CN113701174A - Anti-blocking combined process and system for high treatment efficiency of low-concentration VOC tail gas - Google Patents
Anti-blocking combined process and system for high treatment efficiency of low-concentration VOC tail gas Download PDFInfo
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- CN113701174A CN113701174A CN202111042126.1A CN202111042126A CN113701174A CN 113701174 A CN113701174 A CN 113701174A CN 202111042126 A CN202111042126 A CN 202111042126A CN 113701174 A CN113701174 A CN 113701174A
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- 238000000034 method Methods 0.000 title claims abstract description 40
- 230000008569 process Effects 0.000 title claims abstract description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 151
- 239000003546 flue gas Substances 0.000 claims abstract description 151
- 239000007789 gas Substances 0.000 claims abstract description 92
- 238000001816 cooling Methods 0.000 claims abstract description 72
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 41
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000002808 molecular sieve Substances 0.000 claims abstract description 41
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000010457 zeolite Substances 0.000 claims abstract description 41
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000002912 waste gas Substances 0.000 claims abstract description 30
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 29
- 238000001179 sorption measurement Methods 0.000 claims abstract description 27
- 238000003795 desorption Methods 0.000 claims abstract description 21
- 238000005338 heat storage Methods 0.000 claims abstract description 20
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 18
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 17
- 238000001035 drying Methods 0.000 claims abstract description 15
- 238000009835 boiling Methods 0.000 claims abstract description 13
- 239000005416 organic matter Substances 0.000 claims abstract description 10
- 238000002485 combustion reaction Methods 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 7
- 239000002918 waste heat Substances 0.000 claims abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 238000009825 accumulation Methods 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 238000000859 sublimation Methods 0.000 claims description 4
- 230000008022 sublimation Effects 0.000 claims description 4
- 230000033228 biological regulation Effects 0.000 claims description 3
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 230000002265 prevention Effects 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000005496 tempering Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 13
- 239000002245 particle Substances 0.000 abstract description 9
- 239000000779 smoke Substances 0.000 abstract description 5
- 150000001412 amines Chemical class 0.000 abstract description 4
- 230000002194 synthesizing effect Effects 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 230000018044 dehydration Effects 0.000 abstract 2
- 238000006297 dehydration reaction Methods 0.000 abstract 2
- 238000004220 aggregation Methods 0.000 abstract 1
- 230000002776 aggregation Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000003814 drug Substances 0.000 description 5
- 239000000575 pesticide Substances 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 206010016807 Fluid retention Diseases 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000010914 pesticide waste Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
- F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
- F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
- F23G7/068—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator using regenerative heat recovery means
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to an anti-blocking combined process and system for high treatment efficiency of low-concentration VOC tail gas, which comprises (1) low-concentration VOC tail gas pretreatment, (2) preheating, (3) RTO incineration, (4) high-temperature reverse combustion, (5) tail gas preheating and primary flue gas cooling of flue gas after incineration treatment, (6) secondary cooling of flue gas after primary cooling and cooling dehydration, (7) deacidifying of flue gas after secondary cooling, (8) heating and drying of flue gas after cooling and dehydration, and (9) adsorption of the flue gas in a zeolite molecular sieve for secondary organic matter removal. The invention circularly utilizes the low-temperature flue gas waste heat, improves the charging temperature of the waste gas, and reduces the adsorption and the bed-landing of high waste boiling substances in the charging waste gas on the heat storage bed, thereby reducing the desorption of the high waste boiling substances during the smoke discharge, simultaneously reducing the ammonia of the decomposition product of amine organic substances which is adsorbed on the heat storage bed and directly enters the hearth for decomposition, reducing the ammonia source for synthesizing ammonium salt, and reducing the blockage caused by the aggregation of ammonium salt particles on the heat storage bed layer.
Description
Technical Field
The invention relates to a VOC tail gas treatment process and a system, in particular to a low-concentration VOC tail gas treatment process and a system.
Background
The tail gas of the medicine and pesticide production device is generally condensed, absorbed, adsorbed or subjected to membrane separation to recover organic matters, and the recovered low-concentration VOC-containing tail gas is subjected to tail end treatment by a heat accumulating type incinerator (RTO system for short). The total treatment efficiency of the RTO system to organic matters can reach about 99 percent, so the RTO system is widely applied to tail gas treatment at the tail end of a medicine and pesticide production device.
The tail gas at the tail end of a medicine and pesticide production device is characterized by complex components, large fluctuation of gas flow and concentration and large corrosivity of smoke generated by burning. The main problems of the RTO system for treating the medicine and pesticide waste gas and tail gas are three. Firstly, the removal efficiency is limited, secondly, the corrosion problem is solved, thirdly, the heat storage bed layer is easily blocked by ammonium salt, the ammonium salt blockage aggravates the limitation of the removal efficiency, and the heat storage bed layer is blocked by the ammonium salt to cause the environmental protection device to be forced to stop to influence the preorder production operation.
Due to the improvement of the relevant environmental standard requirements, the internal control indexes of various pharmaceutical and pesticide production enterprises are continuously improved, and along with the extension of the types of the tail gas of the incinerator, the total efficiency of the RTO system is gradually 99 percent and can not meet the requirements. In addition, through research and analysis on RTO tail gas matched with hundreds of sets of medicine and pesticide production devices, more than 90% of incinerators have the phenomenon that more than 85% of residual organic matters in flue gas are organic matters with the boiling points of 100-150 ℃ and the organic matters with the boiling points lower than 100 ℃ only account for about 10%; the sublimation temperature of the substances which are accumulated in the heat storage body and cause the blockage is generally 150-250 ℃.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to overcome the defects in the prior art and provide an anti-blocking combined process and system with high treatment efficiency of low-concentration VOC tail gas, which circularly utilize the waste heat of low-temperature flue gas, improve the charging temperature of the waste gas, reduce the adsorption bed of high-waste-boiling-point substances in the charging waste gas on a heat storage bed, thereby reducing the blockage caused by the accumulation of ammonium salt particles on the heat storage bed layer by desorbing the high-waste-boiling-point substances during smoke discharge, improving the charging temperature of the waste gas, reducing the ammonia of the decomposition product of amine organic substances which is adsorbed on the heat storage bed layer and directly enters a hearth for decomposition, reducing the ammonia source for synthesizing ammonium salt, adopting forced circulation of high-temperature flue gas to sublimate the ammonium salt particles accumulated in the heat storage bed layer and send the ammonium salt particles into the hearth for combustion and decomposition, preventing the regeneration of the ammonium salt, adopting a zeolite molecular sieve to adsorb the flue gas after being burned and cooled, removing secondary organic substances from the flue gas after being burned, and meeting the requirement that the total removal efficiency of the organic substances reaches more than 99.8 percent, the zeolite molecular sieve adsorbing the organic matters is desorbed again in a high-temperature desorption mode, tail gas generated by desorption is combined and incinerated, the zeolite molecular sieve is recycled, and no secondary pollutants are generated in the system.
The technical scheme is as follows: in order to solve the technical problems, the anti-blocking combination process with high treatment efficiency for the low-concentration VOC tail gas comprises the following steps,
(1) collecting and pretreating low-concentration VOC tail gas to ensure that the concentration of the tail gas meets the requirement of being less than 10g/Nm of incineration treatment of an RTO incinerator3；
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in the subsequent step;
(3) preheating the tail gas, and then sending the preheated tail gas into an RTO incinerator for incineration treatment, and removing organic matters in the tail gas at one time, wherein the removal rate is more than 99%, and the temperature of flue gas subjected to incineration treatment by the RTO incinerator is about 120-180 ℃;
(4) the method is characterized in that a high-temperature fan is adopted to lead back-burning flue gas from a hearth and a furnace bottom of the RTO incinerator in proportion, wherein the flue gas in the hearth is as follows: the ratio of the flue gas at the bottom of the furnace is 1:3, the temperature of the back-burning flue gas at the inlet of the high-temperature fan is 280-300 ℃, the back-burning flue gas is sent into a heat accumulation bed layer of the RTO incinerator by the high-temperature fan, the ammonium salt accumulated in the back-burning flue gas is sublimated and is primarily decomposed into ammonia and free acid, the ammonia is sent into a hearth of the RTO incinerator to be decomposed into nitrogen and water vapor, the heat generated by the decomposition of the ammonia during the back burning meets the back-burning heat supply requirement, and the back burning does not increase the fuel consumption;
(5) preheating tail gas of 120-180 ℃ flue gas subjected to incineration treatment by an RTO incinerator, recovering heat in the flue gas, and performing primary cooling on the flue gas, wherein the temperature after the primary cooling is 70-130 ℃;
(6) exchanging heat between the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling and dewatering for secondary cooling, wherein the temperature after secondary cooling is 55-110 ℃;
(7) deacidifying the flue gas subjected to secondary temperature reduction, wherein a deacidification tower is matched with the flue gas subjected to cooling and dewatering, and the temperature of the flue gas subjected to cooling and dewatering is 40 ℃;
(8) the flue gas at 40 ℃ after cooling and dewatering exchanges heat with the flue gas after primary cooling to be heated and dried, the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) the flue gas with the temperature of 50 ℃ after being heated and dried enters a zeolite molecular sieve for adsorption to remove secondary organic matters, the organic matters with the boiling point of 100-150 ℃ are secondarily removed, the secondary organic matter removal efficiency is about 80%, and after the flue gas is incinerated in an RTO incinerator and the zeolite molecular sieve organic matters are secondarily removed, the total organic matter removal efficiency of the system is more than 99.8%;
(10) desorbing the zeolite molecular sieve after the zeolite molecular sieve is saturated in adsorption, wherein the desorption adopts high-temperature air at 150-200 ℃, the temperature of tail gas generated by desorption of the zeolite molecular sieve is about 100 ℃, and the tail gas generated by desorption is merged into the furnace-entering tail gas of the RTO incinerator for cyclic treatment.
Further, the pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration regulation, tempering prevention and safety interlocking of the waste gas.
Further, in the step (2) and the step (5), a heat exchanger is adopted for tail gas preheating and flue gas cooling to achieve waste heat recovery, the temperature of the tail gas at the cold side is about 70 ℃, and the temperature of the tail gas at the hot side is 70-130 ℃ after cooling.
Further, in the step (3), the used RTO incinerator is a box-type heat accumulating incinerator, the high-temperature oxidation temperature is 800-900 ℃, the removal efficiency is 99%, in addition, the temperature of the tail gas at the inlet of the step (3) is about 70 ℃, and the temperature of the generated flue gas is 120-180 ℃.
Further, in the step (4), the temperature of the flue gas used for back burning is necessarily higher than the sublimation decomposition temperature of the ammonium salt possibly generated by the system, so as to ensure the decomposition of the ammonium salt.
Further, in the step (6) and the step (8), the heat exchanger is adopted to perform secondary cooling of the flue gas and heating and drying of the cooling water-removing flue gas, the secondary cooling temperature of the flue gas is 55-110 ℃, and the temperature after drying is about 50 ℃.
An anti-blocking combined system with high treatment efficiency for low-concentration VOC tail gas sequentially comprises a waste gas pretreatment device used in a process step (1), a tail gas preheating and flue gas primary cooler used in process steps (2) and (5), an RTO incinerator used in a process step (3), a flue gas secondary cooler used in process steps (6) and (8), a flue gas cooling and deacidifying device used in a process step (7) and a zeolite molecular sieve adsorption device used in a process step (9), wherein the waste gas pretreatment device is connected with one end of the tail gas preheating and flue gas primary cooler through a waste gas main fan, flue gas subjected to incineration treatment by the RTO incinerator is connected with the other end of the tail gas preheating and flue gas primary cooler through a pipeline, a hearth and a furnace bottom of the RTO incinerator are connected with one end of a high-temperature back-burning fan through pipelines, the other end of the high-temperature back-burning fan is connected with a heat storage bed layer of the RTO incinerator through a pipeline, and an induced draft fan I is arranged between the flue gas secondary cooler and the zeolite molecular sieve adsorption device, and an induced draft fan II is arranged between the zeolite molecular sieve adsorption device and the front end of the waste gas main fan.
Further, the tail gas preheating and flue gas primary cooler and the flue gas secondary cooler are both heat exchangers.
Further, the flue gas burned by the RTO incinerator sequentially passes through a tail gas preheating and flue gas primary cooler cooling end, a flue gas secondary cooler cooling end, a flue gas cooling and deacidifying device, a flue gas secondary cooler heating end and a zeolite molecular sieve adsorption device.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: the waste heat of low-temperature flue gas is recycled, the charging temperature of the waste gas is improved, the adsorption bed of high-waste-boiling-point substances in the charging waste gas on a heat storage bed is reduced, so that desorption of the high-waste-boiling-point substances during smoke discharge is reduced, the charging temperature of the waste gas is improved, ammonia of decomposition products of amine organic matters is reduced, ammonia is adsorbed on the heat storage bed and directly enters a hearth to be decomposed, an ammonia source for synthesizing ammonium salt is reduced, blockage caused by accumulation of ammonium salt particles on the heat storage bed is reduced, forced circulation of the high-temperature flue gas is adopted, the ammonium salt particles accumulated in the heat storage bed are sublimated and sent to the hearth to be combusted and decomposed, ammonium salt regeneration is prevented, the zeolite molecular sieve is adopted to adsorb the flue gas after incineration and cooling, secondary organic matters are removed from the incinerated flue gas, the total organic matter removal efficiency is over 99.8 percent, the zeolite molecular sieve adsorbing the organic matters is desorbed again in a high-temperature desorption mode, and the desorbed tail gas is merged and sent to be incinerated, the zeolite molecular sieve is recycled, no secondary pollutant is generated in the system, and residual organic matters with boiling points of 100-150 ℃ in the flue gas can be effectively removed.
Drawings
FIG. 1 is a schematic view of a process system of the present invention.
Detailed Description
The invention is further described below with reference to the figures and examples.
The invention relates to an anti-blocking combined process with high treatment efficiency for low-concentration VOC tail gas, which comprises the following steps,
(1) collecting and pretreating low-concentration VOC tail gas to ensure that the concentration of the VOC tail gas meets the requirement of being less than 10g/Nm of incineration treatment of an RTO furnace3；
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in a subsequent process;
(3) preheating the tail gas, and then sending the tail gas into an RTO furnace for incineration treatment to remove organic matters in the tail gas for one time, wherein the removal rate is more than 99%, and the temperature of flue gas subjected to incineration treatment in the RTO furnace is about 120-180 ℃;
(4) the high-temperature fan is adopted to lead back-burning flue gas from an RTO hearth and a furnace bottom in proportion, wherein the flue gas in the hearth is as follows: the ratio of the furnace bottom flue gas is 1:3, the temperature of the back-burning flue gas at the inlet of the high-temperature fan is ensured to be about 280-300 ℃, the back-burning flue gas is sent into a regenerative bed layer of the RTO furnace by the high-temperature fan, the ammonium salt accumulated in the back-burning flue gas is sublimated and is primarily decomposed into ammonia and free acid, the ammonia is sent into a hearth of the RTO furnace to be decomposed into nitrogen and water vapor, and one element generated by the ammonium salt is eliminated;
(5) preheating tail gas of 120-180 ℃ flue gas subjected to incineration treatment by an RTO furnace, recovering heat in the flue gas, and performing primary cooling on the flue gas, wherein the temperature after the primary cooling is 70-130 ℃;
(6) exchanging heat between the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling and dewatering for secondary cooling, wherein the temperature after secondary cooling is about 55-110 ℃;
(7) deacidifying the flue gas subjected to secondary temperature reduction, wherein a deacidification tower is matched with the flue gas subjected to cooling and dewatering, and the temperature of the flue gas subjected to cooling and dewatering is 40 ℃;
(8) the flue gas at 40 ℃ after cooling and dewatering exchanges heat with the flue gas after primary cooling to be heated and dried, the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) enabling 50 ℃ flue gas after temperature rise and drying to enter a zeolite molecular sieve for adsorption to remove secondary organic matters, and secondarily removing the organic matters with the boiling point of 100-150 ℃, wherein the secondary organic matter removal efficiency is about 80%, and after RTO incineration and secondary zeolite molecular sieve organic matter removal, the total organic matter removal efficiency of the system is more than 99.8%;
(10) desorbing the zeolite molecular sieve after the zeolite molecular sieve is saturated in adsorption, wherein the desorption adopts high-temperature air at 150-200 ℃, the temperature of tail gas generated by desorption of the zeolite molecular sieve is about 100 ℃, and the tail gas generated by desorption is merged into the furnace-entering tail gas of the RTO incinerator for cyclic treatment.
The pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration regulation, tempering prevention and safety interlocking of the waste gas, so that the safety of the tail gas is ensured.
In the step (2) and the step (5), the heat exchanger is adopted to preheat tail gas and cool the flue gas to achieve the effect of waste heat recovery, the temperature of the tail gas at the cold side is about 70 ℃ after preheating, the temperature of the tail gas at the hot side of the flue gas is 70-130 ℃ after cooling, and the material of the heat exchanger is selected according to the characteristics of the waste gas and the flue gas.
In the step (3), the used RTO incinerator is a traditional box-type heat accumulating type incinerator, the removal principle is high-temperature oxidation decomposition, the high-temperature oxidation temperature is 800-900 ℃, the removal efficiency is 99%, and the heat accumulating type incinerator comprises a complete set of equipment such as a matched combustor, an instrument, a valve and automatic control. And (3) the temperature of the inlet tail gas in the step (3) is about 70 ℃, and the temperature of the generated flue gas is 120-170 ℃.
In the step (4), the temperature of the flue gas used for back combustion is necessarily higher than the sublimation decomposition temperature of the ammonium salt possibly generated by the system, so as to ensure the decomposition of the ammonium salt, a fan used for back combustion must meet the requirements of corrosion resistance and temperature resistance of working conditions, the back combustion is automatically started or manually started according to the pressure difference condition of the RTO incinerator, and the back combustion procedure comprises cooling and safety interlocking.
In the step (6) and the step (8), the heat exchanger is adopted to perform secondary cooling of the flue gas and heating and drying of the cooling and dewatering flue gas, the secondary cooling temperature of the flue gas is 55-110 ℃, the temperature after drying is about 50 ℃, and the material of the heat exchanger is selected according to the characteristics of the flue gas on two sides.
The flue gas cooling effect of the step (6) is to reduce the cooling load in the step (7); and (4) the drying and heating function of the step (8) is to reduce the saturation of the flue gas water vapor in the step (7) and prevent the condensed free water from influencing the adsorption efficiency of the zeolite molecular sieve in the step (9).
In the step (7), the deacidification treatment is a cooling and temperature-reducing deacidification process of a traditional RTO system, a deacidification tower is matched for cooling and dewatering, the temperature of the flue gas after cooling and dewatering is 40 ℃, and the purpose of cooling and dewatering is to reduce the water retention of the flue gas.
The zeolite molecular sieve used in the step (9) is an inorganic porous novel material, the firing temperature is 500-600 ℃, high-temperature thermal desorption at 200-350 ℃ can be adopted, and the zeolite molecular sieve adsorption device is suitable for adsorbing high-boiling organic matters with the boiling point of 100-200 ℃, the step (9) is an independent zeolite molecular sieve adsorption device, the adsorption and desorption are switched automatically according to the on-line monitoring data of flue gas emission, and the waste gas generated by desorption is merged into the inlet of a main waste gas fan through a desorption fan and is sent into an RTO furnace for secondary incineration.
As shown in figure 1, the anti-blocking combined system for high treatment efficiency of low-concentration VOC tail gas sequentially comprises a waste gas pretreatment device 1 used in a process step (1), a tail gas preheating and flue gas primary cooler 2 used in process steps (2) and (5), an RTO incinerator 3 used in process step (3), a flue gas secondary cooler 4 used in process steps (6) and (8), a flue gas cooling and deacidifying device 5 used in process step (7) and a zeolite molecular sieve adsorption device 6 used in process step (9), wherein the tail gas preheating and flue gas primary cooler 2 and the flue gas secondary cooler 4 are heat exchangers, the waste gas pretreatment device 1 is connected with one end of the tail gas preheating and flue gas primary cooler 2 through a waste gas main fan 7, and flue gas incinerated by the RTO incinerator 3 sequentially passes through a tail gas preheating and flue gas primary cooler 2 cooling end, a cooling end and a cooling end, 4 cooling ends of flue gas aftercooler, flue gas cooling deacidification device 5, 4 temperature rise ends of flue gas aftercooler and zeolite molecular sieve adsorption equipment 6, the furnace and the stove bottom that RTO burnt burning furnace 3 all link to each other with 8 one ends of high temperature anti-fan that burns through the pipeline, 8 other ends of high temperature anti-fan that burns link to each other with the heat accumulation bed that RTO burnt furnace 3 through the pipeline be equipped with draught fan I9 between flue gas aftercooler 4 and the zeolite molecular sieve adsorption equipment 6 be equipped with draught fan II 10 between zeolite molecular sieve adsorption equipment 6 and the 7 front ends of waste gas main air fan.
The invention circularly utilizes the waste heat of low-temperature flue gas, improves the charging temperature of the waste gas, reduces the adsorption and the implantation of high waste boiling substances in the charging waste gas on the heat storage bed, thereby reducing the desorption of the high waste boiling substances during smoke discharge, improving the charging temperature of the waste gas, reducing the ammonia of the decomposition product of amine organic matters which is adsorbed on the heat storage bed and directly enters a hearth for decomposition, reducing the ammonia source for synthesizing ammonium salt, reducing the blockage caused by the accumulation of ammonium salt particles on the heat storage bed, adopting the forced circulation of the high-temperature flue gas to sublimate the ammonium salt particles accumulated in the heat storage bed and send the ammonium salt particles into the hearth for combustion and decomposition, preventing the regeneration of the ammonium salt, adopting the zeolite molecular sieve to adsorb the flue gas after incineration and cooling, removing secondary organic matters from the incinerated flue gas, meeting the requirement that the total removal efficiency of the organic matters reaches more than 99.8 percent, and adopting the high-temperature desorption mode of the zeolite molecular sieve adsorbing the organic matters, the tail gas generated by desorption is combined and sent to incineration for incineration, the zeolite molecular sieve is recycled, no secondary pollutant is generated in the system, and the residual organic matter with the boiling point of 100-150 ℃ in the flue gas can be effectively removed.
The present invention provides a thought and a method, and a method and a way for implementing the technical scheme are many, the above is only a preferred embodiment of the present invention, it should be noted that, for a person skilled in the art, a plurality of improvements and modifications can be made without departing from the principle of the present invention, and the improvements and modifications should be regarded as the protection scope of the present invention, and each component not explicitly described in the embodiment can be implemented by the prior art.
Claims (9)
1. The utility model provides a low concentration VOC tail gas high treatment efficiency prevent stifled combination technology which characterized in that: which comprises the following steps of,
(1) collecting and pretreating low-concentration VOC tail gas to ensure that the concentration of the tail gas meets the requirement of being less than 10g/Nm of incineration treatment of an RTO incinerator3；
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in the subsequent step;
(3) preheating the tail gas, and then sending the preheated tail gas into an RTO incinerator for incineration treatment, and removing organic matters in the tail gas at one time, wherein the removal rate is more than 99%, and the temperature of flue gas subjected to incineration treatment by the RTO incinerator is about 120-180 ℃;
(4) the method is characterized in that a high-temperature fan is adopted to lead back-burning flue gas from a hearth and a furnace bottom of the RTO incinerator in proportion, wherein the flue gas in the hearth is as follows: the ratio of the flue gas at the bottom of the furnace is 1:3, the temperature of the back-burning flue gas at the inlet of the high-temperature fan is 280-300 ℃, the back-burning flue gas is sent into a heat accumulation bed layer of the RTO incinerator by the high-temperature fan, the ammonium salt accumulated in the back-burning flue gas is sublimated and is primarily decomposed into ammonia and free acid, the ammonia is sent into a hearth of the RTO incinerator to be decomposed into nitrogen and water vapor, the heat generated by the decomposition of the ammonia during the back burning meets the back-burning heat supply requirement, and the back burning does not increase the fuel consumption;
(5) preheating tail gas of 120-180 ℃ flue gas subjected to incineration treatment by an RTO incinerator, recovering heat in the flue gas, and performing primary cooling on the flue gas, wherein the temperature after the primary cooling is 70-130 ℃;
(6) exchanging heat between the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling and dewatering for secondary cooling, wherein the temperature after secondary cooling is 55-110 ℃;
(7) deacidifying the flue gas subjected to secondary temperature reduction, wherein a deacidification tower is matched with the flue gas subjected to cooling and dewatering, and the temperature of the flue gas subjected to cooling and dewatering is 40 ℃;
(8) the flue gas at 40 ℃ after cooling and dewatering exchanges heat with the flue gas after primary cooling to be heated and dried, the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) the flue gas with the temperature of 50 ℃ after being heated and dried enters a zeolite molecular sieve for adsorption to remove secondary organic matters, the organic matters with the boiling point of 100-150 ℃ are secondarily removed, the secondary organic matter removal efficiency is about 80%, and after the flue gas is incinerated in an RTO incinerator and the zeolite molecular sieve organic matters are secondarily removed, the total organic matter removal efficiency of the system is more than 99.8%;
(10) desorbing the zeolite molecular sieve after the zeolite molecular sieve is saturated in adsorption, wherein the desorption adopts high-temperature air at 150-200 ℃, the temperature of tail gas generated by desorption of the zeolite molecular sieve is about 100 ℃, and the tail gas generated by desorption is merged into the furnace-entering tail gas of the RTO incinerator for cyclic treatment.
2. The high treatment efficiency anti-clogging combination process for low-concentration VOC tail gas according to claim 1, characterized in that: the pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration regulation, tempering prevention and safety interlocking of waste gas.
3. The high treatment efficiency anti-clogging combination process for low-concentration VOC tail gas according to claim 1, characterized in that: and (2) preheating tail gas and cooling the flue gas by using a heat exchanger to recover waste heat, wherein the temperature of the preheated tail gas at a cold side is about 70 ℃, and the temperature of the cooled tail gas at a hot side is 70-130 ℃.
4. The high treatment efficiency anti-clogging combination process for low-concentration VOC tail gas according to claim 1, characterized in that: in the step (3), the used RTO incinerator is a box-type heat accumulating type incinerator, the high-temperature oxidation temperature is 800-900 ℃, the removal efficiency is 99%, the highest allowable input waste gas VOC concentration is 10g/Nm3, in addition, the temperature of the tail gas at the inlet of the step (3) is about 70 ℃, and the temperature of the generated flue gas is 120-180 ℃.
5. The high treatment efficiency anti-clogging combination process for low-concentration VOC tail gas according to claim 1, characterized in that: in the step (4), the temperature of the flue gas used for back burning is necessarily higher than the sublimation decomposition temperature of the ammonium salt possibly generated by the system, so as to ensure the decomposition of the ammonium salt.
6. The high treatment efficiency anti-clogging combination process for low-concentration VOC tail gas according to claim 1, characterized in that: and (6) and (8) performing secondary cooling of the flue gas and heating and drying of the cooling and dewatering flue gas by using a heat exchanger, wherein the secondary cooling temperature of the flue gas is 55-110 ℃, the temperature after drying is about 50 ℃, and the humidity of the dried flue gas is less than 60%.
7. The high treatment efficiency anti-clogging combination system for low concentration VOC tail gas according to claim 1, wherein: the method comprises a waste gas pretreatment device (1) used in a process step (1), a tail gas preheating and flue gas primary cooler (2) used in the process steps (2) and (5), an RTO incinerator (3) used in the process step (3), a flue gas secondary cooler (4) used in the process steps (6) and (8), a flue gas cooling deacidification device (5) used in the process step (7) and a zeolite molecular sieve adsorption device (6) used in the process step (9), wherein the waste gas pretreatment device (1) is connected with one end of the tail gas preheating and flue gas primary cooler (2) through a waste gas main fan (7), flue gas subjected to incineration treatment by the RTO incinerator (3) is connected with the other end of the tail gas preheating and flue gas primary cooler (2) through a pipeline, a hearth and a furnace bottom of the RTO incinerator (3) are both connected with one end of a high-temperature back-burning fan (8) through a pipeline, the other end of the high-temperature reverse combustion fan (8) is connected with a heat storage bed layer of the RTO incinerator (3) through a pipeline, an induced draft fan I (9) is arranged between the flue gas secondary cooler (4) and the zeolite molecular sieve adsorption device (6), and an induced draft fan II (10) is arranged between the zeolite molecular sieve adsorption device (6) and the front end of the waste gas main fan (7).
8. The high treatment efficiency anti-clogging combination system for low concentration VOC tail gas of claim 7, wherein: the tail gas preheating and flue gas primary cooler (2) and the flue gas secondary cooler (4) are both heat exchangers.
9. The low-concentration VOC off-gas high treatment efficiency anti-clogging combination system as claimed in claim 7 or 8, wherein: the flue gas incinerated by the RTO incinerator (3) sequentially passes through a tail gas preheating and flue gas primary cooler (2) cooling end, a flue gas secondary cooler (4) cooling end, a flue gas cooling deacidification device (5), a flue gas secondary cooler (4) heating end and a zeolite molecular sieve adsorption device (6).
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| CN202111042126.1A CN113701174B (en) | 2021-09-07 | Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas |
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| CN117231993A (en) * | 2023-11-01 | 2023-12-15 | 江苏大信环境科技有限公司 | Anti-corrosion anti-blocking RTO system for fine chemical tail gas |
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