CN113701174B - Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas - Google Patents
Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas Download PDFInfo
- Publication number
- CN113701174B CN113701174B CN202111042126.1A CN202111042126A CN113701174B CN 113701174 B CN113701174 B CN 113701174B CN 202111042126 A CN202111042126 A CN 202111042126A CN 113701174 B CN113701174 B CN 113701174B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- temperature
- tail gas
- cooling
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 45
- 230000008569 process Effects 0.000 title claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 134
- 239000003546 flue gas Substances 0.000 claims abstract description 130
- 239000007789 gas Substances 0.000 claims abstract description 92
- 238000001816 cooling Methods 0.000 claims abstract description 62
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 39
- 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 39
- 239000010457 zeolite Substances 0.000 claims abstract description 39
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000002808 molecular sieve Substances 0.000 claims abstract description 33
- 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 33
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 29
- 238000003795 desorption Methods 0.000 claims abstract description 24
- 239000002912 waste gas Substances 0.000 claims abstract description 24
- 238000005338 heat storage Methods 0.000 claims abstract description 23
- 238000001179 sorption measurement Methods 0.000 claims abstract description 22
- 238000001035 drying Methods 0.000 claims abstract description 21
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 19
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 17
- 238000009835 boiling Methods 0.000 claims abstract description 17
- 239000000779 smoke Substances 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 13
- 239000002918 waste heat Substances 0.000 claims abstract description 7
- 239000005416 organic matter Substances 0.000 claims description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 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 6
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000000859 sublimation Methods 0.000 claims description 4
- 230000008022 sublimation Effects 0.000 claims description 4
- 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
- 238000007781 pre-processing Methods 0.000 claims description 3
- 230000002265 prevention Effects 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000005496 tempering Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 17
- 239000002245 particle Substances 0.000 abstract description 9
- 239000002699 waste material Substances 0.000 abstract description 8
- 150000001412 amines Chemical class 0.000 abstract description 4
- 238000002485 combustion reaction Methods 0.000 abstract description 4
- 238000002513 implantation Methods 0.000 abstract description 4
- 230000002194 synthesizing effect Effects 0.000 abstract description 4
- 230000002776 aggregation Effects 0.000 abstract description 2
- 238000004220 aggregation Methods 0.000 abstract description 2
- 239000003814 drug Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000000575 pesticide Substances 0.000 description 6
- 230000006872 improvement Effects 0.000 description 5
- 238000009825 accumulation Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 206010016807 Fluid retention Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
Classifications
-
- 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
-
- 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
Landscapes
- 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 with high treatment efficiency for low-concentration VOC tail gas, which comprises the steps of (1) pretreatment of the low-concentration VOC tail gas, (2) preheating, (3) RTO incineration, (4) high-temperature reverse combustion, (5) preheating tail gas and carrying out primary cooling on the flue gas after incineration treatment, (6) carrying out secondary cooling on the flue gas subjected to primary cooling and the flue gas subjected to cooling and dewatering, (7) deacidifying the flue gas subjected to secondary cooling, (8) heating and drying the flue gas subjected to cooling and dewatering, and (9) adsorbing by a zeolite molecular sieve to remove secondary organic matters. The invention circularly utilizes the waste heat of low-temperature flue gas, improves the charging temperature of the waste gas, reduces the adsorption and 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, simultaneously reducing the direct entry of ammonia, which is an amine organic substance decomposition product, into a hearth for decomposition due to the adsorption of ammonia on the heat storage bed, reducing the ammonia source for synthesizing ammonium salt, and reducing the blockage caused by the aggregation of ammonium salt particles in the heat storage bed.
Description
Technical Field
The invention relates to a VOC tail gas treatment process and system, in particular to a low-concentration VOC tail gas treatment process and system.
Background
The tail gas of the medicine and pesticide production device is generally condensed, absorbed, adsorbed or separated by a membrane to recover organic matters in the tail gas, and the recovered low-concentration VOC-containing tail gas is subjected to tail end treatment by a heat accumulating incinerator (RTO system for short). The total efficiency of the RTO system on the treatment of organic matters can reach about 99%, so that the RTO system is widely used for treating tail gas at the tail end of a medicine and pesticide production device.
The tail gas at the tail end of the production device of the medicine and the pesticide is characterized by complex components, large fluctuation of gas quantity and concentration and large corrosiveness of smoke generated by incineration. The RTO system has three main problems for treating the tail gas of the waste gas of medicines and pesticides. Firstly, the improvement of removal efficiency is limited, secondly, the corrosion problem, thirdly, the heat storage bed layer is easy to be blocked by ammonium salt, and the ammonium salt is blocked, so that the improvement of the removal efficiency is limited, and the heat storage bed layer is blocked by the ammonium salt, so that the environmental protection device is forced to stop to influence the production operation of the preamble.
Due to the improvement of environmental protection related specification requirements, the internal control indexes of various medicine and pesticide production enterprises are continuously improved, and with the expansion of the types of tail gas brought into the incinerator, the total efficiency of the RTO system is 99 percent, so that the requirements cannot be met gradually. In addition, research and analysis are carried out on RTO tail gas matched with hundreds of sets of medicine and pesticide production devices, and the phenomenon that more than 90 percent of incinerators have the phenomenon that more than 85 percent of residual organic matters in flue gas are organic matters with the boiling point of 100-150 ℃ and the organic matters with the boiling point lower than 100 ℃ only account for about 10 percent is found; the sublimation temperature of the clogging-causing substance accumulated in the heat storage body is generally 150 to 250 ℃.
Disclosure of Invention
The invention aims to: the invention aims to overcome the defects in the prior art, and provides an anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas, which are characterized in that low-temperature flue gas waste heat is recycled, the furnace inlet temperature of the waste gas is increased, the adsorption and implantation of high-waste boiling substances in the waste gas into a heat storage bed are reduced, so that the desorption of the high-waste boiling substances during smoke discharging is reduced, the furnace inlet temperature of the waste gas is increased, ammonia which is an amine organic substance decomposition product is adsorbed on the heat storage bed and directly enters a hearth for decomposition, an ammonia source for synthesizing ammonium salt is reduced, ammonium salt particles are accumulated in the heat storage bed for blocking, high-temperature flue gas forced circulation is adopted, the ammonium salt particles accumulated in the heat storage bed are sublimated and fed into the hearth for combustion decomposition, ammonium salt is prevented from being regenerated, the flue gas after incineration and cooling is adsorbed by a zeolite molecular sieve, the secondary organic substance is removed, the total removal efficiency of the organic substance is up to 99.8% or more, the zeolite molecular sieve adsorbed with the organic substance is desorbed by a high-temperature desorption mode, the generated tail gas is combined and burned, and the generated tail gas is recycled, and the system is recycled, and no secondary pollution is generated.
The technical scheme is as follows: in order to solve the technical problems, the anti-blocking combined process with high treatment efficiency for the low-concentration VOC tail gas comprises the following steps of,
(1) Collecting and preprocessing the low-concentration VOC tail gas to ensure that the concentration of the low-concentration VOC tail gas meets the requirements of < 10g/Nm 3 of incineration treatment of an RTO incinerator;
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in the subsequent step;
(3) The tail gas is preheated and then sent into an RTO incinerator for incineration treatment, organic matters in the tail gas are removed once, the removal rate is more than 99%, and the temperature of flue gas after the incineration treatment of the RTO incinerator is about 120-180 ℃;
(4) The method comprises the steps of adopting a high-temperature fan to proportionally lead back-fire smoke from a hearth and a furnace bottom of an RTO incinerator, wherein the smoke of the hearth is: 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 the heat storage bed layer of the RTO incinerator by the high-temperature fan, the ammonium salt accumulated in the back-burning flue gas sublimates and is primarily decomposed into ammonia and free acid, the ammonia is sent into the hearth of the RTO incinerator to be decomposed into nitrogen and water vapor, the heat generated by the ammonia decomposition during 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 ℃ after incineration treatment of an RTO incinerator, recovering heat in the flue gas, and cooling the flue gas once, wherein the temperature after the primary cooling is 70-130 ℃;
(6) Carrying out secondary cooling on the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling water removal by heat exchange, wherein the temperature after the secondary cooling is 55-110 ℃;
(7) Deacidifying the flue gas subjected to secondary cooling, wherein a deacidification tower is matched for cooling and dewatering, and the temperature of the cooled and dewatered flue gas is 40 ℃;
(8) Carrying out heat exchange on the flue gas subjected to water removal by cooling and the flue gas subjected to primary cooling, and carrying out heating drying, wherein the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) The flue gas at 50 ℃ after heating and drying enters a zeolite molecular sieve to be adsorbed for secondary organic matter removal, the organic matter with the boiling point of 100-150 ℃ is subjected to secondary organic matter removal, the secondary organic matter removal efficiency is about 80%, and after the flue gas is burnt by an RTO incinerator and the organic matter of the zeolite molecular sieve is removed secondarily, the total organic matter removal efficiency of the system is more than 99.8%;
(10) And (3) carrying out desorption after adsorption saturation of the zeolite molecular sieve, wherein the desorption adopts high-temperature air with the temperature of 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 tail gas entering the RTO incinerator for cyclic treatment.
Further, the pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration adjustment, tempering prevention and safety interlocking of the waste gas.
Further, the step (2) and the step (5) adopt a heat exchanger to preheat tail gas and cool the flue gas to achieve waste heat recovery, the temperature of the cold side tail gas after preheating is about 70 ℃, and the temperature of the flue gas after cooling on the hot side is 70-130 ℃.
Further, in the step (3), the RTO incinerator is a box type heat accumulating incinerator, the high-temperature oxidation temperature is 800-900 ℃, the removal efficiency is 99%, 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 in the back-firing must be 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, the step (6) and the step (8) adopt a heat exchanger to carry out secondary cooling of the flue gas and heating drying of the cooled and dehydrated flue gas, the secondary cooling temperature of the flue gas is 55-110 ℃, and the temperature after drying is about 50 ℃.
The utility model provides a low concentration VOC tail gas high treatment efficiency prevents stifled combination system, it includes the exhaust gas pretreatment device that process step (1) used, the tail gas preheating and the flue gas primary cooler that process step (2) and (5) used in proper order, the RTO burns the stove that process step (3) used, the flue gas secondary cooler that process step (6) and (8) used, the zeolite molecular sieve adsorption equipment that flue gas cooling deacidification device that process step (7) used and process step (9) used, exhaust gas pretreatment device links to each other with tail gas preheating and flue gas primary cooler one end through the main fan of waste gas, the flue gas after the RTO burns the stove burns the treatment links to each other with tail gas preheating and flue gas primary cooler other end through the pipeline, the furnace and the stove bottom of RTO burns the fan all link to each other with high temperature anti-burning fan one end through the pipeline, the high temperature anti-burning fan other end links to each other with the heat accumulation bed layer of RTO burns the stove, be equipped with draught fan I between zeolite molecular sieve adsorption equipment and the main fan front end.
Further, the tail gas preheating and flue gas primary cooler and the flue gas secondary cooler are both heat exchangers.
Further, the flue gas after being incinerated by the RTO incinerator sequentially passes through a tail gas preheating end of a primary flue gas cooler, a cooling end of a secondary flue gas cooler, a flue gas cooling deacidification device, a heating end of the secondary flue gas cooler and a zeolite molecular sieve adsorption device.
The beneficial effects are that: compared with the prior art, the invention has the remarkable advantages that: the method is characterized in that low-temperature flue gas waste heat is recycled, the furnace inlet temperature of waste gas is improved, the adsorption and implantation of high-waste boiling substances in the waste gas entering the furnace on a heat storage bed are reduced, so that the desorption of the high-waste boiling substances during smoke discharging is reduced, the furnace inlet temperature of the waste gas is improved, ammonia which is an amine organic substance decomposition product is directly absorbed in the heat storage bed and directly enters a hearth for decomposition, an ammonia source for synthesizing ammonium salt is reduced, the accumulation of ammonium salt particles in the heat storage bed is reduced, the blockage caused by the accumulation of ammonium salt particles in the heat storage bed is reduced, high-temperature flue gas is forced to circulate, the ammonium salt particles accumulated in the heat storage bed sublimate and are sent into the hearth for combustion decomposition, ammonium salt regeneration is prevented, the flue gas after incineration and cooling is adsorbed by a zeolite molecular sieve, the secondary organic substances in the flue gas after incineration are removed, the total removal efficiency of the organic substances reaches more than 99.8%, the zeolite molecular sieve with the adsorbed organic substances is desorbed by adopting a high-temperature desorption mode, the tail gas generated by desorption is combined and sent to be incinerated, the zeolite molecular sieve is recycled, and the secondary pollution is avoided, and the residual organic substances in the flue gas can be effectively removed at the boiling point of 100-150 ℃.
Drawings
FIG. 1 is a schematic diagram of a process system of the present invention.
Detailed Description
The invention is further described below with reference to the drawings 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 preprocessing the low-concentration VOC tail gas to ensure that the concentration of the low-concentration VOC tail gas meets the requirements of less than 10g/Nm 3 of the incineration treatment of an RTO furnace;
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in a subsequent process;
(3) The tail gas is preheated and then sent into an RTO furnace for incineration treatment, organic matters in the tail gas are removed once, the removal rate is more than 99%, and the temperature of flue gas after the incineration treatment of the RTO furnace is about 120-180 ℃;
(4) The high-temperature fan is adopted to proportionally lead the back-fire smoke from the RTO hearth and the hearth, and the hearth smoke is as follows: the ratio of the flue gas at the bottom of the furnace is 1:3, the temperature of the back-burned flue gas at the inlet of the high-temperature fan is ensured to be about 280-300 ℃, the back-burned flue gas is sent into the RTO furnace heat storage bed layer by the high-temperature fan, the ammonium salt accumulated in the back-burned flue gas is sublimated into ammonia and primarily decomposed into free acid, the ammonia is sent into the RTO furnace to be decomposed into nitrogen and steam, and one element generated by the ammonium salt is eliminated;
(5) Preheating tail gas of the flue gas at 120-180 ℃ after incineration treatment of an RTO furnace, recovering heat in the flue gas, and cooling the flue gas once, wherein the temperature after primary cooling is 70-130 ℃;
(6) Carrying out secondary cooling on the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling water removal by heat exchange, wherein the temperature after the secondary cooling is about 55-110 ℃;
(7) Deacidifying the flue gas subjected to secondary cooling, wherein a deacidification tower is matched for cooling and dewatering, and the temperature of the cooled and dewatered flue gas is 40 ℃;
(8) Carrying out heat exchange on the flue gas subjected to water removal by cooling and the flue gas subjected to primary cooling, and carrying out heating drying, wherein the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) The flue gas at 50 ℃ after heating and drying enters a zeolite molecular sieve to be adsorbed for secondary organic matter removal, the organic matter with the boiling point of 100-150 ℃ is subjected to secondary organic matter removal, the secondary organic matter removal efficiency is about 80%, and after RTO incineration and secondary organic matter removal of the zeolite molecular sieve, the total organic matter removal efficiency of the system is more than 99.8%;
(10) And (3) carrying out desorption after adsorption saturation of the zeolite molecular sieve, wherein the desorption adopts high-temperature air with the temperature of 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 tail gas entering the RTO incinerator for cyclic treatment.
The pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration adjustment, 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 smoke so as to achieve the effect of waste heat recovery, the temperature of the cold side tail gas after preheating is about 70 ℃, the temperature of the smoke after cooling on the hot side is 70-130 ℃, and the materials of the heat exchanger are selected according to the characteristics of waste gas and smoke.
In the step (3), the used RTO incinerator is a traditional box type heat accumulating incinerator, the removal principle is high-temperature oxidative decomposition, the high-temperature oxidative temperature is 800-900 ℃, the removal efficiency is 99%, and the heat accumulating incinerator comprises a complete set of equipment such as a matched combustor, an instrument, a valve, automatic control and the like. 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 burning is necessarily higher than the sublimation decomposition temperature of ammonium salt possibly generated by the system, so that the decomposition of the ammonium salt is ensured, a fan used for back burning is required to meet the corrosion and temperature resistance requirements of working conditions, the back burning is automatically started or manually started according to the pressure difference condition of the RTO incinerator, and the back burning procedure comprises cooling and safety interlocking.
In the step (6) and the step (8), the heat exchangers are adopted to carry out secondary cooling of the flue gas and heating and drying of the cooled and dehydrated flue gas, the secondary cooling temperature of the flue gas is 55-110 ℃, the temperature after drying is about 50 ℃, and the materials of the heat exchangers are selected according to the characteristics of the flue gas at two sides.
The flue gas cooling effect of the step (6) is to reduce the cooling load of the step (7); the drying and heating function of the step (8) is to reduce the saturation degree of the flue gas and the steam of the step (7) and prevent the condensation of free water from affecting the adsorption efficiency of the zeolite molecular sieve of the step (9).
In the step (7), the deacidification treatment is a cooling deacidification flow of a traditional RTO system, the deacidification tower is matched with the cooling deacidification flow to carry out cooling water removal, the temperature of the cooled and dehydrated flue gas is 40 ℃, and the purpose of cooling water removal 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 ℃, 200-350 ℃ high-temperature thermal desorption can be adopted, the zeolite molecular sieve 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 switching is automatically switched according to the online monitoring data of the flue gas emission, and the waste gas generated by the desorption is merged into a waste gas main fan inlet through a desorption fan and sent into an RTO furnace for secondary incineration.
As shown in figure 1, the anti-blocking combined system with high treatment efficiency for low-concentration VOC tail gas sequentially comprises a tail gas pretreatment device 1 used in the process step (1), 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 tail gas preheating and flue gas primary cooler 2 and the flue gas secondary cooler 4 are heat exchangers, the tail gas pretreatment device 1 is connected with one end of the tail gas preheating and flue gas primary cooler 2 through a main exhaust fan 7, the flue gas after being incinerated by the RTO incinerator 3 sequentially passes through a cooling end of the tail gas preheating and flue gas primary cooler 2, a cooling end of the flue gas secondary cooler 4, a flue gas cooling deacidification device 5, the flue gas secondary cooler 4 and the zeolite molecular sieve adsorption device 6, a hearth of the O incinerator 3 and a furnace bottom and a high-temperature furnace are connected with a high-temperature zeolite layer 6 through a high-temperature pipeline, and a zeolite layer I is arranged between the main exhaust fan 7 and the heat exchanger 6, and one end of the zeolite layer I is connected with the high-temperature zeolite adsorption device 6 through a high-temperature layer I, and the air layer II is arranged between the main exhaust layer and the main exhaust gas layer.
The invention circularly utilizes the waste heat of low-temperature flue gas, improves the charging temperature of waste gas, reduces the adsorption and implantation of high-waste boiling matters in the charging waste gas on a heat storage bed, thereby reducing the desorption of the high-waste boiling matters in the waste gas during smoke discharge, improving the charging temperature of the waste gas, reducing the decomposition products of amine organic matters, ammonia in the heat storage bed to be adsorbed and directly enter a hearth for decomposition, reducing the ammonia source for synthesizing ammonium salt, reducing the blocking caused by the aggregation of ammonium salt particles in the heat storage bed, adopting high-temperature flue gas forced circulation to sublimate the ammonium salt particles aggregated in the heat storage bed and send the ammonium salt particles into the hearth for combustion decomposition, preventing the regeneration of ammonium salt, adopting a zeolite molecular sieve to adsorb the flue gas after burning and cooling, carrying out secondary organic matter removal on the flue gas after burning, meeting the requirement that the total removal efficiency of organic matters reaches more than 99.8 percent, adopting a high-temperature desorption mode to desorb the zeolite molecular sieve, combining and sending the generated tail gas to for burning and burning, recycling the zeolite molecular sieve, and realizing the secondary pollution free generation, and the effective removal of the residual organic matters with the boiling point of 100-150 ℃.
The present invention provides a method and a thought, and a method for implementing the technical scheme are numerous, the above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, several improvements and modifications can be made, and these improvements and modifications should also be regarded as protection scope of the present invention, and each component that is not explicitly described in the present embodiment can be implemented by the prior art.
Claims (9)
1. An anti-blocking combined process with high treatment efficiency for low-concentration VOC tail gas is characterized by comprising the following steps of: it comprises the following steps of the method,
(1) Collecting and preprocessing the low-concentration VOC tail gas to ensure that the concentration of the low-concentration VOC tail gas meets the requirements of < 10g/Nm 3 of incineration treatment of an RTO incinerator;
(2) Preheating the pretreated tail gas to 70 ℃, wherein a tail gas preheating heat source is hot flue gas in the subsequent step;
(3) The tail gas is preheated and then sent into an RTO incinerator for incineration treatment, organic matters in the tail gas are removed once, the removal rate is more than 99%, and the temperature of flue gas after the incineration treatment of the RTO incinerator is about 120-180 ℃;
(4) The method comprises the steps of adopting a high-temperature fan to proportionally lead back-fire smoke from a hearth and a furnace bottom of an RTO incinerator, wherein the smoke of the hearth is: 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 the heat storage bed layer of the RTO incinerator by the high-temperature fan, the ammonium salt accumulated in the back-burning flue gas sublimates and is primarily decomposed into ammonia and free acid, the ammonia is sent into the hearth of the RTO incinerator to be decomposed into nitrogen and water vapor, the heat generated by the ammonia decomposition during 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 ℃ after incineration treatment of an RTO incinerator, recovering heat in the flue gas, and cooling the flue gas once, wherein the temperature after the primary cooling is 70-130 ℃;
(6) Carrying out secondary cooling on the flue gas with the temperature of 70-130 ℃ subjected to primary cooling and the flue gas subjected to cooling water removal by heat exchange, wherein the temperature after the secondary cooling is 55-110 ℃;
(7) Deacidifying the flue gas subjected to secondary cooling, wherein a deacidification tower is matched for cooling and dewatering, and the temperature of the cooled and dewatered flue gas is 40 ℃;
(8) Carrying out heat exchange on the flue gas subjected to water removal by cooling and the flue gas subjected to primary cooling, and carrying out heating drying, wherein the temperature after drying is 50 ℃, and the humidity of the flue gas after drying is less than 60%;
(9) The flue gas at 50 ℃ after heating and drying enters a zeolite molecular sieve to be adsorbed for secondary organic matter removal, the organic matter with the boiling point of 100-150 ℃ is subjected to secondary organic matter removal, the secondary organic matter removal efficiency is about 80%, and after the flue gas is burnt by an RTO incinerator and the organic matter of the zeolite molecular sieve is removed secondarily, the total organic matter removal efficiency of the system is more than 99.8%;
(10) And (3) carrying out desorption after adsorption saturation of the zeolite molecular sieve, wherein the desorption adopts high-temperature air with the temperature of 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 tail gas entering the RTO incinerator for cyclic treatment.
2. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is characterized in that: the pretreatment in the step (1) comprises the steps of acid removal, dust removal, concentration adjustment, tempering prevention and safety interlocking of the waste gas.
3. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is characterized in that: and (2) and (5) preheating tail gas and cooling the flue gas by adopting a heat exchanger to achieve waste heat recovery, wherein the temperature of the cold side tail gas after preheating is about 70 ℃, and the temperature of the flue gas after cooling on the hot side is 70-130 ℃.
4. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is characterized in that: in the step (3), the RTO incinerator is a box type regenerative incinerator, the high-temperature oxidation temperature is 800-900 ℃, the removal efficiency is 99%, the maximum allowable input waste gas VOC concentration is 10g/Nm < 3 >, the inlet tail gas temperature of the step (3) is about 70 ℃, and the generated flue gas temperature is 120-180 ℃.
5. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is 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 ammonium salt possibly generated by the system, so as to ensure the decomposition of the ammonium salt.
6. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is characterized in that: and (6) and (8) adopt a heat exchanger to carry out secondary cooling of the flue gas and heating and drying of the cooled and dehydrated flue gas, wherein the secondary cooling temperature of the flue gas is 55-110 ℃, the temperature after drying is about 50 ℃, and the humidity of the flue gas after drying is less than 60%.
7. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 1, which is characterized in that: the device 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) in sequence, 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 after the incineration treatment of 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 connected with one end of a high-temperature back-burning fan (8) through pipelines, the other end of the high-temperature back-burning fan (8) is connected with a heat storage bed layer of the RTO incinerator (3) through a pipeline, a zeolite molecular sieve adsorption device (10) is arranged between the flue gas secondary cooler (4) and the zeolite adsorption device (6), and a zeolite adsorption device (10) is arranged between the main fan (6).
8. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 7, wherein the anti-blocking combination process is characterized in that: the tail gas preheating and flue gas primary cooler (2) and the flue gas secondary cooler (4) are heat exchangers.
9. The anti-blocking combination process with high treatment efficiency for low-concentration VOC tail gas according to claim 7 or 8, characterized in that: flue gas after being 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).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111042126.1A CN113701174B (en) | 2021-09-07 | 2021-09-07 | Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111042126.1A CN113701174B (en) | 2021-09-07 | 2021-09-07 | Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113701174A CN113701174A (en) | 2021-11-26 |
| CN113701174B true CN113701174B (en) | 2024-07-12 |
Family
ID=78660752
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111042126.1A Active CN113701174B (en) | 2021-09-07 | 2021-09-07 | Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113701174B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114198758A (en) * | 2021-12-06 | 2022-03-18 | 江苏瑞鼎环境工程有限公司 | Normal butane method maleic anhydride tail gas is with incineration disposal system |
| CN117231993B (en) * | 2023-11-01 | 2024-06-07 | 江苏大信环境科技有限公司 | Anti-corrosion anti-blocking RTO system for fine chemical tail gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109442438A (en) * | 2018-10-24 | 2019-03-08 | 江苏大信环境科技有限公司 | The comprehensive processing technique and system of a kind of organic exhaust gas containing ammonia and the organic wastewater containing ammonia |
| CN112902200A (en) * | 2021-01-28 | 2021-06-04 | 南京工大环境科技有限公司 | Heat storage incineration RTO treatment process for tail gas produced by ammonia oxidation process |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100467801B1 (en) * | 2001-08-31 | 2005-01-24 | 재단법인 포항산업과학연구원 | Method and Device for high temperature incineration and thermal decomposition of wastes |
| JP5459965B2 (en) * | 2008-02-05 | 2014-04-02 | メタウォーター株式会社 | Method for removing N2O in exhaust gas |
| CN204494431U (en) * | 2015-03-18 | 2015-07-22 | 北京鞍信天硕工程技术有限公司 | Based on color-coating line exhaust-gas treatment and the heat recovery system of thermal accumulating incinerator |
| CN206073094U (en) * | 2016-08-25 | 2017-04-05 | 苏州天成涂装系统股份有限公司 | A kind of VOC waste gas total system |
-
2021
- 2021-09-07 CN CN202111042126.1A patent/CN113701174B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109442438A (en) * | 2018-10-24 | 2019-03-08 | 江苏大信环境科技有限公司 | The comprehensive processing technique and system of a kind of organic exhaust gas containing ammonia and the organic wastewater containing ammonia |
| CN112902200A (en) * | 2021-01-28 | 2021-06-04 | 南京工大环境科技有限公司 | Heat storage incineration RTO treatment process for tail gas produced by ammonia oxidation process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113701174A (en) | 2021-11-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107971330B (en) | System and method for repairing ectopic thermal desorption of organic contaminated soil by efficiently utilizing waste heat | |
| CN113701174B (en) | Anti-blocking combined process and system with high treatment efficiency for low-concentration VOC tail gas | |
| CN103785289B (en) | Process method and the flue gas treating system of rich carbonated flue gas | |
| US6666911B2 (en) | Treatment system for waste gas containing volatile organic compounds | |
| CN108704435B (en) | Energy-saving and emission-reducing method and device for waste gas/pollutants of coking enterprise | |
| CN111174619A (en) | Thermal desorption combined use and waste heat recycling method and system adopted by same | |
| CN103288314A (en) | Substance heat treatment separation and energy recovery system | |
| CN110818220A (en) | Sludge low-temperature drying coupling pyrolysis system | |
| CN110975515A (en) | Activated carbon adsorption purification system and method for power-on heating regeneration | |
| CN210832034U (en) | Treatment system for rectification wastewater vapor for producing sodium hydrosulfite | |
| CN210206264U (en) | Treatment device for tar processing asphalt smoke | |
| CN114887443A (en) | Oil gas condensation recovery combined RTO petrochemical tank area waste gas treatment system and process | |
| CN107642789B (en) | Graded air distribution type heat accumulating incinerator | |
| CN113772915A (en) | Equipment and process technology for integrally treating oily sludge through high-temperature oxidation pyrolysis thermal desorption | |
| CN211987828U (en) | Nitrogen protection active carbon adsorption desorption device | |
| CN212119479U (en) | Zeolite runner adsorbs desorption catalytic combustion all-in-one | |
| CN206176412U (en) | Energy -saving organic waste gas waste heat utilization equipment | |
| CN111185144A (en) | Activated carbon thermal regeneration device and process | |
| CN212713214U (en) | Sludge drying treatment equipment | |
| CN212068772U (en) | Active carbon thermal regeneration device | |
| CN212467671U (en) | Cremation tail gas clean-up system | |
| CN212166975U (en) | Processing system of wash oil regeneration residue flue gas | |
| TWM600208U (en) | Soil pollution heat treatment system | |
| CN114234209A (en) | High-salt high-COD wastewater resource recycling treatment system and method | |
| CN111620542A (en) | Sludge drying treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |