CN105423314A - Waste gas treatment process - Google Patents
Waste gas treatment process Download PDFInfo
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- CN105423314A CN105423314A CN201410478043.0A CN201410478043A CN105423314A CN 105423314 A CN105423314 A CN 105423314A CN 201410478043 A CN201410478043 A CN 201410478043A CN 105423314 A CN105423314 A CN 105423314A
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Abstract
The invention relates to a waste gas treatment process. The waste gas treatment process is characterized by sequentially comprising the steps that regenerative chambers are heated; waste gas is evenly fed into part of the regenerative chambers through a gas distributor, and the temperature of the waste gas is increased to the temperature of the decomposition point of organic matter such as benzene, n-butane and carbon monoxide in the waste gas through heating; the waste gas heated by regenerators is fed into a thermal oxidation chamber to be incinerated, and the organic matter is converted into carbon dioxide and water vapor so as to be turned into harmless high-temperature flue gas; part of the high-temperature flue gas is fed into the remaining regenerative chambers to be subjected to heat exchange with the regenerators, so that the high-temperature flue gas is cooled and exhausted into the atmosphere; the remaining high-temperature flue gas is fed into a waste heat recovery device, heat energy is recovered, and the high-temperature flue gas entering the waste heat recovery device is cooled to be turned into low-temperature flue gas meeting the emission requirement; and the steps of reverse blowing, dust removal and the like are conducted on the regenerative chambers in turn. By the adoption of the process, one-time investment and operation cost can be reduced, and atmospheric pollution is reduced. The waste gas treatment process is suitable for conducting regenerative oxidation treatment on the exhausted waste gas in the maleic anhydride production process.
Description
Technical field
The present invention relates to environmental technology field, particularly relate to a kind of organic waste gas treatment method.
Background technology
At present at waste gas production industry, mainly adopt following three kinds of methods to the process of the waste gas produced in production process, one is water absorption method, and two is catalytic burning methods, and three is heating power burning methods.Water absorption method carries out water at last procedure of maleic anhydride production to maleic anhydride waste gas to absorb process, and owing to containing benzene in maleic anhydride waste gas, and benzene is difficult to be dissolved in the water.Therefore, process maleic anhydride waste gas in this way, effect is poor.Catalytic burning method is initiation temperature maleic anhydride waste gas being preheating to catalyst, after preheating, waste gas enters catalytic reactor, make organic matter in maleic anhydride waste gas and oxygen in catalyst surface generation oxidation reaction, finally make organic matter be converted into the innocuous gas such as carbon dioxide and water vapour.This innocuous gas enters waste-heat recovery device, again enters air after reclaiming to waste heat.Due to catalyst costly, one-time investment is large.Again because catalytic burning temperature is lower, only have 500 ~ 600 DEG C, make the temperature entering waste-heat recovery device also low, the heat of recovery is also few.In addition, because the elements such as halogen, sulphur, phosphorus in waste gas are higher, and these elements are to the toxic effect of catalyst, make the service life of catalyst not long, often therefore need more catalyst changeout, and operating cost is higher.It is send into heating power incinerator after maleic anhydride waste gas is preheating to uniform temperature that heating power burns, by the combustion-supporting burning of the fuel such as natural gas, the incineration temperature of maleic anhydride waste gas is made to reach more than 800 DEG C, in waste gas, organic matter complete oxidation decomposes, sending into waste-heat recovery device by burning the flue gas produced, after carrying out energy recovery, entering air again.Adopt the fuel needed in this way more, to process 20,000 tons of normal butane maleic anhydride waste gas, per hourly need consume natural gas more than 1600 cubic meter, therefore operating cost is higher.
In addition, because the heating by the exhaust gases device in catalytic burning technique and heating power burning process, burned waste gas device, smoke temperature reducer are completed by individual equipment respectively, by comparatively multi-pipeline connection between equipment, plant area area is large.
Summary of the invention
The problem to be solved in the present invention is to provide a kind of waste gas treatment process.Adopt this technique, one-time investment and operating cost can be reduced, reduce atmosphere pollution.
For solving the problem, take following technical scheme:
Processing process of maleic anhydride waste gas feature of the present invention comprises the following steps successively:
(1) get regenerator ready, and regenerator is heated to running status; Wherein, heat storage is had in regenerator;
(2) be 35-40 DEG C by gas distributor by temperature, the waste gas of pressure 4000-12000Pa sends into part regenerator uniformly, absorb by waste gas the heat that in regenerator, heat storage stores, EGT is heated to more than decomposition point temperature 600-700 DEG C of organic matter in waste gas (benzene, normal butane, carbon monoxide);
(3) maleic anhydride waste gas heated through heat storage is sent into the thermal oxidizer burning 1-1.2s that temperature is 800-900 DEG C, make the organic matter generation oxidative decomposition in waste gas, make organic matter be converted into carbon dioxide and water vapour, become harmless high-temperature flue gas;
(4) part in above-mentioned high-temperature flue gas is sent into remaining part regenerator, make high-temperature flue gas and heat storage carry out heat exchange, make high-temperature flue-gas be down to 80-100 DEG C and enter air by chimney; Remaining high-temperature flue gas is sent into waste-heat recovery device, heat energy is reclaimed, makes the high-temperature flue-gas entering waste-heat recovery device be down to 130-160 DEG C, become the low-temperature flue gas reaching emission request;
(5) meanwhile, close one of them regenerator air inlet/outlet in turn, with waste-heat recovery device part low-temperature flue gas out, blowback is carried out to this regenerator, remove waste gas remaining in regenerator and flue dust; Waste-heat recovery device residue flue gas is out entered air by chimney simultaneously.
Adopt such scheme, have the following advantages:
Because the present invention carries out heat exchange by making waste gas directly contact with the heat storage in regenerator, heat exchange efficiency is up to 85-90%, can by heating by the exhaust gases to after 550-600 DEG C, send into thermal oxidizer to burn, the little fuel of such use can reach the object of complete waste gas from incinerator, and operating cost is lower.
Again because the present invention carries out heat exchange by making waste gas directly contact with the heat storage in regenerator, heat exchange efficiency, up to 85-90%, by heating by the exhaust gases to after 600-700 DEG C, can be sent into thermal oxidizer and burns.Heat storage is wherein ceramic, and price is lower and service life is longer, compared with catalytic burning technique, does not need catalyst, thus greatly reduces one-time investment.
In addition, because method of the present invention is the incinerator arranging multiple regenerator in a railway carriage or compartment, thus heating by the exhaust gases device, burned waste gas device, smoke temperature reducer are integrated in one, decrease the facility such as waste gas, flue, Appropriate application space, plant area area is less.
Detailed description of the invention
below in conjunction with embodiment, the present invention will be further described:
Embodiment one
First get out ten regenerator, and regenerator is heated to running status.All heat storage is installed in ten regenerator.Described heat storage is ceramic, it is evenly equipped with vertical hole, so that it is cellular to make heat storage be formed.
Afterwards, be 30 DEG C by gas distributor by temperature, the waste gas of pressure 11000Pa sends into five regenerator uniformly, absorbed the heat stored in thermal storage ceramic in five regenerator by waste gas, EGT is heated to organic decomposition point temperature 650 DEG C in waste gas.
Afterwards, the thermal oxidizer being 800 DEG C by the waste gas feeding temperature heated by heat storage burned for 1 second, made the organic matter generation oxidative decomposition in waste gas, made organic matter be converted into carbon dioxide and water vapour, become harmless high-temperature flue gas.
Afterwards, the part in above-mentioned high-temperature flue gas is sent into five remaining regenerator, makes high-temperature flue gas and this five heat storages carry out heat exchange, make high-temperature flue-gas be down to 80 DEG C and enter air by chimney.Remaining another part high-temperature flue gas is sent into waste-heat recovery device, by waste-heat recovery device, heat energy is reclaimed, make the high-temperature flue-gas entering waste-heat recovery device be down to 150 DEG C, become the low-temperature flue gas reaching emission request.
Finally, close the inlet, outlet of a regenerator in ten regenerator in turn, with waste-heat recovery device part low-temperature flue gas out, blowback is carried out to this regenerator, remove waste gas remaining in regenerator and flue dust.Meanwhile, waste-heat recovery device residue flue gas is out entered air by chimney.
Embodiment two
First get out ten regenerator, and regenerator is heated to running status.All heat storage is installed in ten regenerator.This heat storage is ceramic, it is evenly equipped with vertical hole, so that it is cellular to make heat storage be formed.
Afterwards, be 30 DEG C by gas distributor by temperature, the waste gas of pressure 12000Pa sends into five regenerator uniformly, the heat stored in thermal storage ceramic in these five regenerator is absorbed, by decomposition point temperature 720 DEG C organic in maleic anhydride waste gas heating temperatures to waste gas by maleic anhydride waste gas.
Afterwards, the thermal oxidizer being 850 DEG C by the waste gas feeding temperature heated by heat storage burned for 3 seconds, made the organic matter generation oxidative decomposition in waste gas, made organic matter be converted into carbon dioxide and water vapour, become harmless high-temperature flue gas.
Afterwards, the part in above-mentioned high-temperature flue gas is sent into five remaining regenerator, makes high-temperature flue gas and heat storage carry out heat exchange, make high-temperature flue-gas be down to 90 DEG C and enter air by chimney.Remaining another part high-temperature flue gas is sent into waste-heat recovery device, by waste-heat recovery device, heat energy is reclaimed, make the high-temperature flue-gas entering waste-heat recovery device be down to 160 DEG C, become the low-temperature flue gas reaching emission request.
Finally, close the inlet, outlet of a regenerator in ten regenerator in turn, with waste-heat recovery device part low-temperature flue gas out, blowback is carried out to this regenerator, remove waste gas remaining in regenerator and flue dust.Meanwhile, waste-heat recovery device residue flue gas is out entered air by chimney.
Claims (4)
1. a waste gas treatment process, is characterized in that comprising the following steps successively:
(1) get regenerator ready, and regenerator is heated to running status; Wherein, heat storage is had in regenerator;
(2) be 35-40 DEG C by gas distributor by temperature, the waste gas of pressure 4000-12000Pa sends into part regenerator uniformly, absorb by waste gas the heat that in regenerator, heat storage stores, EGT is heated to more than decomposition point temperature 600-700 DEG C of organic matter in waste gas (benzene, normal butane, carbon monoxide);
(3) maleic anhydride waste gas heated through heat storage is sent into the thermal oxidizer burning 1-1.2s that temperature is 800-900 DEG C, make the organic matter generation oxidative decomposition in waste gas, make organic matter be converted into carbon dioxide and water vapour, become harmless high-temperature flue gas;
(4) part in above-mentioned high-temperature flue gas is sent into remaining part regenerator, make high-temperature flue gas and heat storage carry out heat exchange, make high-temperature flue-gas be down to 80-100 DEG C and enter air by chimney; Remaining high-temperature flue gas is sent into waste-heat recovery device, heat energy is reclaimed, makes the high-temperature flue-gas entering waste-heat recovery device be down to 130-160 DEG C, become the low-temperature flue gas reaching emission request;
(5) meanwhile, close one of them regenerator air inlet/outlet in turn, with waste-heat recovery device part low-temperature flue gas out, blowback is carried out to this regenerator, remove waste gas remaining in regenerator and flue dust; Waste-heat recovery device residue flue gas is out entered air by chimney simultaneously.
2. waste gas treatment process according to claim 1, is characterized in that described regenerator is no less than four.
3. waste gas treatment process according to claim 1, is characterized in that described regenerator is ten.
4. the waste gas treatment process according to any one of claims 1 to 3, is characterized in that described heat storage is ceramic, it is evenly equipped with vertical hole, to be formed cellular.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410478043.0A CN105423314A (en) | 2014-09-19 | 2014-09-19 | Waste gas treatment process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410478043.0A CN105423314A (en) | 2014-09-19 | 2014-09-19 | Waste gas treatment process |
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| CN105423314A true CN105423314A (en) | 2016-03-23 |
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Cited By (1)
| 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 |
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2014
- 2014-09-19 CN CN201410478043.0A patent/CN105423314A/en active Pending
Cited By (1)
| 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 |
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Application publication date: 20160323 |
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