CN116538514A - Treatment method of waste gas generated in VAE emulsion production - Google Patents
Treatment method of waste gas generated in VAE emulsion production Download PDFInfo
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- CN116538514A CN116538514A CN202310409568.8A CN202310409568A CN116538514A CN 116538514 A CN116538514 A CN 116538514A CN 202310409568 A CN202310409568 A CN 202310409568A CN 116538514 A CN116538514 A CN 116538514A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 81
- 239000000839 emulsion Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 75
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000002918 waste heat Substances 0.000 claims abstract description 9
- 239000008234 soft water Substances 0.000 claims description 25
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 238000001816 cooling Methods 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 5
- 238000007872 degassing Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 claims description 4
- 239000003546 flue gas Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 3
- 239000005977 Ethylene Substances 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims description 2
- 238000004945 emulsification Methods 0.000 claims 2
- 238000006864 oxidative decomposition reaction Methods 0.000 claims 1
- 239000010815 organic waste Substances 0.000 abstract description 5
- 238000000576 coating method Methods 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000003973 paint Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000001694 spray drying Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000004078 waterproofing Methods 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 239000010425 asbestos Substances 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229920001038 ethylene copolymer Chemical class 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910052895 riebeckite Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
- F22B1/1892—Systems therefor not provided for in F22B1/1807 - F22B1/1861
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/50—Feed-water heaters, i.e. economisers or like preheaters incorporating thermal de-aeration of feed-water
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G1/00—Steam superheating characterised by heating method
- F22G1/02—Steam superheating characterised by heating method with heat supply by hot flue gases from the furnace of the steam boiler
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention aims to provide a method for treating waste gas generated in the production of a VAE emulsion, which realizes a safe, economical and reliable novel process for treating organic waste gas; in order TO achieve the above purpose, the invention provides a treatment method of waste gas produced by VAE emulsion, wherein the waste gas from different waste gas sources is collected in a pressure-equalizing water sealed tank and then enters a gas holder, the working pressure of the gas holder is reasonably determined, the waste gas from the gas holder is directly fed into a TO furnace, the waste gas from the TO furnace is cooled by a waste heat recovery boiler system and by-produced superheated steam, the cooled waste gas is subjected TO denitration by a denitration device, and the denitration waste gas is led TO a chimney for discharge after being further cooled by the heat recovery device.
Description
Technical Field
The invention relates to the field of waste gas treatment, in particular to a method for treating waste gas generated in the production of a VAE emulsion.
Background
The VAE emulsion is one of vinyl acetate and ethylene copolymer compounds and has excellent cohesiveness, flexibility, weather resistance, acid and alkali resistance and film forming property. From the market of VAE emulsion to the present, through the development of nearly half century, the research of the foreign VAE emulsion with high solid content, low viscosity and environmental friendliness is very extensive and deep, a plurality of new varieties have been developed, and the domestic VAE emulsion production scale and varieties have a large gap from the foreign.
However, the VAE emulsion market demand in China is quite rapid. In particular, in recent years, as the awareness of environmental protection in China increases and application technology increases, the application of VAE emulsions in some new industrial fields is expanding. The great use of VAE emulsions in the construction waterproofing field is a major feature of the chinese VAE emulsion industry, since VAE emulsions are rarely used for waterproofing paint from the world's application of the VAE emulsion industry. In China, the waterproof faucet enterprise eastern rainbow uses the paint film formed by the VAE emulsion to have the characteristics of water resistance, alkali resistance, aging resistance, foaming resistance, softness, elasticity and the like, and the VAE emulsion is widely applied to the fields of preparing various building waterproof coatings, such as inner and outer wall coatings, roof waterproof coatings, bathroom waterproof coatings, fireproof coatings, antirust coatings and the like. The VAE emulsion paint can be coated on concrete, mortar, brick, asbestos, gypsum, wood, etc., and can also be used for preparing smooth paint and thick paste paint.
At present, most of VAE emulsion needed in the waterproof industry is purchased from technology-carried enterprises to foreign enterprises which build factories in China, and as the capacity of waterproof coating of the waterproof enterprise increases, the purchase amount of the VAE emulsion is increased continuously, and the purchase of the VAE emulsion becomes a bottleneck of waterproof coating production of the waterproof enterprise. Thus, in the future, the waterproof enterprises develop the VAE emulsion production technology by themselves, and start the construction of the VAE emulsion factory. The invention is a new safe, economical and reliable process for treating waste gas in the development of the VAE emulsion production technology.
Therefore, the method for treating the waste gas generated in the process of producing the VAE emulsion is a technical problem to be solved in a targeted way.
Disclosure of Invention
The invention aims to provide a method for treating waste gas generated in the production of a VAE emulsion, which realizes a novel process for safely, economically and reliably treating organic waste gas.
In order TO achieve the above purpose, the solution of the invention is TO provide a treatment method of waste gas produced by VAE emulsion, waste gas from different waste gas sources is collected in a pressure-equalizing water sealed tank and then enters a gas holder, and the waste gas from the gas holder is directly fed into a TO furnace by reasonably determining the working pressure of the gas holder, the waste gas from the TO furnace is cooled by a waste heat recovery boiler system and by-produced superheated steam, the cooled waste gas is subjected TO denitration by a denitration device, and the denitration waste gas is led TO a chimney for discharge after being further cooled by the heat recovery device; preferably, the gas holder is a wet type vertical lifting gas holder, and the working pressure of the gas holder system is adjusted TO enable the exhaust gas from the gas holder TO directly enter the TO furnace combustion system, so that gas conveying equipment between the gas holder and the TO furnace is reduced.
Further, the exhaust gas sources comprise at least one of degassing tank production exhaust gas, ethylene compressor purge exhaust gas and vinyl acetate storage tank exhaust gas.
Further, a heat accumulator retaining wall is arranged in the TO furnace, waste gas TO be treated is fully contacted with oxygen in a hearth in the heat accumulator wall, so that the oxidation and decomposition efficiency of the waste gas is greatly improved, tail waste gas of a leading part of the TO furnace enters the front end of the TO furnace, the temperature in the furnace is controlled TO be 900-1000 ℃, and NOx is prevented from being generated; preferably, the front end of the hearth is provided with a feed inlet, the rear end of the hearth is provided with an exhaust port, and the feed inlet is connected with a gas holder; the upper end of the hearth is provided with a first air inlet, the first air inlet is used for introducing oxygen, the lower end of the hearth is provided with a second air inlet, the second air inlet is used for introducing circulating waste gas TO adjust the internal temperature of the hearth, and compared with a conventional TO furnace, the TO furnace reduces the internal temperature of the hearth, increases the volume of the furnace body, and improves the residence time of the waste gas in the furnace by 20%.
Further, a tempering-preventing low-nitrogen burner is arranged at the feed inlet of the TO furnace.
Further, an oxygen content detector is arranged in the pressure-equalizing water sealed tank, and when the oxygen content of the waste gas in the pressure-equalizing water sealed tank is more than 3%, the waste gas is forbidden to enter the gas holder; preferably, the depth of the exhaust gas source inserted into the water-sealed tank under the water surface is different according to the air pressure of the exhaust gas source, and the higher the air pressure of the exhaust gas source is, the greater the depth is; preferably, for the waste gas produced by the degassing tank, because the flow rate is large and the flow fluctuation is large, a porous pipe head is designed at the outlet of the pipeline below the water surface, so that the waste gas smoothly enters the pressure equalizing water sealed tank.
Further, the heat recovery boiler system includes: the waste gas generated by the TO furnace enters the boiler device for cooling and then enters the superheater for heat exchange and then further cooling, steam is generated after the boiler device exchanges heat, the steam drum receives the steam from the boiler and the heat recovery device, and the steam in the steam drum enters the superheater for heat exchange and then is discharged; preferably, the steam generated by the heat recovery boiler system is used for spray drying of the VAE emulsion, the steam being superheated steam at 1.0MPaG, 240 ℃.
Further, the boiler device is a fire tube type boiler or a water tube type boiler, wherein the fire tube type boiler is selected when the fluctuation of the exhaust gas quantity is large, and the water tube type boiler is selected when the fluctuation of the exhaust gas quantity is small and is relatively stable.
Further, the waste gas discharged by the superheater enters a denitration device, and the denitration device is an SCR denitration system or an SNCR denitration system.
Further, the heat recovery device includes: the flue gas exhausted by the denitration device enters the economizer to be cooled further and then enters the chimney to be discharged outwards, the deaerator receives a part of steam from the superheater, soft water is introduced into the deaerator, oxygen in the soft water is steamed out through steam heating of the soft water, corrosiveness of the soft water to the economizer is reduced, and the deaerator enters the economizer to exchange heat after deoxidizing the soft water and then enters the steam drum.
Further, a soft water heater or a water cooler is arranged between the economizer and the chimney, the soft water heater is used for cooling waste gas at the outlet of the economizer and heating soft water, if the temperature of the finally discharged waste gas is less than or equal to 75 ℃, the soft water heater is selected, and if no temperature requirement exists, the soft water heater or the water cooler can not be arranged; preferably, an induced draft fan is arranged between the economizer and the chimney.
The invention has the advantages that:
1. collecting all organic waste gas generated in normal production by adopting a gas holder and passing through a direct-fired incinerator
And (5) efficiently oxidizing and decomposing all organic waste gas (TO furnace), recycling heat generated by oxidizing and decomposing the organic waste gas through byproduct superheated steam, fully recovering waste heat by arranging an economizer and a soft water heater, and fully utilizing waste heat and standard (critique evaluation and evaluation) emission by the waste gas of standard emission and the like of the flue gas index after oxidizing and decomposing through a denitration procedure.
2. The front end of the gas holder is provided with a water sealed tank for collecting waste gases with three different pressures and different components, and the potential safety hazard of exceeding oxygen content is eliminated at the front end of the gas holder, so that the generation of large potential safety hazard is avoided.
3. According TO the TO furnace gas pressure requirement, the design pressure of the gas holder is considered, and no gas conveying equipment is arranged between the gas holder and the TO furnace, so that the operation cost can be saved.
4. TO furnace system: a) Setting a backfire-proof low-nitrogen burner; b) Leading part of tail flue gas TO a TO furnace combustion system and a furnace body cooling system; c) The temperature in the hearth is properly reduced (compared with a conventional TO furnace), the volume of the furnace body is properly increased, and the residence time of waste gas in the furnace is increased by 20%; d) A heat accumulator retaining wall is arranged on a rear gas passage of the TO furnace, and the principle of a heat accumulating combustion furnace (RTO furnace) is applied TO a direct combustion furnace (TO furnace).
5. And (3) a fire tube type boiler is selected to recycle the waste heat of the waste gas generated in the VAE emulsion production and to produce 240 ℃ superheated steam as a byproduct for the VAEP rubber powder production.
Drawings
FIG. 1 is a flow chart of a method for treating exhaust gas from VAE emulsion production provided by the invention;
FIG. 2 is a schematic diagram of a TO furnace provided by the invention;
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
As shown in figure 1, in the treatment method of the waste gas produced by the VAE emulsion, the waste gas from different waste gas sources is collected in a pressure-equalizing water sealed tank and then enters a gas holder, the total number of the waste gas sources is 3, the waste gas produced by a degassing tank, the waste gas blown by an ethylene compressor and the waste gas discharged by a vinyl acetate storage tank are respectively, the working pressure of the gas holder is reasonably determined, the waste gas from the gas holder is directly introduced into a TO furnace, the waste gas from the TO furnace is cooled by a waste heat recovery boiler system and by-produced superheated steam, the cooled waste gas is subjected TO denitration by a denitration device, and the denitration waste gas is further cooled by a heat recovery device and is then led TO a chimney for discharge; the gas holder is wet-type vertical lift gas holder, makes the gas holder come out waste gas and directly go into TO stove combustion system through adjusting gas holder system operating pressure, gas holder exhaust waste gas's pressure is 4000pa, reduces the gas conveying equipment between gas holder and the TO stove.
An oxygen content detector is arranged in the pressure equalizing water sealed tank, and when the oxygen content of the waste gas in the pressure equalizing water sealed tank is more than 3%, the waste gas is forbidden to enter the gas holder; according to different air pressures of the waste gas sources, the waste gas sources are inserted into the water-sealed tank to different depths below the water surface, and the higher the air pressure of the waste gas sources is, the greater the depth is; aiming at the waste gas produced by the degassing tank, because the flow is larger and the flow fluctuation is larger, a porous pipe head is designed at the outlet of a pipeline below the water surface, so that the waste gas is stably fed into the pressure equalizing water sealed tank; an oxygen content detection device is arranged on each pipeline of the waste gas source, an oxygen content detector in the pressure equalizing water sealed tank is connected with the SIS system, the oxygen content of waste gas entering the gas holder is strictly controlled to be less than 3%, and the oxygen content of waste gas in the gas holder is prevented from reaching the limit of forming explosive gas.
As shown in fig. 2, a heat accumulator retaining wall is arranged in the TO furnace, tail waste gas of a leading part of the TO furnace enters the front end of the TO furnace, and the temperature in the furnace is controlled TO 900-1000 ℃ TO prevent NOx; the front end of the hearth is provided with a feed inlet, the rear end of the hearth is provided with an exhaust port, and the feed inlet is connected with a gas holder; the upper end of the hearth is provided with a first air inlet, the first air inlet is used for introducing oxygen, the lower end of the hearth is provided with a second air inlet, the second air inlet is used for introducing circulating waste gas TO adjust the internal temperature of the hearth, and a tempering-preventing low-nitrogen burner is arranged at the feed inlet of the TO furnace.
The waste heat recovery boiler system includes: the waste gas generated by the TO furnace enters the boiler device for cooling and then enters the superheater for heat exchange and then further cooling, steam is generated after the boiler device exchanges heat, the steam drum receives the steam from the boiler and the heat recovery device, and the steam in the steam drum enters the superheater for heat exchange and then is discharged; the steam generated by the waste heat recovery boiler system is used for spray drying of the VAE emulsion, the steam is superheated steam of 1.0MPaG and 240 ℃,85% of the steam is used for spray drying of the VAE emulsion, 15% of the steam enters the deaerator, the boiler device is a fire tube type boiler, the temperature of exhaust gas discharged by the boiler device is 350 ℃, the exhaust gas discharged by the superheater enters the denitration device, the temperature of the exhaust gas discharged by the superheater is 305 ℃, the denitration device is an SCR denitration system, the NOx content of gas discharged from a TO furnace is about 100mg/m & lt 3 & gt, the emission requirement still cannot be met, an SCR denitration system is designed in a 300-350 ℃ area, the NOx removal rate is not lower than 60%, the SCR denitration system is connected with the urea pyrolysis system, and the temperature of the exhaust gas discharged by the denitration device is 300 ℃.
The heat recovery device includes: the waste gas discharged by the denitration device enters the economizer to be further cooled and then enters a chimney to be discharged, the deaerator receives a part of steam from the superheater, soft water at 30 ℃ is introduced into the deaerator, oxygen in the soft water is boiled out through heating the soft water by the steam, the corrosiveness of the soft water to the economizer is reduced, and the deaerator deoxidizes the soft water and then enters the economizer to exchange heat and then enters the steam drum; a soft water heater and an induced draft fan are sequentially arranged between the economizer and the chimney, the soft water heater is used for cooling waste gas at the outlet of the economizer and heating soft water, the temperature of the waste gas discharged by the economizer is 150 ℃, and the temperature of the waste gas discharged by the soft water heater is 75 ℃.
It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to fall within the scope of the invention.
Claims (10)
1. A treatment method of waste gas produced by a VAE emulsion is characterized in that waste gas from different waste gas sources is collected in a pressure equalizing water sealed tank and then enters a gas holder, the working pressure of the gas holder is reasonably determined, the waste gas from the gas holder is directly fed into a TO furnace, the waste gas from the TO furnace is cooled by a waste heat recovery boiler system and by-produced superheated steam, the cooled waste gas is subjected TO denitration by a denitration device, and the denitration waste gas is led TO a chimney and is discharged after being further cooled by the heat recovery device.
2. The method of claim 1, wherein the exhaust gas source comprises at least one of a degassing tank process exhaust gas, an ethylene compressor purge exhaust gas, and a vinyl acetate tank exhaust gas.
3. The method for treating waste gas generated by producing a VAE emulsion according TO claim 2, wherein a heat accumulator retaining wall is arranged in the TO furnace, waste gas TO be treated is fully contacted with oxygen in a hearth in the heat accumulator wall, so that the oxidative decomposition efficiency of the waste gas is greatly improved, tail waste gas of a leading part of the TO furnace enters the front end of the TO furnace, the temperature in the furnace is controlled TO 900-1000 ℃, and NOx generation is prevented.
4. The method for treating exhaust gas from VAE emulsion production of claim 3, wherein an anti-flashback low nitrogen burner is provided at the feed inlet of the TO furnace.
5. The method according to claim 4, wherein an oxygen content detector is arranged in the pressure equalizing water sealed tank, and when the oxygen content of the exhaust gas in the pressure equalizing water sealed tank is more than 3%, the exhaust gas is prohibited from entering the gas holder.
6. The method for treating VAE emulsion process exhaust gas according to claim 5, wherein the heat recovery boiler system comprises: the waste gas generated by the TO furnace enters the boiler device for cooling and then enters the superheater for heat exchange and then further cooling, steam is generated after the boiler device exchanges heat, the steam drum receives the steam from the boiler and the heat recovery device, and the steam in the steam drum enters the superheater for heat exchange and then is discharged.
7. The method for treating exhaust gas from VAE emulsion production of claim 6, wherein the boiler device is a fire tube boiler or a water tube boiler.
8. The method for treating exhaust gas generated in VAE emulsion production according to claim 7, wherein the exhaust gas discharged from the superheater enters a denitration device, and the denitration device is an SCR denitration system or an SNCR denitration system.
9. The method for treating VAE emulsion process exhaust gas according to claim 8, wherein the heat recovery device comprises: the flue gas exhausted by the denitration device enters the economizer to be further cooled and then enters the chimney to be discharged, the deaerator receives a part of steam from the superheater, soft water is introduced into the deaerator, and the deaerator deoxidizes the soft water and then enters the economizer to exchange heat and then enters the steam drum.
10. The method according to claim 9, wherein a soft water heater or a water cooler is provided between the economizer and the chimney, and the soft water heater is used for cooling the exhaust gas at the outlet of the economizer and heating the soft water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310409568.8A CN116538514A (en) | 2023-04-17 | 2023-04-17 | Treatment method of waste gas generated in VAE emulsion production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310409568.8A CN116538514A (en) | 2023-04-17 | 2023-04-17 | Treatment method of waste gas generated in VAE emulsion production |
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| Publication Number | Publication Date |
|---|---|
| CN116538514A true CN116538514A (en) | 2023-08-04 |
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|---|---|---|---|
| CN202310409568.8A Pending CN116538514A (en) | 2023-04-17 | 2023-04-17 | Treatment method of waste gas generated in VAE emulsion production |
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| Country | Link |
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| CN (1) | CN116538514A (en) |
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- 2023-04-17 CN CN202310409568.8A patent/CN116538514A/en active Pending
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