removed by adding a post-treatment device such as active carbon spraying and a bag dust collector for trace heavy metals which may be separated out during cooling and a small amount of regenerated dioxin, the collected dust is discharged from a discharge port of the bag dust collector, and the fly ash collected in the part is greatly reduced compared with fly ash collected by the traditional incineration treatment process, so that the fly ash emission reduction and recycling are realized.
The traditional tail gas treatment process is characterized in that the flue gas is heated by steam after being cooled and enters an SCR denitration device to remove nitrogen oxides, because the SCR catalyst needs to operate at relatively clean flue gas and at a proper reaction temperature (250-320 ℃), the traditional process is limited by the temperature resistance of bag dust removal, and the flue gas can only be heated to 180-200 ℃ after the bag (140 ℃) to consume a large amount of steam, so that the incineration fly ash disposal cost accounts for more than 40% of the total operation cost; by adopting the flue gas treatment system, the operation cost of the garbage incineration treatment plant can be greatly reduced (the comprehensive reduction of the waste heat recovery is more than 50 percent), and the flue gas treatment system has high economic benefit.
The utility model has the beneficial effects that:
(1) High-temperature dry-method high-efficiency desulfurization: the high-temperature dry desulfurization is carried out by taking the high-pore-volume high-specific-surface-area calcium-based desulfurizing agent as an absorbent, and the high-pore-volume high-specific-surface-area calcium-based desulfurizing agent has extremely high removal efficiency on high-concentration acidic pollutants at the temperature of 350-450 ℃ so as to fully remove the high-concentration acidic pollutants in the waste incineration flue gas, a grinding system is not needed, the fly ash is less in production amount, no waste water is generated, the viscous flue gas has a tempering effect, a protective effect is formed on ceramic fiber tubes of subsequent process sections, and the service life is prolonged.
(2) High-efficiency integrated dust removal, denitration and dioxin removal: the catalyst ceramic fiber tube is adopted to realize the high-temperature dust removal, denitration and dioxin removal integrated reaction of the flue gas, so that the process flow is shortened, the occupied area is reduced, the running stability and the operation portability of the device are improved, and the investment cost and the running cost are reduced.
(3) Perfect combination of high-temperature dry desulfurization and catalytic ceramic fiber tube: the combination of high-temperature dry desulfurization and the catalyst ceramic fiber tube is adopted, pollutants can be efficiently and cleanly treated at the high temperature of the front end, the ultra-clean emission requirement of the waste incineration flue gas is met by a shorter process flow, and the blocking and corrosion effects of the clean flue gas at the rear end on equipment can be reduced to the minimum.
(4) Waste heat recovery efficiency is high: the flue gas is directly led out from a proper temperature window between the economizers, the temperature loss treated by the high-temperature section dry desulfurization and the catalyst ceramic fiber filter cylinder is small (< 20 ℃), the treated clean flue gas is led back to the economizers for waste heat recovery, the flue gas heat recovery of the full-temperature section can be almost covered, the recovery benefit is high, the difficult problem of high-efficiency recovery and utilization of the waste heat after the pollutants are removed from the high-temperature section is solved, and the purposes of energy conservation and consumption reduction are achieved.
(5) The dust is safe and can be recycled: the collected dust ash is verified to be basically consistent with the slag in nature, and the collected dust ash can directly enter a household garbage landfill for disposal or can be recycled after being inspected to be qualified, so that the emission reduction and recycling of the fly ash are realized.
(6) High-temperature high-efficiency denitration does not need repeated heating: the SCR catalyst needs to operate at relatively clean flue gas and at a proper reaction temperature (250-320), the traditional process is limited by the temperature resistance of bag dust removal, the flue gas can only be heated to 180-200 ℃ for denitration after the bag is filled with the flue gas (140 ℃), and a large amount of steam is consumed.
Drawings
Fig. 1 is a schematic view showing the overall structure of the garbage incineration disposal system in example 1.
Detailed Description
The following description of the preferred embodiments of the present utility model in further detail with reference to the accompanying drawings, it should be noted that the following embodiments are intended to facilitate an understanding of the present utility model, and are not intended to limit the utility model in any way, and all of the features disclosed in the embodiments of the present utility model, or all of the steps in the methods or processes disclosed, can be combined in any way, except mutually exclusive features and/or steps.
Example 1 the refuse incineration flue gas treatment system provided by the utility model
The garbage incineration flue gas treatment system provided by the embodiment is shown in fig. 1, and comprises a superheater 1, a dry desulfurization device 2, an ammonia injection system 3, a catalytic ceramic fiber tube reactor 4, an economizer 5 and a post-treatment device 6.
The superheater 1 includes a convection evaporator 7, a high temperature superheater 8, a medium temperature superheater 9 and a low temperature superheater 10. The outlet of the low-temperature superheater 10 is connected with the dry desulfurization device 2, and the outlet of the catalytic ceramic fiber tube reactor 4 is connected with the inlet of the economizer 5.
Preferably, the catalytic ceramic fiber tube reactor 4 comprises a ceramic fiber tube body and a catalytic catalyst; the ceramic fiber pipe body consists of ceramic fibers; the catalyst is distributed on the ceramic fiber pipe body from inside to outside; the catalyst is a vanadium-titanium catalyst.
The post-treatment device 5 in the embodiment comprises an activated carbon injection device 12 and a bag-type dust collector 13, and the outlet 5 of the economizer 5 is connected with the post-treatment device 5.
When the flue gas exhausted from the garbage incinerator 11 is subjected to heat exchange to 370-400 ℃ through the heater 1, the flue gas is exhausted through the outlet of the heater 1, enters the dry desulfurization device 2 (if the flue is long enough, the flue gas can be directly sprayed from the flue), and the dry desulfurization device 2 sprays calcium-based desulfurizing agent slaked lime powder with high pore volume and high specific surface area to perform desulfurization and deacidification, SO that HCl and SO in the flue gas are treated X The flue gas is subjected to quenching and tempering treatment in the process until the flue gas meets the ultra-low emission requirement, so that the influence of sticky dust and tar matters on the normal operation of subsequent process equipment is prevented. The garbage incinerator 11 adopted in the embodiment is a grate furnace, but this is not meant to limit the utility model, and any flue gas obtained by incinerating the garbage incinerator can be treated by adopting the garbage incineration flue gas treatment system provided by the utility model, and the utility model is within the protection scope of the utility model.
The specific surface area of the calcium-based desulfurizing agent slaked lime powder is 40+/-2 m 2 Per g, pore volume of 0.22.+ -. 0.2cm 3 And/g. Then through the ammonia spraying system 3, the flue gas and ammonia water are mixed and enter a catalytic ceramic fiber tube for reaction 4, a large amount of dust (containing heavy metals and dioxin) and desulfurization byproducts are intercepted and filtered by the high-precision filtering capacity of a catalytic ceramic filter tube and are sprayed to the outside of a dust collecting ash bucket through pulse, the flue gas after dust removal passes through the filter tube and fully contacts with catalyst catalysts distributed in the tube, at the stage, gaseous dioxin is catalytically decomposed, and nitrogen oxides are catalytically reduced; the temperature of the flue gas in the catalyst ceramic fiber tube reactor 4 is 350-390 ℃ and the flow rate of the flue gas is 0.8-1.2 m/min. The temperature of the flue gas discharged from the catalyst ceramic fiber tube reactor 4 is reduced (10-20 ℃), and the flue gas is treatedThe flue gas still has higher temperature, and then returns to the economizer 5 to recover heat, the temperature of the flue gas before heat exchange is 330-370 ℃, and the temperature of the flue gas after heat exchange is 20 ℃ above the acid dew point. Considering that a small amount of heavy metal can be separated out and dioxin can be regenerated in the flue gas cooling stage, an activated carbon supply system 12 and a bag-type dust collector 13 are additionally arranged at the tail end to adsorb and remove the separated heavy metal and dioxin, dust is collected by the bag-type dust collector 13, and the heavy metal in the dust can be recycled. The purified flue gas is discharged to the air through the chimney.
Example 2 Effect of different temperatures, calcium to Sulfur ratio contaminants on desulfurization Effect of different desulfurizing Agents
The high-efficiency desulfurizing agent provided by the embodiment is divided into two types, wherein one type is a common calcium-based desulfurizing agent, and the other type is an enhanced calcium-based adsorbent with high specific surface area and high pore volume, and the high-efficiency removal of acidic pollutants is achieved by activating the surface activity.
Wherein the chemical index of the first common calcium-based desulfurizing agent is as follows: effective calcium>88%, moisture content<1%; physical properties indexes: specific surface area of 18+ -2 m 2 Per g, pore volume of 0.15+ -0.2 cm 3 And/g. The test method meets the requirements of BS ISO 9277:2010; test equipment, vacPrep 061,MICROMERITICS Tristar IIPlus 3030; the specific surface area and pore volume parameters are based on average values.
Another chemical index of enhanced calcium-based sorbents: effective calcium>90%, moisture content<1%; physical properties indexes: specific surface area of 40+ -2 m 2 Per g, pore volume of 0.22+ -0.2 cm 3 And/g. The test method meets the requirements of BS ISO 9277:2010; test equipment, vacPrep 061,MICROMERITICS Tristar IIPlus 3030; the specific surface area parameter is based on average value, and the minimum value of specific surface area is not less than 38m 2 /g, pore volume minimum value not less than 0.20cm 3 /g。
2.1 adsorption Performance test
By using SO-containing materials 2 ：1500mg/Nm 3 Gas slaked lime to SO with CO2:9%, sr=3 2 Testing the adsorption performance, wherein the test temperature is from 150 ℃ to 500 ℃, and the average value is calculated for the dry and wet waste incineration flue gas with 5%, 15% and 25% respectivelyThe flue gas flow rate is 6-8m/s, the filling mode is pneumatic conveying, and the pipeline travel (contact residence time) is 3-5 seconds, and the detection results are shown in Table 1.
TABLE 1 influence of temperature on the adsorption performance of high-efficiency desulfurizing agent
As can be seen from Table 1, the deacidification efficiency was generally low when the first common calcium-based desulfurizing agent was used, and there was no obvious difference in deacidification efficiency as the temperature increased from 150℃to 500 ℃.
When the second enhanced calcium-based adsorbent is adopted, the deacidification efficiency is obviously increased, and the deacidification efficiency is obviously different along with the change of temperature; in the temperature range of 150-300 ℃, the deacidification efficiency is low due to the possible competitive adsorption of other gases in the flue gas, and the deacidification efficiency is not greatly different when the enhanced calcium-based adsorbent and the common calcium-based desulfurizing agent are adopted; the deacidification efficiency of the range of 50-150 ℃ (under the condition of humidifying the flue gas) and 350-450 ℃ (whether the flue gas is dry or wet), the sensitivity to the influence of the moisture content and other gases in the flue gas is low, particularly, the adsorption performance of the enhanced calcium-based adsorbent is rapidly increased in the range of 350-450 ℃, while the adsorption amplitude of the common calcium-based desulfurizing agent is very small although the adsorption performance is increased; and as the temperature continues to rise to 500 ℃, the adsorption efficiency is reduced again, and the adsorption performance of the enhanced calcium-based adsorbent is reduced more rapidly, so that the deacidification efficiency is not greatly different when the enhanced calcium-based adsorbent and the common calcium-based desulfurizing agent are adopted. Therefore, the adsorption efficiency can be obviously improved by adopting the enhanced calcium-based adsorbent and selecting 350-450 ℃.
The utility model provides a garbage incineration flue gas treatment system, the temperature of the flue gas led out of the garbage incineration flue gas treatment system is just 370-400 ℃, and the temperature range required by the optimal adsorption efficiency of the enhanced calcium-based adsorbent is completely met.
2.2 Low concentration acid pollutant with Ca/S ratio of 2 at 320 deg.c less than 360 deg.c
The flue gas treatment provided in example 1 was usedThe system comprises a calcium-based adsorbent, wherein the calcium-based adsorbent adopts common calcium-based desulfurizing agent and enhanced calcium-based adsorbent slaked lime powder respectively, and tests are carried out under the conditions that the inlet temperature is 320 ℃ and less than 360 ℃ and the calcium-sulfur ratio is 2, SO that SO of inlet and outlet flue gas is detected respectively 2 And HCl mean value, calculate SO 2 And HCl removal efficiency, wherein the inlet flue gas sample is taken at the inlet of the ceramic fiber pipe, because the inlet flue gas is not yet subjected to desulfurization reaction at the inlet of the ceramic fiber pipe after the slaked lime powder is sprayed, and the outlet flue gas sample is taken at the outlet of the cloth bag, and the desulfurization reaction is complete at the moment, and the detection result is shown in Table 2.
TABLE 2 detection results for low concentration of acidic contaminants at 320 < T < 360℃and a calcium to sulfur ratio of 2
As can be seen from Table 2, SO in the inlet flue gas 2 Mean value 82.31mg/m 3 HCl average value 4.76mg/m 3 The SO of the first enhanced calcium-based desulfurizing agent is low in concentration of acidic pollutants 2 The removal efficiency is 75.64%, and the HCl removal efficiency is 32.56%; SO in inlet flue gas 2 Average value 70.56mg/m 3 HCl mean 9.42mg/m 3 Is low-concentration acidic pollutant, and when common calcium-based desulfurizing agent is adopted, SO is generated 2 The removal efficiency was 62.34% and the HCl removal efficiency was 28.48%. The enhanced calcium-based adsorbent has better adsorption effect on low-concentration acidic pollutants than that of the common calcium-based desulfurizing agent at the high temperature of 320 ℃ less than 360 ℃ and the calcium-sulfur ratio of 2.
2.3 inlet temperature 320 ℃ less than 360 ℃, low concentration acid pollutant, calcium-sulfur ratio 1.5
By adopting the flue gas treatment system provided in example 1, the calcium-based adsorbent adopts the common calcium-based desulfurizing agent and the enhanced calcium-based adsorbent slaked lime powder respectively, and tests are carried out under the conditions that the inlet temperature is 320 ℃ less than 360 ℃, the low-concentration acid pollutant and the calcium-sulfur ratio are 1.5, SO that SO of the inlet flue gas and the SO of the outlet flue gas are detected respectively 2 And HCl mean value, calculateSO 2 And HCl removal efficiency, wherein an inlet smoke sample is taken at the inlet of the ceramic fiber tube, an outlet smoke sample is taken at the outlet of the cloth bag, and the detection results are shown in Table 3.
TABLE 3 detection results for low concentration of acidic contaminants at 320 < T < 360℃and a calcium to sulfur ratio of 1.5
As can be seen from Table 3, SO in the inlet flue gas 2 Mean value 58.78mg/m 3 HCl average value 0.47mg/m 3 The SO of the first enhanced calcium-based desulfurizing agent is low in concentration of acidic pollutants 2 The removal efficiency is 31.83%, and the HCl removal efficiency is 0; SO in inlet flue gas 2 Average value 68.39mg/m 3 HCl average value 0.87mg/m 3 Is low-concentration acidic pollutant, and when common calcium-based desulfurizing agent is adopted, SO is generated 2 The removal efficiency was 28.61% and the HCl removal efficiency was 0. It can be seen that the enhanced calcium-based adsorbent has SO to low concentration acidic pollutants at a high temperature of 320 ℃ less than 360 ℃ and a calcium-sulfur ratio of 1.5 2 The adsorption effect is slightly better than that of a common calcium-based desulfurizing agent, and the adsorption effect on HCl is not obviously different.
2.4 inlet temperature 216 ℃ less than T less than 241 ℃, high concentration acid pollutant, calcium-sulfur ratio is 2.5
In the embodiment, the flue gas treatment system provided in the embodiment 1 is adopted, the calcium-based adsorbent is reinforced calcium-based adsorbent slaked lime powder, and the tests are carried out under the conditions that the inlet temperature is 216 ℃ and less than 241 ℃ and the low-concentration acidic pollutants and the calcium-sulfur ratio are 2.5, SO that the SO of the inlet flue gas and the SO of the outlet flue gas are detected respectively 2 And HCl mean value, calculate SO 2 And HCl removal efficiency, wherein an inlet smoke sample is taken at the inlet of the ceramic fiber tube, an outlet smoke sample is taken at the outlet of the cloth bag, and the detection results are shown in Table 4.
TABLE 4 detection results of high concentration of acidic contaminants at 216℃ < T < 241℃and calcium-sulfur ratio of 2.5
As can be seen from Table 4, SO in the inlet flue gas 2 Average value 865.79mg/m 3 HCl mean 3310.81mg/m 3 When the first enhanced calcium-based desulfurizing agent is adopted as the high-concentration acidic pollutant, SO is generated 2 The removal efficiency is 5.75%, and the HCl removal efficiency is 99.81; SO in inlet flue gas 2 Average value 954.13mg/m 3 HCl mean 3520.93mg/m 3 Is high-concentration acidic pollutant, and when common calcium-based desulfurizing agent is adopted, SO is generated 2 The removal efficiency was 4.17% and the HCl removal efficiency was 75.31%.
It can be seen that the enhanced calcium-based adsorbent has SO to low concentration acidic pollutants at a high temperature of 216 ℃ less than T less than 241 ℃ and a calcium-sulfur ratio of 2.5 2 The adsorption effect of the catalyst is equivalent to or even slightly lower than that of a common calcium-based desulfurizing agent, and the adsorption effect of the catalyst on HCl is obviously higher than that of the common calcium-based desulfurizing agent, so that the adsorption removal effect of the enhanced calcium-based adsorbent is not far higher than that of the common calcium-based desulfurizing agent, and the enhanced calcium-based desulfurizing agent is influenced by various conditions such as temperature, acid pollutant concentration, smoke components and the like.
2.5 inlet temperature is more than 350 ℃ and less than 370 ℃, high concentration acid pollutant, and calcium-sulfur ratio is 2.5
In the embodiment, the flue gas treatment system provided in the embodiment 1 is adopted, the calcium-based adsorbent is reinforced calcium-based adsorbent slaked lime powder, and the tests are carried out under the conditions that the inlet temperature is more than 350 ℃ and less than 370 ℃ and the calcium-sulfur ratio is 2.5, SO that the SO of the inlet flue gas and the SO of the outlet flue gas are detected respectively 2 And HCl mean value, calculate SO 2 And HCl removal efficiency, wherein an inlet smoke sample is taken at the inlet of the ceramic fiber tube, an outlet smoke sample is taken at the outlet of the cloth bag, and the detection results are shown in Table 5.
TABLE 5 detection results for high concentration of acidic contaminants at 350 ℃ < T < 370 ℃ and a calcium to sulfur ratio of 2.5
As can be seen from Table 5, SO in the inlet flue gas 2 Mean value of299.05mg/m 3 HCl mean 13843.30mg/m 3 When the first enhanced calcium-based desulfurizing agent is adopted as the high-concentration acidic pollutant, SO is generated 2 The removal efficiency is 99.99 percent, and the HCl removal efficiency is 99.82 percent; SO in inlet flue gas 2 Average value 237.84mg/m 3 HCl mean 12459.45mg/m 3 Is high-concentration acidic pollutant, and when common calcium-based desulfurizing agent is adopted, SO is generated 2 The removal efficiency was 70.05% and the HCl removal efficiency was 82.31%. The enhanced calcium-based adsorbent has obviously higher adsorption effect on high-concentration acidic pollutants than that of a common calcium-based desulfurizing agent and has higher adsorption effect on HCl and SO when the calcium-sulfur ratio is 2.5 at the high temperature of 350 ℃ less than 370 DEG C 2 The adsorption effect of the catalyst can reach more than 99%, and the adsorption effect is extremely excellent.
It can be seen that the adsorption effect of the common calcium-based desulfurizing agent and the enhanced calcium-based adsorbent on pollutant gases with different concentrations is different under different conditions, and the adsorption effect of the common calcium-based desulfurizing agent is different from that of the enhanced calcium-based adsorbent (such as 2.4) under the medium and low temperature conditions, but the deacidification efficiency of the enhanced calcium-based adsorbent can reach more than 99% under a certain temperature range, acid pollutant concentration and calcium-sulfur ratio, and almost completely remove acid pollutants.
For the enhanced calcium-based adsorbents, the test data comparing 2.2, 2.3 shows that: under the conditions of low concentration acid pollutants and higher temperature, the higher the calcium-sulfur ratio is, the higher the deacidification efficiency is, but the overall acid pollutant removal efficiency is not high, and the higher removal efficiency is difficult to achieve due to the smaller concentration of the imported acid pollutants; the experimental data comparing 2.4 and 2.5 can be seen: under the condition of a certain calcium-sulfur ratio of high-concentration acidic pollutants, the higher the temperature is, the higher the deacidification efficiency is, and the overall acidic pollutant removal efficiency is also higher; from the data of 2.2, 2.3, 2.4 and 2.5, the higher the concentration of the acidic contaminant, the higher the temperature and the higher the calcium-sulfur ratio, the higher the removal efficiency of the contaminant. Wherein the temperature is 350-370 ℃, and the high-concentration pollutant with the calcium-sulfur ratio of 2.5 has the best effect.
The specific surface area of the enhanced calcium-based adsorbent in this example is not limited to 40.+ -.2 m 2 Per g, pore volume must be 0.22.+ -. 0.2cm 3 According to the experimental results, when the specific surface area is larger, the Kong Rongyue is larger, the superiority is more obvious, and the deacidification adsorption efficiency is more obviously improved at 350-450 ℃.
The concentration of the acidic pollutants in the waste incineration flue gas is different along with the concentration of the pollutants in different furnace types, when the concentration of the acidic pollutants in the flue gas is higher, the acidic pollutants are controlled in a proper temperature range and under a proper adding amount, and the flue gas is particularly suitable for deacidifying the enhanced calcium-based adsorbent with high specific surface area and high pore volume, provided by the utility model, SO that the SO of the flue gas is reduced 2 And HCl can be basically removed, and has good removal effect.
Example 3 comparison with a conventional refuse incineration flue gas treatment System
In this example, the garbage incineration flue gas treatment system provided in example 1 and the conventional garbage incineration flue gas treatment system (southbound 500 ton/day circulating fluidized bed garbage incineration device) existing in the market at present are adopted respectively, the garbage incineration flue gas treatment effect and the cost are compared, the treatment time is 24 hours, and the comparison result is shown in table 6.
TABLE 6 comparison with conventional refuse incineration flue gas treatment System
As can be seen from table 6, the garbage incineration flue gas treatment device provided by the utility model greatly improves the energy utilization rate, reasonably and efficiently utilizes the flue gas waste heat, and obviously inhibits the discharge of pollutant dioxin.
Various changes and modifications may be made by one skilled in the art without departing from the spirit and scope of the utility model, and the scope of the utility model should be assessed accordingly to that of the appended claims.
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