CN212651583U - Dual cycle formula active carbon separation is analytic msw incineration flue gas processing system - Google Patents
Dual cycle formula active carbon separation is analytic msw incineration flue gas processing system Download PDFInfo
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- CN212651583U CN212651583U CN202020933392.8U CN202020933392U CN212651583U CN 212651583 U CN212651583 U CN 212651583U CN 202020933392 U CN202020933392 U CN 202020933392U CN 212651583 U CN212651583 U CN 212651583U
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Abstract
The utility model discloses a dual cycle formula active carbon separation analytic waste incineration flue gas processing system, this system including burn burning furnace, boiler, quench tower, dry-type deacidification tower, dust remover, hydrogen halide adsorption tower, SOx/NOx control tower, hydrogen halide analytic tower and the thermal regeneration analytic tower of active carbon. The utility model discloses different according to msw incineration flue gas flow and flue gas component, nimble design serial-type adsorbs analytic flow or parallel adsorbs analytic flow, and then realizes that preferential desorption hydrogen halide gas carries out the thermal desorption of other pollutants again, realizes the accurate desorption of multiple pollutant, prevents that equipment from corroding, improves operation security and stability, and the dioxin desorption is effectual simultaneously, and the active carbon loss is low, and the running cost is low.
Description
Technical Field
The utility model relates to a flue gas treatment facility technique, concretely relates to analytic msw incineration flue gas processing system of dual cycle formula active carbon separation belongs to flue gas purification technical field.
Background
The hazardous waste is various in types, complex in components, toxic, corrosive, flammable and explosive, has potential and lagging pollution, and is one of key and difficult problems of global environmental protection. With the development of socio-economy, the dangerous waste is no longer only a product of industrial production, and other sources include residential life, commercial structures, agricultural production, medical services, imperfect environmental protection facilities and the like, the yield of the dangerous waste is increased sharply, so that the dangerous waste treatment has a great market space.
Since the last century, China gradually began to apply incineration to hazardous wastes, which can effectively reduce the amount of hazardous wastes by destroying and changing the composition and structure of solid wastes at high temperature and rapidly dispose the hazardous wastes to a certain extent. The incineration device can realize the reduction and harmless disposal of hazardous wastes and simultaneously can realize the recovery and utilization of waste heat, but the concentration and the material content of incineration smoke have larger floating due to the various types, uncertainty of incoming materials and uncertainty of compatibility of hazardous wastes, so that the treatment difficulty of tail end is much greater than that of the same air volume in the general industry.
In the traditional process for treating incineration flue gas, the flue gas is discharged after sequentially passing through a quenching tower, a deacidification tower, a dust remover, a wet-type deacidification tower, a flue gas heater, an SCR heater and other working procedures, wherein the quenching tower is rapidly cooled to reduce the generation of dioxin and finish primary deacidification; the flue gas heater aims to heat the flue gas, so that the flue gas reaches the temperature required by the SCR reactor, and meanwhile, the flue gas is beneficial to discharge; the purpose of the SCR reactor is to remove NOx from the flue gas. The process can meet lower environmental protection standards, but has the following problems: and (1) the process is long, the operation and maintenance are difficult, the dioxin removal efficiency is limited, and the dioxin is not eliminated and is only transferred to the external ash discharge. (2) the energy consumption is large, the investment is high, the operating cost is high, the incineration heat is not effectively utilized, the water consumption is large, the moisture content in the discharged flue gas is high, and meanwhile, wastewater is generated; (3) the HCl concentration in the waste incineration flue gas is very high, and the Cl in the circulating liquid is controlled when wet deacidification is adopted-Concentration, the need to discharge large amounts of wastewater, increases the workload of wastewater treatment.
In the dry incineration flue gas treatment process, the boiler flue gas enters a deacidification tower to remove 80% of acid gas, then enters a bag-type dust remover to remove ash, then enters a draught fan to be pressurized, and is sent to an active carbon adsorption tower to be subjected to deashingSOx, HCl, HF, NOx and dioxin are removed, ammonia is added in front of the active carbon adsorption tower to improve the denitration effect, and the flue gas is discharged from a chimney after being purified. However, due to the particularity of the raw materials in the hazardous waste, the content of hydrogen halides (HCl, HF) in the flue gas is high (maximum > 1000 mg/Nm)3) The content of water vapor is high (30%), the acid dew point is high, the corrosivity is strong, the dust hygroscopicity is strong, the scale and hardening are easy, although the removal efficiency of the hydrogen halide can reach 80% after the treatment of the deacidification tower, the content of the hydrogen halide entering the activated carbon flue gas purification system is still high due to the high concentration of the original hydrogen halide, the exhaust temperature can be reduced below the acid dew point under the condition of lower temperature (130-.
SUMMERY OF THE UTILITY MODEL
To prior art not enough, the utility model designs a concentrate and adsorb, separately analytic msw incineration flue gas processing system and adopt this system to carry out the method that msw incineration flue gas handled. The utility model discloses the active carbon that will have adsorbed the pollutant takes the mode of priority getting rid of hydrogen halide, then carries out the desorption reaction of other pollutants again, can realize the accurate desorption of multiple pollutants such as dioxin, nitrogenous, sulphur, reduces technology operation load, prevents that analytic equipment from corroding, ensures the long-term high-efficient safety and stability operation of system.
In order to achieve the above object, the utility model discloses the technical scheme who adopts specifically as follows:
the utility model provides a dual cycle formula active carbon separation analytic waste incineration flue gas processing system, this system is including burning furnace, boiler, quench tower, dry-type deacidification tower, dust remover, SOx/NOx control tower, hydrogen halide analytic tower, active carbon thermal regeneration analytic tower and hydrogen halide adsorption tower. Wherein, the feed inlet of the incinerator is connected with a first pipeline. And according to the trend of the flue gas, the smoke outlet of the incinerator is directly connected with the boiler. And the smoke outlet of the boiler is connected to the smoke inlet of the quenching tower through a second pipeline or a third pipeline is led out from the second pipeline and is directly connected to a fourth pipeline. And the smoke outlet of the quenching tower is connected to the smoke inlet of the dry deacidification tower through a fourth pipeline. And the smoke outlet of the dry deacidification tower is connected to the smoke inlet of the dust remover through a fifth pipeline. And the smoke outlet of the dust remover is connected to the smoke inlet of the desulfurization and denitrification tower through a sixth pipeline. And the smoke outlet of the desulfurization and denitrification tower is communicated to the outside through a seventh pipeline. The hydrogen halide adsorption tower is arranged on a sixth pipeline, and a discharge port of the hydrogen halide adsorption tower is connected to a feed port of the hydrogen halide desorption tower through a fifth active carbon conveying pipeline. The discharge port of the hydrogen halide desorption tower is connected to the feed port of the activated carbon thermal regeneration desorption tower through a third activated carbon conveying pipeline and is connected to the feed port of the hydrogen halide desorption tower through a sixth activated carbon conveying pipeline. And the discharge port of the hydrogen halide desorption tower, the third active carbon conveying pipeline and the sixth active carbon conveying pipeline are connected through a three-way valve. And the discharge port of the desulfurization and denitrification tower is directly connected to the feed inlet of the activated carbon thermal regeneration desorption tower through a second activated carbon conveying pipeline. The discharge port of the activated carbon thermal regeneration desorption tower is connected to the feed port of the desulfurization and denitrification tower through a first activated carbon conveying pipeline, and a fourth activated carbon conveying pipeline is led out from the first activated carbon conveying pipeline and connected to the feed port of the hydrogen halide adsorption tower; 1-20 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower; and 1-20 hydrogen halide adsorption units are arranged in the hydrogen halide adsorption tower.
Preferably, an ammonia spraying device is further arranged at the outlet of the smoke inlet of the desulfurization and denitrification tower, and the ammonia spraying device is communicated with the sixth pipeline. 2-15 desulfurization and denitrification units, preferably 3-12 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower. The hydrogen halide adsorption tower is internally provided with 2-15 hydrogen halide adsorption units, preferably 3-12 hydrogen halide adsorption units.
Preferably, the system also comprises an activated carbon vibrating screen and an activated carbon powder recovery pipeline. The active carbon vibrating screen is arranged at a discharge outlet of the active carbon thermal regeneration desorption tower. One end of the activated carbon powder recovery pipeline is connected to the lower part of the activated carbon vibrating screen, and the other end of the activated carbon powder recovery pipeline is connected to a feed inlet of the incinerator.
Preferably, the lower part of the dry deacidification tower is also provided with an activated carbon powder conveying pipe and a lime powder conveying pipe. The upstream end of the activated carbon powder conveying pipe is communicated with an activated carbon powder recovery pipeline.
Preferably, the system also comprises an induced draft fan. And the induced draft fan is arranged on the sixth pipeline and is positioned at the upstream of the connection part of the hydrogen halide adsorption tower and the sixth pipeline.
Preferably, the second pipeline is provided with a flow detection device, a temperature detection device and a first valve. The first valve is located downstream of the junction of the third conduit and the second conduit. And a second valve is arranged on the third pipeline. And a third valve, a first concentration detection device, a second concentration detection device, a third concentration detection device and a fourth concentration detection device are arranged on the fourth pipeline. The third valve is positioned at the upstream of the joint of the third pipeline and the fourth pipeline, and the first concentration detection device, the second concentration detection device, the third concentration detection device and the fourth concentration detection device are all positioned at the downstream of the joint of the third pipeline and the fourth pipeline.
According to the utility model discloses a second embodiment provides an adopt first embodiment the waste incineration flue gas processing system based on active carbon separation is analytic carries out the method that the flue gas was handled, this method includes following step:
1) incineration waste materials are conveyed to an incinerator through a first pipeline for incineration treatment, and raw flue gas generated by incineration sequentially undergoes boiler heat exchange treatment, quenching tower cooling treatment, dry deacidification tower deacidification treatment, dust remover dust removal treatment and desulfurization and denitrification treatment of a desulfurization and denitrification tower. And discharging the purified flue gas subjected to desulfurization and denitrification treatment through a seventh pipeline. Or
The method comprises the following steps of sequentially carrying out boiler heat exchange treatment, quench tower cooling treatment, dry deacidification tower deacidification treatment, dust remover dedusting treatment, hydrogen halide adsorption tower adsorption deacidification treatment and desulfurization denitration tower desulfurization denitration treatment on raw flue gas generated by incineration. And discharging the purified flue gas subjected to desulfurization and denitrification treatment through a seventh pipeline.
2) The activated carbon subjected to thermal regeneration treatment by the activated carbon thermal regeneration desorption tower is conveyed to the desulfurization and denitrification tower through the first activated carbon conveying pipeline to perform desulfurization and denitrification treatment on the flue gas. And the activated carbon subjected to desulfurization and denitrification treatment is conveyed to an activated carbon thermal regeneration desorption tower through a second activated carbon conveying pipeline for thermal regeneration treatment. Meanwhile, a fourth activated carbon conveying pipeline is led out from the first activated carbon conveying pipeline and conveys the activated carbon subjected to thermal regeneration treatment to a hydrogen halide adsorption tower for adsorption deacidification treatment. And the activated carbon after the adsorption and deacidification treatment is conveyed to a hydrogen halide desorption tower through a fifth activated carbon conveying pipeline for hydrogen halide desorption treatment. And the activated carbon after the hydrogen halide removal treatment is conveyed to a feed inlet of the hydrogen halide adsorption tower through a sixth activated carbon conveying pipeline for continuous adsorption deacidification treatment or is directly conveyed to an activated carbon thermal regeneration desorption tower through a third activated carbon conveying pipeline for thermal regeneration treatment, and the steps are repeated. Meanwhile, the activated carbon powder screened out by the activated carbon vibrating screen is conveyed to an incinerator or a dry deacidification tower for reuse.
Preferably, the method further comprises: a flow detection device is arranged on the second pipeline for detecting the flow of the original flue gas in real time as q, Nm3H is used as the reference value. And a temperature detection device is also arranged for detecting the temperature t and the temperature DEG C of the original flue gas in real time.
Preferably, on the fourth duct L4 downstream of the junction of said third duct and fourth duct: the first concentration detection device is arranged to detect the concentration of HCl in the original flue gas to be c1, mg/Nm3. The second concentration detection device is also arranged to detect the concentration of HF in the original flue gas as c2, mg/Nm in real time3. A third concentration detection device is also arranged for detecting SO in the original flue gas in real time2Has a concentration of c3, mg/Nm3. A fourth concentration detection device is also arranged to detect the concentration of NOx in the original smoke in real time as c4, mg/Nm3。
Preferably, the system HCl emission concentration control index is set to c5, mg/Nm3. The HF discharge concentration control index of the system is set to c6, mg/Nm3. Setting System SO2The emission concentration control index was c7, mg/Nm3. The NOx emission concentration control index of the system is set to be c8 mg/Nm3. Then:
W1＝q*(c1(1-α1)-c5)/m1*10-9formula I.
W2＝q*(c2(1-α2)-c6)/m2*10-9Formula II.
W3＝q*(c3(1-α3)-c7)/m3*10-9Formula III.
W4＝q*(c4-c8)/m4*10-9Formula IV.
Wherein W1 is the circulation volume of the activated carbon needed by HCl removal of the system, t/h. W2 is the circulation volume of the activated carbon required by the HF removal of the system, t/h. W3 for removing SO from system2The required circulation amount of the activated carbon is t/h. W4 is the circulation volume of the activated carbon required by the system to remove NOx, t/h. Alpha 1 is the HCl removal rate of the dry acid removal tower. Alpha 2 is the HF eliminating rate of the dry acid eliminating tower. Alpha 3 is SO removal of dry type deacidification tower2And (4) rate. And m1 is the adsorption capacity of the carbon-based adsorption material to HCl, mg/g-AC. And m2 is the adsorption capacity of the carbon-based adsorption material to HF, mg/g-AC. m3 is SO of carbon-based adsorption material2The adsorption capacity of (b), mg/g-AC. And m4 is the NOx adsorption capacity of the carbon-based adsorption material, mg/g-AC.
Preferably, the adsorption efficiency of the carbon-based adsorbent for HCl is set to K1 in consideration of the influence of system environmental factors. The adsorption efficiency of the carbon-based adsorbent for HF was set to K2. Setting the carbon-based adsorption material to SO2The adsorption efficiency of (3) was K3. The adsorption efficiency of the carbon-based adsorbent for NOx was set to K4. Then:
formula I is converted to:
W1＝K1*q*(c1(1-α1)-c5)/m1*10-9formula V.
Formula II converts to:
W2＝K2*q*(c2(1-α2)-c6)/m2*10-9formula VI.
Formula III converts to:
W3＝K3*q*(c3(1-α3)-c7)/m3*10-9formula VII.
Formula IV converts to:
W4＝K4*q*(c4-c8)/m4*10-9formula VIII.
Preferably, K1 has a value in the range of 1 to 1.5, preferably 1 to 1.2.
Preferably, K2 has a value in the range of 1 to 1.5, preferably 1 to 1.2.
Preferably, K3 has a value in the range of 1 to 1.3, preferably 1 to 1.1.
Preferably, K4 has a value in the range of 1 to 1.3, preferably 1 to 1.1.
Preferably, when only the activated carbon desulfurization and denitrification tower is used for pollutant adsorption in the system, the total circulation amount of the activated carbon in the desulfurization and denitrification tower is as follows:
w5 ═ W1+ W2+ W3+ W4 formula IX.
When only the activated carbon desulfurization and denitrification tower is used for pollutant adsorption, the total circulating quantity of the activated carbon conveyed to the activated carbon desulfurization and denitrification tower by the activated carbon thermal regeneration desorption tower is regulated to be the calculated value W5, t/h of the formula IX.
Preferably, when the system simultaneously comprises the hydrogen halide adsorption tower and the desulfurization and denitrification tower for respectively adsorbing pollutants, the total circulation amount of the activated carbon of the hydrogen halide adsorption tower is as follows:
w6 ═ W1+ W2 formula X.
The total circulation amount of the activated carbon of the desulfurization and denitrification tower is as follows:
w7 ═ W3+ W4 formula XI.
When the system is provided with a hydrogen halide adsorption tower and a desulfurization and denitrification tower for respectively adsorbing pollutants, the total circulating quantity of the activated carbon conveyed to the hydrogen halide adsorption tower by the hydrogen halide desorption tower or the activated carbon thermal regeneration desorption tower is regulated to be the calculated value W6 t/h of the formula X. And adjusting the total circulating quantity of the activated carbon conveyed to the activated carbon desulfurization and denitrification tower by the activated carbon thermal regeneration desorption tower to be calculated value W7, t/h of formula XI.
In the existing wet flue gas treatment process, flue gas is rapidly cooled in a quench tower, so that the generation of dioxin is reduced, simultaneously, preliminary deacidification can be performed, then treatments such as deacidification, dust removal, dioxin removal and the like are further performed in a dry deacidification tower and a bag-type dust remover, then fine deacidification is realized in a wet deacidification tower, and then the temperature of the flue gas is raised through a flue gas heater, so that the flue gas reaches the temperature required by an SCR reactor, and the flue gas emission is facilitated. The purpose of the SCR reactor is to remove NOx from the flue gas. The process can meet lower environmental protection standards, but has the following problems: (1) the method has the advantages that the flow is long, the operation and maintenance are difficult, the dioxin removal efficiency is limited, and the dioxin is not eliminated but only transferred to the external ash discharge; (2) the energy consumption is large, the investment is high, the operating cost is high, the incineration heat is not effectively utilized, the water consumption is large, the moisture content in the discharged flue gas is high, and meanwhile, wastewater is generated; (3) the HCl concentration in the waste incineration flue gas is very high, and wet deacidification is adoptedIn order to control Cl in the circulating liquid-Concentration, the need to discharge large amounts of wastewater, increases the workload of wastewater treatment.
In the prior art, flue gas after waste incineration firstly enters an acid removal tower to remove 80% of acid gas, then enters a bag-type dust remover to remove ash, then enters a draught fan to pressurize, and is sent to an activated carbon adsorption tower to remove SOx, HCl, HF, NOx, dioxin and the like. In the process, pollutants such as SOx, HCl, HF and dioxin are adsorbed by activated carbon, and NOx is simultaneously catalyzed by NH added into the activated carbon3Reduction to H2O and N2. And the active carbon adsorbed with the pollutants is sent to an analytical tower for thermal desorption and regeneration for recycling. Meanwhile, dioxin adsorbed by the activated carbon is cracked at high temperature in the desorption tower, and SOx, HCl and HF are desorbed and released from the activated carbon in the desorption tower and are sent to the dry deacidification tower for deacidification again. Generally, if the concentration of nitrogen oxides in the incineration flue gas is too high, SNCR can also be used at the boiler site to lower the NOx concentration entering the flue gas cleaning system in advance. But because of the particularity of raw materials in the hazardous waste, the content of hydrogen halide (HCl and HF) in the incineration flue gas of the hazardous waste garbage is higher (the maximum content is more than 1000 mg/Nm)3) High water vapor content (30%), high acid dew point, high corrosion, high dust hygroscopicity, and easy scaling and hardening. Although the removal efficiency of the hydrogen halide can reach 80% after the treatment of the deacidification tower, the content of the hydrogen halide entering the activated carbon flue gas purification system is still higher due to the higher concentration of the original hydrogen halide, and the flue gas temperature can be reduced to be below the acid dew point under the condition of lower temperature (130-.
Generally, in order to more thoroughly release the pollutants (SO) adsorbed by the activated carbon2NOx, HCl, HF, dioxin, etc.), the thermal regeneration temperature of the activated carbon desorption tower is designed to be about 400 ℃, but the acid dew point is higher and the corrosivity is extremely strong due to the content of hydrogen halide in the flue gas and under the high water condition, so that the equipment is easily corroded; and if the activated carbon is used for resolving the heat of the towerThe raw temperature is designed to be low (for example, about 180 ℃), and pollutants adsorbed by the activated carbon cannot be completely resolved. Therefore the utility model discloses in, the design is earlier in the SOx/NOx control tower adsorbed the active carbon of pollutant carry out thermal desorption hydrogen halide through hydrogen halide desorption tower (SOx/NOx control tower, hydrogen halide desorption tower, active carbon thermal regeneration desorption tower are serial-type design), still contain higher hydrogen halide, SO among the flue gas component that gets into the hydrogen halide desorption tower2Water vapor, etc., and the active carbon adsorbing material filled in the hydrogen halide desorption tower preferentially adsorbs the halide to realize the fine removal of the hydrogen halide and the SO2And removing a small amount. And then the activated carbon after halide removal treatment is conveyed to an activated carbon regeneration desorption tower for thermal regeneration treatment, so that fresh regenerated activated carbon is obtained for recycling. The activated carbon powder generated in the flowing process of the activated tower can be sent to an incinerator as fuel after being screened by an activated carbon vibrating screen. Or the mixed solution is mixed with a desulfurizer of the dry deacidification tower and enters the deacidification tower to perform chemical reaction or chemical adsorption with acid gas or remove dioxin. And then or the dioxin or the residual acid gas is removed after the dioxin is introduced into the deacidification tower and before the bag-type dust remover, so that the comprehensive recycling of resources is realized.
The utility model discloses in, can also design and increase the hydrogen halide in the preferential absorption flue gas of hydrogen halide adsorption tower, then carry out SOx/NOx control processing again, meanwhile, the active carbon after the hydrogen halide adsorbs in the hydrogen halide adsorption tower completion flue gas is carried to the hydrogen halide analytic tower and is carried out thermal desorption hydrogen halide, and the active carbon that has adsorbed other pollutants in the SOx/NOx control tower then carries to carry out thermal regeneration in the active carbon regeneration analytic tower and handles (namely hydrogen halide adsorption tower, hydrogen halide analytic tower and SOx/NOx control tower, the active carbon regeneration analytic tower is the parallel design). Wherein, when the regeneration temperature of the hydrogen halide desorption tower is about 180 ℃, the activated carbon after hydrogen halide desorption is conveyed to the activated carbon regeneration desorption tower for thermal regeneration treatment (the part of the activated carbon adsorbs SO in addition to hydrogen halide)2Pollutants such as NOx and dioxin). When the designed regeneration temperature of the hydrogen halide desorption tower is about 400 ℃ at the lowest, the hydrogen halide desorption tower is thermally regeneratedThe active carbon can be directly circulated to the adsorption tower of the hydrogen halide adsorption tower for recycling, and does not need to be subjected to thermal regeneration treatment by the active carbon regeneration desorption tower, so that the abrasion consumption of the active carbon material is reduced.
The utility model discloses in, the bin outlet of hydrogen halide analysis tower is connected to the feed inlet of active carbon thermal regeneration analysis tower and is connected to the feed inlet of hydrogen halide analysis tower through sixth active carbon conveying pipeline through third active carbon conveying pipeline. And the discharge port of the hydrogen halide desorption tower, the third active carbon conveying pipeline and the sixth active carbon conveying pipeline are connected through a three-way valve. That is to say, the active carbon in the hydrogen halide desorption tower can be directly conveyed to the hydrogen halide adsorption tower for recycling when the adsorption task in the hydrogen halide adsorption tower can still be ensured after loss (mainly wear loss), and the conveying pipeline is not required to be increased to convey the active carbon to the active carbon regeneration desorption tower for uniform distribution, so that the conveying path of the active carbon can be effectively shortened, and the wear loss is reduced.
The utility model discloses in, the exhaust port of boiler is connected to the smoke inlet or the second pipeline of quench tower through the second pipeline and is drawn forth third pipeline lug connection to fourth pipeline. And meanwhile, a temperature detection device and a first valve are arranged on the second pipeline. The first valve is located downstream of the junction of the third conduit and the second conduit. And a second valve is arranged on the third pipeline. And a third valve is arranged on the fourth pipeline. The third valve is located upstream of the junction of the third conduit and the fourth conduit. Namely, detect former flue gas temperature through temperature-detecting device, when former flue gas temperature is higher, close the second valve, open first valve and third valve for the flue gas gets into the quench tower via the second pipeline and carries out cooling treatment, then carries to the dry-type deacidification tower via the fourth pipeline again and carries out deacidification. And when the temperature of the original flue gas is lower, the first valve and the third valve are closed, and the second valve is opened, so that the flue gas is directly conveyed to a dry-type deacidification tower through the third pipeline and the fourth pipeline for deacidification treatment. The temperature is higher or lower than the deacidification temperature of the dry deacidification tower, but the temperature in the flue gas is higher than the dew point temperature of the acid, so that the equipment is prevented from being corroded by the acid.
The present invention provides a method of operating a pipeline system, comprising: the first concentration detection device is arranged to detect the concentration of HCl in the original flue gas to be c1, mg/Nm3. The second concentration detection device is also arranged to detect the concentration of HF in the original flue gas as c2, mg/Nm in real time3. A third concentration detection device is also arranged for detecting SO in the original flue gas in real time2Has a concentration of c3, mg/Nm3. A fourth concentration detection device is also arranged to detect the concentration of NOx in the original smoke in real time as c4, mg/Nm3。
Further, the system HCl emission concentration control index is set to c5, mg/Nm3. The HF discharge concentration control index of the system is set to c6, mg/Nm3. Setting System SO2The emission concentration control index was c7, mg/Nm3. The NOx emission concentration control index of the system is set to be c8 mg/Nm3. Then:
W1＝q*(c1(1-α1)-c5)/m1*10-9formula I.
W2＝q*(c2(1-α2)-c6)/m2*10-9Formula II.
W3＝q*(c3(1-α3)-c7)/m3*10-9Formula III.
W4＝q*(c4-c8)/m4*10-9Formula IV.
Wherein W1 is the circulation volume of the activated carbon needed by HCl removal of the system, t/h. W2 is the circulation volume of the activated carbon required by the HF removal of the system, t/h. W3 for removing SO from system2The required circulation amount of the activated carbon is t/h. W4 is the circulation volume of the activated carbon required by the system to remove NOx, t/h. Alpha 1 is the HCl removal rate of the dry acid removal tower 4. Alpha 2 is the HF eliminating rate of the dry acid eliminating tower 4. Alpha 3 is SO removal of dry type deacidification tower 42And (4) rate. And m1 is the adsorption capacity of the carbon-based adsorption material to HCl, mg/g-AC. And m2 is the adsorption capacity of the carbon-based adsorption material to HF, mg/g-AC. m3 is SO of carbon-based adsorption material2The adsorption capacity of (b), mg/g-AC. And m4 is the NOx adsorption capacity of the carbon-based adsorption material, mg/g-AC.
In order to realize the accurate adsorption treatment of the smoke pollutants, the influence of system environmental factors is considered, and the adsorption efficiency of the carbon-based adsorption material on HCl is set to be K1. Setting the adsorption of the carbon-based adsorption material to HFThe efficiency was K2. Setting the carbon-based adsorption material to SO2The adsorption efficiency of (3) was K3. The adsorption efficiency of the carbon-based adsorbent for NOx was set to K4. Then:
formula I is converted to:
W1＝K1*q*(c1(1-α1)-c5)/m1*10-9formula V.
Formula II converts to:
W2＝K2*q*(c2(1-α2)-c6)/m2*10-9formula VI.
Formula III converts to:
W3＝K3*q*(c3(1-α3)-c7)/m3*10-9formula VII.
Formula IV converts to:
W4＝K4*q*(c4-c8)/m4*10-9formula VIII.
Wherein, the value range of K1 is 1-1.5, preferably 1-1.2. K2 has a value in the range of 1-1.5, preferably 1-1.2. The value range of K3 is 1-1.3, preferably 1-1.1. The value range of K4 is 1-1.3, preferably 1-1.1.
Preferably, when only the activated carbon desulfurization and denitrification tower is used for pollutant adsorption in the system, the total circulation amount of the activated carbon in the desulfurization and denitrification tower is as follows:
w5 ═ W1+ W2+ W3+ W4 formula IX.
When only the activated carbon desulfurization and denitrification tower is used for pollutant adsorption in the system, the total circulating quantity of the activated carbon conveyed to the activated carbon desulfurization and denitrification tower by the activated carbon thermal regeneration desorption tower 8 is regulated to be the calculated value W5, t/h of the formula IX.
Preferably, when the system simultaneously comprises the hydrogen halide adsorption tower and the desulfurization and denitrification tower for respectively adsorbing pollutants, the total circulation amount of the activated carbon of the hydrogen halide adsorption tower is as follows:
w6 ═ W1+ W2 formula X.
The total circulation amount of the activated carbon of the desulfurization and denitrification tower is as follows:
w7 ═ W3+ W4 formula XI.
When the system is provided with a hydrogen halide adsorption tower and a desulfurization and denitrification tower for respectively adsorbing pollutants, the total circulating quantity of the activated carbon conveyed to the hydrogen halide adsorption tower by the hydrogen halide desorption tower or the activated carbon thermal regeneration desorption tower is regulated to be the calculated value W6 t/h of the formula X. And adjusting the total circulating quantity of the activated carbon conveyed to the activated carbon desulfurization and denitrification tower by the activated carbon thermal regeneration desorption tower to be calculated value W7, t/h of formula XI.
The utility model discloses in, be provided with 1-20 SOx/NOx control units in the SOx/NOx control tower, preferably 2-15 SOx/NOx control units, preferably 3-12 SOx/NOx control units. The hydrogen halide adsorption tower is internally provided with 1 to 20 hydrogen halide adsorption units, preferably 2 to 15 hydrogen halide adsorption units, and preferably 3 to 12 hydrogen halide adsorption units.
Compared with the prior art, the utility model discloses a beneficial technological effect as follows:
1. waste incineration flue gas processing system can realize the accurate desorption of multiple pollutant according to pollutant characteristic and charcoal base material (active carbon) adsorption characteristic, reduce technology operation load.
2. Msw incineration flue gas processing system to under msw incineration flue gas high hydrogen halide content, the high water condition, the acid dew point is higher, corrosivity is extremely strong, take the thermal desorption of preferential desorption hydrogen halide gas carrying on other pollutants, can prevent that equipment from corroding, improve operation security and stability.
3. Msw incineration flue gas processing system for to the charcoal base material (active carbon) to adsorbing different pollutants, but realize the independent fine control regeneration of disconnect-type, reduce energy resource consumption, realize accessory substance kind simplification, help resource utilization, if dehydrohalogenation tower only produces hydrogen halide, the hot regeneration tower of active carbon only produces SO2。
4. Waste incineration flue gas processing system can all heat charcoal base adsorption material (active carbon) to more than 400 ℃ finally, realize dealing with the decomposition of dioxin.
5. Msw incineration flue gas processing system take independent conveying system with charcoal base adsorbing material (active carbon) after the analysis, can control adsorbing material's circulation volume respectively, reduce the material loss, reduce the running cost.
6. Waste incineration flue gas processing system can be according to the raw materials component difference, select different flue gas flows in a flexible way, different according to waste incineration flue gas flow and flue gas component promptly, the active carbon circulation volume of nimble control hydrogen halide adsorption tower and SOx/NOx control tower reduces the active carbon loss.
Drawings
FIG. 1 is a flow chart of a wet incineration flue gas treatment process in the prior art.
FIG. 2 is a flow chart of a dry incineration flue gas treatment process in the prior art.
Fig. 3 is the structure diagram of a waste incineration flue gas treatment system with dual cycle activated carbon separation and desorption.
Fig. 4 is a schematic structural diagram of a waste incineration flue gas treatment system with a dual cycle type activated carbon separation and desorption function and a detection mechanism.
Reference numerals: 1: an incinerator; 101: an incinerator ash discharge port; 2: a boiler; 3: a quench tower; 4: a dry deacidification tower; 401: an active carbon powder conveying pipe; 402: a lime powder conveying pipe; 5: a dust remover; 501: a dust discharging port of the dust remover; 6: a desulfurization and denitrification tower; 7: a hydrogen halide desorption column; 8: an activated carbon thermal regeneration desorption tower; 9: an ammonia injection device; 10: an induced draft fan; 11: an active carbon vibrating screen; 12: a hydrogen halide adsorption column; 13: a three-way valve; l1: a first conduit; l2: a second conduit; l3: a third pipeline; l4: a fourth conduit; l5: a fifth pipeline; l6: a sixth pipeline; l7: a seventh pipe; l8: an activated carbon powder recovery pipeline; s1: a first activated carbon delivery line; s2: a second activated carbon delivery line; s3: a third activated carbon delivery line; s4: a fourth activated carbon delivery line; s5: a fifth activated carbon delivery line; s6: a sixth activated carbon delivery line; q: a flow detection device; t: a temperature detection device; m1: a first valve; m2: a second valve; m3: a third valve; c1: a first concentration detection device; c2: a second concentration detection device; c3: a third concentration detection means; c4: and a fourth concentration detection means.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed invention includes but is not limited to the following embodiments.
A double-circulation type waste incineration flue gas treatment system for activated carbon separation and desorption comprises an incinerator 1, a boiler 2, a quench tower 3, a dry deacidification tower 4, a dust remover 5, a desulfurization and denitrification tower 6, a hydrogen halide desorption tower 7, an activated carbon thermal regeneration desorption tower 8 and a hydrogen halide adsorption tower 12. Wherein, the feed inlet of the incinerator 1 is connected with a first pipeline L1. According to the trend of the flue gas, the smoke outlet of the incinerator 1 is directly connected with the boiler 2. The smoke outlet of the boiler 2 is connected to the smoke inlet of the quenching tower 3 through a second pipeline L2 or a third pipeline L3 is led out of the second pipeline L2 and is directly connected to a fourth pipeline L4. The smoke outlet of the quenching tower 3 is connected to the smoke inlet of the dry deacidification tower 4 through a fourth pipeline L4. The smoke outlet of the dry deacidification tower 4 is connected to the smoke inlet of the dust remover 5 through a fifth pipeline L5. The smoke outlet of the dust remover 5 is connected to the smoke inlet of the desulfurization and denitrification tower 6 through a sixth pipeline L6. And the smoke outlet of the desulfurization and denitrification tower 6 is communicated to the outside through a seventh pipeline L7. The hydrogen halide adsorption column 12 is provided on the sixth conduit L6. The discharge port of the hydrogen halide adsorption column 12 is connected to the feed port of the hydrogen halide desorption column 7 through a fifth activated carbon transfer line S5. The discharge outlet of the hydrogen halide desorption tower 7 is connected to the feed inlet of the activated carbon thermal regeneration desorption tower 8 through a third activated carbon conveying pipeline S3 and is connected to the feed inlet of the hydrogen halide desorption tower 7 through a sixth activated carbon conveying pipeline S6. The discharge port of the hydrogen halide desorption tower 7, the third activated carbon conveying pipeline S3 and the sixth activated carbon conveying pipeline S6 are connected through a three-way valve 13. The discharge outlet of the desulfurization and denitrification tower 6 is directly connected to the feed inlet of the activated carbon thermal regeneration desorption tower 8 through a second activated carbon conveying pipeline S2. The discharge outlet of the activated carbon thermal regeneration desorption tower 8 is connected to the feed inlet of the desulfurization and denitrification tower 6 through a first activated carbon conveying pipeline S1, and meanwhile, a fourth activated carbon conveying pipeline S4 is led out from the first activated carbon conveying pipeline S1 and connected to the feed inlet of the hydrogen halide adsorption tower 12. And 1-20 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower 6. The hydrogen halide adsorption tower 12 is internally provided with 1 to 20 hydrogen halide adsorption units.
Preferably, an ammonia injection device 9 is further disposed at the outlet of the flue gas inlet of the desulfurization and denitrification tower 6, and the ammonia injection device 9 is communicated with a sixth pipeline L6. 2-15 desulfurization and denitrification units, preferably 3-12 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower 6. The hydrogen halide adsorption tower 12 is internally provided with 2 to 15 hydrogen halide adsorption units, preferably 3 to 12 hydrogen halide adsorption units.
Preferably, the system further comprises an activated carbon vibrating screen 11 and an activated carbon powder recovery pipeline L8. The activated carbon vibrating screen 11 is arranged at a discharge outlet of the activated carbon thermal regeneration desorption tower 8. One end of the activated carbon powder recycling pipeline L8 is connected to the lower part of the activated carbon vibrating screen 11, and the other end of the activated carbon powder recycling pipeline L8 is connected to the feed inlet of the incinerator 1.
Preferably, the dry deacidification tower 4 is further provided at a lower portion thereof with an activated carbon powder duct 401 and a lime powder duct 402. The upstream end of the activated carbon powder conveying pipe 401 is communicated with an activated carbon powder recycling pipeline L8.
Preferably, the system also comprises an induced draft fan 10. The induced draft fan 10 is disposed on the sixth pipeline L6 and upstream of the connection between the hydrogen halide adsorption tower 12 and the sixth pipeline L6.
Preferably, the second duct L2 is further provided with a flow rate detector Q, a temperature detector T, and a first valve M1. The first valve M1 is located downstream of the junction of the third line L3 and the second line L2.
Preferably, a second valve M2 is provided in the third line L3. The fourth pipeline L4 is provided with a third valve M3, a first concentration detection device C1, a second concentration detection device C2, a third concentration detection device C3 and a fourth concentration detection device C4. The third valve M3 is located upstream of the junction of the third line L3 and the fourth line L4.
Preferably, the fourth pipeline L4 is provided with a first concentration detection device C1, a second concentration detection device C2, a third concentration detection device C3 and a fourth concentration detection device C4. The first concentration detection device C1, the second concentration detection device C2, the third concentration detection device C3 and the fourth concentration detection device C4 are all located at the downstream of the connection position of the third pipeline L3 and the fourth pipeline L4.
Example 1
As shown in fig. 3, the system for treating waste incineration flue gas by using a dual cycle type activated carbon separation and desorption method includes an incinerator 1, a boiler 2, a quenching tower 3, a dry deacidification tower 4, a dust remover 5, a desulfurization and denitrification tower 6, a hydrogen halide desorption tower 7, an activated carbon thermal regeneration desorption tower 8, and a hydrogen halide adsorption tower 12. Wherein, the feed inlet of the incinerator 1 is connected with a first pipeline L1. According to the trend of the flue gas, the smoke outlet of the incinerator 1 is directly connected with the boiler 2. The smoke outlet of the boiler 2 is connected to the smoke inlet of the quenching tower 3 through a second pipeline L2 or a third pipeline L3 is led out of the second pipeline L2 and is directly connected to a fourth pipeline L4. The smoke outlet of the quenching tower 3 is connected to the smoke inlet of the dry deacidification tower 4 through a fourth pipeline L4. The smoke outlet of the dry deacidification tower 4 is connected to the smoke inlet of the dust remover 5 through a fifth pipeline L5. The smoke outlet of the dust remover 5 is connected to the smoke inlet of the desulfurization and denitrification tower 6 through a sixth pipeline L6. And the smoke outlet of the desulfurization and denitrification tower 6 is communicated to the outside through a seventh pipeline L7. The hydrogen halide adsorption column 12 is provided on the sixth conduit L6. The discharge port of the hydrogen halide adsorption column 12 is connected to the feed port of the hydrogen halide desorption column 7 through a fifth activated carbon transfer line S5. The discharge outlet of the hydrogen halide desorption tower 7 is connected to the feed inlet of the activated carbon thermal regeneration desorption tower 8 through a third activated carbon conveying pipeline S3 and is connected to the feed inlet of the hydrogen halide desorption tower 7 through a sixth activated carbon conveying pipeline S6. The discharge port of the hydrogen halide desorption tower 7, the third activated carbon conveying pipeline S3 and the sixth activated carbon conveying pipeline S6 are connected through a three-way valve 13. The discharge outlet of the desulfurization and denitrification tower 6 is directly connected to the feed inlet of the activated carbon thermal regeneration desorption tower 8 through a second activated carbon conveying pipeline S2. The discharge outlet of the activated carbon thermal regeneration desorption tower 8 is connected to the feed inlet of the desulfurization and denitrification tower 6 through a first activated carbon conveying pipeline S1, and meanwhile, a fourth activated carbon conveying pipeline S4 is led out from the first activated carbon conveying pipeline S1 and connected to the feed inlet of the hydrogen halide adsorption tower 12. And 1-20 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower 6. The hydrogen halide adsorption tower 12 is internally provided with 8 hydrogen halide adsorption units.
Example 2
Example 1 is repeated, except that an ammonia injection device 9 is further disposed at the outlet of the flue gas inlet of the desulfurization and denitrification tower 6, and the ammonia injection device 9 is communicated with a sixth pipeline L6. And 5 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower 6. The hydrogen halide adsorption tower 12 is provided with 5 hydrogen halide adsorption units therein.
Example 3
Example 2 was repeated except that the system further included an activated carbon vibrating screen 11 and an activated carbon powder recovery line L8. The activated carbon vibrating screen 11 is arranged at a discharge outlet of the activated carbon thermal regeneration desorption tower 8. One end of the activated carbon powder recycling pipeline L8 is connected to the lower part of the activated carbon vibrating screen 11, and the other end of the activated carbon powder recycling pipeline L8 is connected to the feed inlet of the incinerator 1.
Example 4
Example 3 is repeated except that an activated carbon powder delivery pipe 401 and a lime powder delivery pipe 402 are further provided at the lower portion of the dry deacidification tower 4. The upstream end of the activated carbon powder conveying pipe 401 is communicated with an activated carbon powder recycling pipeline L8.
Example 5
Example 4 is repeated except that the system also includes an induced draft fan 10. The induced draft fan 10 is disposed on the sixth pipeline L6 and upstream of the connection between the hydrogen halide adsorption tower 12 and the sixth pipeline L6.
Example 6
Example 5 is repeated except that the second pipe L2 is further provided with a flow rate detector Q, a temperature detector T, and a first valve M1. The first valve M1 is located downstream of the junction of the third line L3 and the second line L2.
Example 7
Example 6 is repeated except that the third pipe L3 is provided with a second valve M2. The fourth pipeline L4 is provided with a third valve M3, a first concentration detection device C1, a second concentration detection device C2, a third concentration detection device C3 and a fourth concentration detection device C4. The third valve M3 is located upstream of the junction of the third line L3 and the fourth line L4.
Example 8
Example 7 was repeated except that the fourth line L4 was provided with a first concentration detecting means C1, a second concentration detecting means C2, a third concentration detecting means C3 and a fourth concentration detecting means C4. The first concentration detection device C1, the second concentration detection device C2, the third concentration detection device C3 and the fourth concentration detection device C4 are all located at the downstream of the connection position of the third pipeline L3 and the fourth pipeline L4.
Claims (11)
1. The utility model provides a dual cycle formula active carbon separation analytic msw incineration flue gas processing system which characterized in that: the system comprises an incinerator (1), a boiler (2), a quench tower (3), a dry deacidification tower (4), a dust remover (5), a desulfurization and denitrification tower (6), a hydrogen halide desorption tower (7), an active carbon thermal regeneration desorption tower (8) and a hydrogen halide adsorption tower (12); wherein a first pipeline (L1) is connected with a feed inlet of the incinerator (1); according to the trend of the flue gas, the smoke outlet of the incinerator (1) is directly connected with the boiler (2); the smoke outlet of the boiler (2) is connected to the smoke inlet of the quenching tower (3) through a second pipeline (L2) or a third pipeline (L3) is led out from the second pipeline (L2) and is directly connected to a fourth pipeline (L4); the smoke outlet of the quenching tower (3) is connected to the smoke inlet of the dry deacidification tower (4) through a fourth pipeline (L4); the smoke outlet of the dry deacidification tower (4) is connected to the smoke inlet of the dust remover (5) through a fifth pipeline (L5); the smoke outlet of the dust remover (5) is connected to the smoke inlet of the desulfurization and denitrification tower (6) through a sixth pipeline (L6); the smoke outlet of the desulfurization and denitrification tower (6) is communicated to the outside through a seventh pipeline (L7); the hydrogen halide adsorption column (12) is disposed on a sixth piping (L6); the discharge outlet of the hydrogen halide adsorption tower (12) is connected to the feed inlet of the hydrogen halide desorption tower (7) through a fifth activated carbon conveying pipeline (S5); the discharge port of the hydrogen halide desorption tower (7) is connected to the feed port of the activated carbon thermal regeneration desorption tower (8) through a third activated carbon conveying pipeline (S3) and is connected to the feed port of the hydrogen halide desorption tower (7) through a sixth activated carbon conveying pipeline (S6); the discharge port of the hydrogen halide desorption tower (7), the third activated carbon conveying pipeline (S3) and the sixth activated carbon conveying pipeline (S6) are connected through a three-way valve (13); the discharge port of the desulfurization and denitrification tower (6) is directly connected to the feed port of the activated carbon thermal regeneration desorption tower (8) through a second activated carbon conveying pipeline (S2); the discharge outlet of the activated carbon thermal regeneration desorption tower (8) is connected to the feed inlet of the desulfurization and denitrification tower (6) through a first activated carbon conveying pipeline (S1), and a fourth activated carbon conveying pipeline (S4) is led out from the first activated carbon conveying pipeline (S1) and is connected to the feed inlet of the hydrogen halide adsorption tower (12); 1-20 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower (6); and 1-20 hydrogen halide adsorption units are arranged in the hydrogen halide adsorption tower (12).
2. The system of claim 1, wherein: an ammonia spraying device (9) is further arranged at the outlet of the smoke inlet of the desulfurization and denitrification tower (6), and the ammonia spraying device (9) is communicated with a sixth pipeline (L6); 2-15 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower (6); 2-15 hydrogen halide adsorption units are arranged in the hydrogen halide adsorption tower (12).
3. The system of claim 2, wherein: 3-12 desulfurization and denitrification units are arranged in the desulfurization and denitrification tower (6); and 3-12 hydrogen halide adsorption units are arranged in the hydrogen halide adsorption tower (12).
4. The system according to any one of claims 1-3, wherein: the system also comprises an activated carbon vibrating screen (11) and an activated carbon powder recovery pipeline (L8); the activated carbon vibrating screen (11) is arranged at a discharge outlet of the activated carbon thermal regeneration desorption tower (8); one end of the activated carbon powder recovery pipeline (L8) is connected to the lower part of the activated carbon vibrating screen (11), and the other end of the activated carbon powder recovery pipeline (L8) is connected to the feed inlet of the incinerator (1).
5. The system according to any one of claims 1-3, wherein: the lower part of the dry deacidification tower (4) is also provided with an activated carbon powder conveying pipe (401) and a lime powder conveying pipe (402); the upstream end of the activated carbon powder conveying pipe (401) is communicated with an activated carbon powder recovery pipeline (L8).
6. The system of claim 4, wherein: the lower part of the dry deacidification tower (4) is also provided with an activated carbon powder conveying pipe (401) and a lime powder conveying pipe (402); the upstream end of the activated carbon powder conveying pipe (401) is communicated with an activated carbon powder recovery pipeline (L8).
7. The system of claim 5, wherein: the system also comprises an induced draft fan (10); the induced draft fan (10) is arranged on the sixth pipeline (L6) and is positioned at the upstream of the connection position of the hydrogen halide adsorption tower (12) and the sixth pipeline (L6).
8. The system of claim 6, wherein: the system also comprises an induced draft fan (10); the induced draft fan (10) is arranged on the sixth pipeline (L6) and is positioned at the upstream of the connection position of the hydrogen halide adsorption tower (12) and the sixth pipeline (L6).
9. The system according to claim 7 or 8, characterized in that: the second pipeline (L2) is also provided with a flow detection device (Q), a temperature detection device (T) and a first valve (M1); the first valve (M1) is located downstream of the junction of the third conduit (L3) and the second conduit (L2).
10. The system of claim 9, wherein: a second valve (M2) is arranged on the third pipeline (L3); a third valve (M3), a first concentration detection device (C1), a second concentration detection device (C2), a third concentration detection device (C3) and a fourth concentration detection device (C4) are arranged on the fourth pipeline (L4); the third valve (M3) is located upstream of the connection of the third conduit (L3) and the fourth conduit (L4).
11. The system of claim 10, wherein: the first concentration detection device (C1), the second concentration detection device (C2), the third concentration detection device (C3) and the fourth concentration detection device (C4) are all located at the downstream of the connection position of the third pipeline (L3) and the fourth pipeline (L4).
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