CN101362051A - Acrylonitrile device tail-gas treatment technique - Google Patents
Acrylonitrile device tail-gas treatment technique Download PDFInfo
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- CN101362051A CN101362051A CNA200810200595XA CN200810200595A CN101362051A CN 101362051 A CN101362051 A CN 101362051A CN A200810200595X A CNA200810200595X A CN A200810200595XA CN 200810200595 A CN200810200595 A CN 200810200595A CN 101362051 A CN101362051 A CN 101362051A
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention discloses a technique for treating the tail gas of an acrylonitrile device, which is suitable for treating acrylonitrile tail gas discharged by the acrylonitrile device. The technique is characterized in that: after free water is separated out by a gas-liquid separator, the acrylonitrile tail gas is mixed with air, a noble metal monolithic catalyst is taken as a catalyst and catalytic oxidation reaction is carried out to turn harmful volatile organic compounds into carbon dioxide and water; then a selective reduction monolithic catalyst is taken as a catalyst and selective catalytic reduction reaction with added ammonia is carried out to reduce nitrogen oxide in the tail gas into nitrogen and water. The technique has the advantages of simple technique, turning the harmful volatile organic compounds and nitrogen oxide in the tail gas into carbon dioxide, nitrogen and water, without secondary pollution, the test results totally meeting the environmental protection control requirements of the State Standard of China, adopting a tail gas heat exchanger to recycle reaction heat to heat input tail gas, needing no additional fuel during the normal operation process, small system resistance and low operation cost.
Description
Technical field
The present invention relates to a kind of in industrial production acrylonitrile process tail gas treatment process, relate in particular to a kind of acrylonitrile device tail-gas treatment technique that adopts catalytic oxidation and catalytic reduction technology.
Background technology
Ammoxidation of propylene technology is adopted in the production of acrylonitrile installation, is primary raw material with propylene, ammonia and air, and under the effect of catalyst, reaction generates acrylonitrile and other byproduct, through over-quenching, recovery, technological process such as refining, obtains the acrylonitrile product afterwards.In removal process, be provided with acrylonitrile absorbing tower, discharge one gas, be referred to as tail gas from absorption tower (AOG) in this column overhead.The main component of acrylonitrile tail gas is nitrogen, water vapour and carbon dioxide, contains a certain amount of carbon monoxide, acrylonitrile, propylene, propane, nitrogen oxide etc. simultaneously, and wherein the harm composition to environment is mainly NMHC and nitrogen oxide.Because organic concentration is low in the tail gas from absorption tower of acrylonitrile installation, toxicity is high, adopts general tail gas treatment process can not satisfy environmental requirement.
Tail gas from absorption tower of acrylonitrile installation generally adopts the directly discharging of the high point of chimney at present, and environment is caused severe contamination.
Also there is part propylene nitrile device to adopt thermal oxidation method such as heating power burning process and heat accumulation type thermal oxidation technology to handle tail gas in addition, but the shortcoming of heating power burning process and heat accumulation type thermal oxidation technology is to need to consume a large amount of fuel, operating cost is higher, and it is bigger to burn capacity, has part nitrogen in the thermal oxidation process and is oxidized to nitrogen oxide.
Patent CN1903415 adopts catalytic oxidation process for treating, NMHC in the tail gas from absorption tower of acrylonitrile installation is converted into carbon dioxide and water, but and reckon without the processing of the another kind of environmental hazard composition nitrogen oxide in the acrylonitrile tail gas, and do not adopt an effective measure gas-liquid separation, the existence of small amount of liquid will reduce the service life of catalyst and the security of boiler in the tail gas.
Summary of the invention
Technical problem to be solved by this invention be propose that a kind of technology is simple, SR is little, need not add auxiliary fuel, do not make catalyst poisoning, operating cost is low, the acrylonitrile device tail-gas treatment technique of non-secondary pollution, thorough tail gas treatment.
In order to achieve the above object, the technical scheme that adopts is: acrylonitrile device tail-gas treatment technique, it is characterized in that: acrylonitrile tail gas mixes with air behind the gas-liquid separator separates free water, after the tail gas heat exchanger heating, enter catalyst oxidation reactor and carry out catalytic oxidation, the catalyst fixed bed noble metal honeycomb catalyst that is provided with of described catalyst oxidation reactor, at pressure 0～30kPa (G), inlet temperature is 100～450 ℃, outlet temperature is under 350～750 ℃ the condition, and harmful volatile organic matter is converted into carbon dioxide and water; The gas that comes out from catalyst oxidation reactor is behind heat reclaim unit recovery section heat, enter catalytic reduction reactor, the mid-selective reduction honeycomb catalyst of described catalytic reduction reactor, at pressure 0～30kPa (G), inlet temperature is 120～500 ℃, outlet temperature is to carry out selective catalytic reduction reaction with the ammonia of adding in 125～600 ℃ the catalytic reduction reactor, and the nitrogen oxide in the tail gas is reduced into the nitrogen G﹠W; At last cleaning of off-gas is entered atmosphere.Described catalyst oxidation reactor and catalytic reduction reactor all adopt fixed bed catalytic reactor.
The inlet temperature of described catalyst oxidation reactor is preferably 300 ℃; Outlet temperature is preferably in below 700 ℃.
The inlet temperature of described catalytic reduction reactor is preferably 400 ℃; Outlet temperature is preferably in below 500 ℃.
The noble metal honeycomb catalyst is noble metal honeycomb metallic catalyst or noble metal ceramic honeycomb catalyst in the described catalyst oxidation reactor, and the noble metal in the noble metal honeycomb catalyst is the combination of any one or two kinds of noble metals in platinum, the palladium.
As the preferred technical solution of the present invention, behind catalyst oxidation reactor tail gas discharged process heat reclaim unit tail gas heat exchanger recovery section energy, enter catalytic reduction reactor.The selective reduction honeycomb catalyst that is equipped with in the described catalytic reduction reactor is the vanadium/titanium/tungsten ceramic honeycomb catalyst that contains vanadium, titanium, tungsten.
As another optimal technical scheme of the present invention, behind catalyst oxidation reactor tail gas discharged process heat reclaim unit steam superheater and waste heat boiler recovery section energy, enter catalytic reduction reactor, directly enter atmosphere behind cleaning of off-gas or the process tail gas heat exchanger recovery section heat; Or the part cleaning of off-gas returned by circulating fan and with enter tail gas heat exchanger again after acrylonitrile tail gas mixes, enter catalyst oxidation reactor then and carry out catalytic oxidation, the part cleaning of off-gas directly enters atmosphere.
As the preferred technical solution of the present invention, acrylonitrile tail gas enters catalyst oxidation reactor with after air mixes after tail gas heat exchanger is heated to the catalyst initiation temperature.
As the preferred technical solution of the present invention, enter catalyst oxidation reactor after the preheating of acrylonitrile tail gas heater via when system's intensification goes into operation and carry out catalytic oxidation.
Carry out the system's heater go into operation that heats up and to adopt steam heater or electric heater or oil burner or gas burner; Tail gas heat exchanger is preferably welded plate type heat exchanger or heat exchange of heat pipe or finned tube exchanger.
There is the bypass valve of a conditioned reaction device inlet temperature described catalyst oxidation reactor porch.
As catalytic oxidation mechanism of the present invention, following chemical reaction has mainly taken place in the catalyst oxidation reactor:
4C
3H
3N+15O
2＝12CO
2+6H
2O+2N
2+Q
2CO+O
2＝2CO
2+Q
2C
3H
6+9O
2＝6CO
2+6H
2O+Q
C
3H
8+5O
2＝3CO
2+4H
2O+Q
4C
2H
3N+11O
2＝8CO
2+6H
2O+2N
2+Q
As catalytic reduction mechanism of the present invention, following chemical reaction has mainly taken place in the catalytic reduction reactor:
4NH
3+4NO+O
2＝4N
2+6H
2O+Q
4NH
3+2NO
2+O
2＝3N
2+6H
2O+Q
Advantage of the present invention is: technology of the present invention is simple, with volatile organic matter and conversion of nitrogen oxides harmful in the acrylonitrile installation tail gas is carbon dioxide, water and nitrogen, non-secondary pollution, thorough tail gas treatment, testing result satisfy the environment protection control requirements of national Specification fully; In addition, the present invention has very broad opereating specification, and in the time of can guaranteeing that organic matter and amount of nitrogen oxides change in the acrylonitrile tail gas, system can stable operation; The catalyst that the present invention adopts, mechanical strength height, long service life, resistance are low; At last, the present invention adopts high-efficiency heat pipe heat exchanger, welded plate type heat exchanger and finned tube exchanger to reclaim reaction heat to add hot feed tail gas, need not additional fuel in the normal course of operation.
Description of drawings
Fig. 1 (uses tail gas heat exchanger recovery section heat for the process chart of acrylonitrile device tail-gas treatment technique of the present invention; The cleaning of off-gas emptying does not circulate);
Fig. 2 (uses steam superheater and waste heat boiler recovery section heat for the process chart of acrylonitrile device tail-gas treatment technique of the present invention; Emptying behind the cleaning of off-gas process tail gas heat exchanger recovery section heat);
Fig. 3 (uses steam superheater and waste heat boiler recovery section heat for the process chart of acrylonitrile device tail-gas treatment technique of the present invention; A part participates in circulation through tail gas heat exchanger again in the cleaning of off-gas).
Among the figure: 1 is gas-liquid separator; 2 is air-blaster; 3 is tail gas heat exchanger; 4 is electric heater or steam heater; 5 is catalyst oxidation reactor; 6 is steam superheater; 7 is waste heat boiler; 8 is catalytic reduction reactor; 9 is circulating fan; 10 is chimney.
The specific embodiment
Below in conjunction with drawings and Examples technology of the present invention is further elaborated.
By Fig. 1～3 as seen: acrylonitrile device tail-gas treatment technique, it is characterized in that: acrylonitrile tail gas at first enters gas-liquid separator 1 separated free water, mix with air by air-blaster 2 then, and with after tail gas heat exchanger 3 heating, enter catalyst oxidation reactor 5 and carry out catalytic oxidation, the catalyst fixed bed noble metal honeycomb catalyst that is provided with of described catalyst oxidation reactor 5, at pressure 0～30kPa (G), inlet temperature is 100～450 ℃, outlet temperature is under 350～750 ℃ the condition, and harmful volatile organic matter is converted into carbon dioxide and water; The gas that comes out from catalyst oxidation reactor 5 is behind heat reclaim unit recovery section heat, enter catalytic reduction reactor 8 and carry out catalytic reduction reaction, the catalyst fixed bed selective reduction honeycomb catalyst that is provided with of described catalytic reduction reactor 8, at pressure 0～30kPa (G), inlet temperature is 120～500 ℃, outlet temperature is under 125～600 ℃ the condition, the nitrogen oxide in the tail gas is carried out selective catalytic reduction reaction with the ammonia of adding change into the nitrogen G﹠W; Final purification tail gas enters atmosphere.
Described catalyst oxidation reactor 5 inlet temperatures are preferably 300 ℃, and outlet temperature is preferably below 700 ℃.
Described catalytic reduction reactor 8 inlet temperatures are preferably 400 ℃; Outlet temperature is preferably in below 500 ℃.
Described noble metal honeycomb catalyst is noble metal honeycomb metallic catalyst or noble metal ceramic honeycomb catalyst.Noble metal in the described noble metal catalyst is the combination of any one or two kinds of noble metals in platinum, the palladium.
Described selective reduction honeycomb catalyst is vanadium/titanium/tungsten ceramic honeycomb catalyst.
The preferred version of described recovery section heat is for entering catalytic reduction reactor 8 behind catalyst oxidation reactor 5 tail gas discharged process tail gas heat exchanger 3 recovery section energy.
Another preferred version of described recovery section heat directly enters atmosphere for enter catalytic reduction reactor 8 behind catalyst oxidation reactor 5 tail gas discharged process steam superheater 6 and waste heat boiler 7 recovery section energy behind the cleaning of off-gas process tail gas heat exchanger 3 recovery section heats.
A preferred version again of described recovery section heat is for entering catalytic reduction reactor 8 behind catalyst oxidation reactor 5 tail gas discharged process steam superheater 6 and waste heat boiler 7 recovery section energy, cleaning of off-gas is through behind the tail gas heat exchanger 3 recovery section heats, wherein a part of cleaning of off-gas return by circulating fan 9 and with enter tail gas heat exchanger 3 participation process cycles again after acrylonitrile tail gas mixes.
Acrylonitrile tail gas enters catalyst oxidation reactor 5 with after air mixes after tail gas heat exchanger 3 is heated to the catalyst initiation temperature.Described tail gas heat exchanger 3 is welded plate type heat exchanger or heat exchange of heat pipe or finned tube exchanger.
Enter catalyst oxidation reactor 5 after 4 preheatings of acrylonitrile tail gas heater via when system's intensification goes into operation and carry out catalytic oxidation.Carry out heater 4 employing steam heater or electric heater or oil burner or the gas burners that system heats up and goes into operation.
There is the bypass valve of a conditioned reaction device inlet temperature described catalyst oxidation reactor 5 porch.Tail gas among the embodiment derives from certain company's acrylonitrile installation, and working condition is as shown in table 1.
Certain company's acrylonitrile installation tail gas of table 1 is formed
| Exhaust gas component | Form (w%) |
| Propane | 0.0026-0.0060 |
| Propylene | 0.0018-0.0029 |
| Acrylonitrile | 0.0001 |
| Carbon monoxide | 1.20 |
| Carbon dioxide | 3.25 |
| Water | 3.62 |
| Oxygen | 1.10 |
| Acetonitrile | 0.0032 |
| NO X | 0.068 |
| Nitrogen | 89.72 |
| Add up to | 100 |
| Unstripped gas adds up to Kg/h | 100000 |
| Temperature ℃ | 35 |
| Pressure kPa (G) | 20 |
After tail gas and air mix through after tail gas heat exchanger 3 and/or electric heater 4 heating, inlet temperature is 280 ℃, enter catalyst oxidation reactor 5 and on the noble metal platinum that places catalyst fixed bed layer, palladium honeycomb metallic catalyst, carry out catalytic oxidation, keep catalyst oxidation reactor 5 internal pressures to be about 16kPa (G), harmful volatile organic matter is converted into carbon dioxide and water, and discharging a large amount of heat, outlet temperature is 650 ℃.The gas that comes out from catalyst oxidation reactor 5 enters that temperature is 350 ℃ behind the tail gas heat exchanger 3 recovery section heats, enter catalytic reduction reactor 8, carry out catalytic reduction reaction at the vanadium/titanium/tungsten ceramic honeycomb catalyst that places catalyst fixed bed layer, keep catalytic reduction reactor 8 internal pressures to be about 12kPa (G), nitrogen oxide in the tail gas carries out selective catalytic reduction reaction with the ammonia of adding and becomes the nitrogen G﹠W, outlet temperature is 375 ℃, at last cleaning of off-gas is entered atmosphere.
Detect sending into the laboratory after the discharging gas sampling after handling, the content detection result of acrylonitrile, NMHC and nitrogen oxide is as shown in table 2 in the cleaning of off-gas.
Certain economizes environmental monitoring central station Monitoring Data and control index table 2
| The pollutant title | Concentration of emission | Concentration of emission evaluation criterion (mg/m 3) |
| Acrylonitrile | 15 | 22 |
| NMHC | 105 | 120 |
| Nitrogen oxide NOx | 170 | 240 |
Annotate: concentration of emission is repeatedly the mean value of sampling in the table
After tail gas and air mix through after tail gas heat exchanger 3 and/or electric heater 4 heating, inlet temperature is 300 ℃, enter catalyst oxidation reactor 5, on the noble metal platinum that places catalyst fixed bed layer, palladium honeycomb metallic catalyst, carry out catalytic oxidation, keep catalyst oxidation reactor 5 internal pressures to be about 20kPa (G), harmful volatile organic matter is converted into carbon dioxide and water, and discharges a large amount of heat, outlet temperature is 620 ℃.The gas that comes out from catalyst oxidation reactor 5 enters that temperature is 380 ℃ behind steam superheater 7 and the waste heat boiler 8 recovery section heats, enter catalytic reduction reactor 8, place the vanadium/titanium/tungsten ceramic honeycomb catalyst of catalyst fixed bed layer to carry out catalytic reduction reaction, keep catalytic reduction reactor 8 internal pressures to be about 15kPa (G), nitrogen oxide in the tail gas carries out selective catalytic reduction reaction with the ammonia of adding and becomes the nitrogen G﹠W, outlet temperature is 400 ℃, enters at last to enter atmosphere after heat is reclaimed in tail gas heat exchanger 3 heat exchanges.
Detect sending into the laboratory after the discharging gas sampling after handling, the content detection result of acrylonitrile, NMHC and nitrogen oxide is as shown in table 3 in the cleaning of off-gas.
Certain economizes environmental monitoring central station Monitoring Data and control index table 3
| The pollutant title | Concentration of emission | Concentration of emission evaluation criterion (mg/m 3) |
| Acrylonitrile | 15 | 22 |
| NMHC | 105 | 120 |
| Nitrogen oxide NOx | 160 | 240 |
Annotate: concentration of emission is repeatedly the mean value of sampling in the table.
Embodiment 9
After mixing, tail gas and air heat through tail gas heat exchanger 3 and/or electric heater 4, inlet temperature is 260 ℃, enter catalyst oxidation reactor 5, on the noble metal platinum that places catalyst fixed bed layer, palladium honeycomb metallic catalyst, carry out catalytic oxidation, keep catalyst oxidation reactor 5 internal pressures to be about 18kPa (G), harmful volatile organic matter is converted into carbon dioxide and water, and discharges a large amount of heat, outlet temperature is 630 ℃.After the gas that comes out from catalyst oxidation reactor 5 enters steam superheater 7 and waste heat boiler 8 recovery section heats, enter catalytic reduction reactor 8 and carry out catalytic reduction reaction, catalytic reduction reactor 8 inlet temperatures are 360 ℃.Tail gas carries out catalytic reduction reaction at the vanadium/titanium/tungsten ceramic honeycomb catalyst that places catalyst fixed bed layer, keep catalytic reduction reactor 8 internal pressures to be about 12kPa (G), temperature is about 380 ℃, nitrogen oxide in the tail gas carries out selective catalytic reduction reaction with the ammonia of adding and becomes the nitrogen G﹠W, and outlet temperature is 400 ℃.Final purification tail gas enter tail gas heat exchanger 3 heat exchanges reclaim heat after a part directly enter atmosphere, a part by circulating fan 9 with enter tail gas heat exchanger 3 again after acrylonitrile tail gas mixes.
Detect the content detection result of NMHC (concentration of emission is repeatedly the mean value of sampling) as shown in table 4 in the cleaning of off-gas to sending into the laboratory after the discharging gas sampling after handling.
Certain economizes environmental monitoring central station Monitoring Data and control index table 4
| The pollutant title | Concentration of emission | Concentration of emission evaluation criterion (mg/m 3) |
| Acrylonitrile | 15 | 22 |
| NMHC | 101 | 120 |
| Nitrogen oxide NOx | 160 | 240 |
Embodiment 11
Embodiment 12
Certain company's acrylonitrile emission-control equipment builds up and comes into operation, be subjected to the trust of China Environmental Monitoring General Station, certain economizes the requirement of environmental monitoring central station according to China Environmental Monitoring General Station, the acrylonitrile emission-control equipment has been carried out the spot sampling monitoring checked and accepted, testing result satisfies the environment protection control requirements of national Specification fully.
Claims (15)
1, the treatment process of acrylonitrile installation tail gas, it is characterized in that acrylonitrile tail gas at first enters gas-liquid separator (1) separated free water, mix with air then, after tail gas heat exchanger (3) heating, enter catalyst oxidation reactor (5) and carry out catalytic oxidation, the catalyst fixed bed noble metal honeycomb catalyst that is provided with of described catalyst oxidation reactor (5), at pressure 0～30kPa (G), inlet temperature is 100～450 ℃, outlet temperature is under 350～750 ℃ the condition, and harmful volatile organic matter is converted into carbon dioxide and water; The gas that comes out from catalyst oxidation reactor (5) is behind heat reclaim unit recovery section heat, enter catalytic reduction reactor (8) and carry out catalytic reduction reaction, the catalyst fixed bed selective reduction honeycomb catalyst that is provided with of described catalytic reduction reactor (8), at pressure 0～30kPa (G), inlet temperature is 120～500 ℃, outlet temperature is under 125～600 ℃ the condition, the nitrogen oxide in the tail gas is carried out selective catalytic reduction reaction with the ammonia of adding change into the nitrogen G﹠W.
2, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: catalyst oxidation reactor (5) inlet temperature is preferably 300 ℃, and outlet temperature is preferably below 700 ℃.
3, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: catalytic reduction reactor (8) inlet temperature is preferably 400 ℃, and outlet temperature is preferably below 500 ℃.
4, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: described noble metal honeycomb catalyst is noble metal honeycomb metallic catalyst or noble metal ceramic honeycomb catalyst.
5, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: the noble metal in the described noble metal honeycomb catalyst is the combination of any one or two kinds of noble metals in platinum, the palladium.
6, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: described selective reduction honeycomb catalyst is vanadium/titanium/tungsten ceramic honeycomb catalyst.
7, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: acrylonitrile installation tail gas enters catalyst oxidation reactor (5) with after air or oxygen mixes after tail gas heat exchanger (3) is heated to the catalyst initiation temperature.
8, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: the technology of described recovery section heat is for entering catalytic reduction reactor (8) behind catalyst oxidation reactor (5) tail gas discharged process steam superheater (6) and waste heat boiler (7) recovery section energy.
9, acrylonitrile device tail-gas treatment technique according to claim 8 is characterized in that: directly enter atmosphere after the described cleaning of off-gas that comes out from catalytic reduction reactor (8) reclaims heat through tail gas heat exchanger (3).
10, acrylonitrile device tail-gas treatment technique according to claim 8, it is characterized in that: after the described cleaning of off-gas that comes out from catalytic reduction reactor (8) reclaims heat through tail gas heat exchanger (3), the part cleaning of off-gas return by circulating fan (9) and with enter tail gas heat exchanger (3) again after pending acrylonitrile tail gas mixes.
11, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: described tail gas heat exchanger (3) is welded plate type heat exchanger or heat exchange of heat pipe or finned tube exchanger.
12, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that system heats up to enter catalyst oxidation reactor (5) after acrylonitrile tail gas heater via (4) preheating when going into operation and carry out catalytic oxidation.
13, acrylonitrile device tail-gas treatment technique according to claim 12 is characterized in that: carry out heater (4) employing steam heater or electric heater or oil burner or gas burner that system heats up and goes into operation.
14, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: there is the bypass valve of a conditioned reaction device inlet temperature described catalyst oxidation reactor (5) porch.
15, acrylonitrile device tail-gas treatment technique according to claim 1 is characterized in that: described catalyst oxidation reactor and catalytic reduction reactor all adopt fixed bed catalytic reactor.
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| CN102233231A (en) * | 2011-07-21 | 2011-11-09 | 上海师范大学 | Purification equipment and treatment process for tail gas from acrylonitrile absorption tower |
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| CN104534486A (en) * | 2014-12-18 | 2015-04-22 | 濮阳市华星化工有限公司 | Cyanide-containing waste water treatment system |
| CN104772038A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Method for purifying acrylonitrile apparatus absorbing tower tail gas by using Pd-CeO2/Me-beta molecular sieve |
| CN104772037A (en) * | 2015-03-25 | 2015-07-15 | 中国石油天然气股份有限公司 | Method for purifying acrylonitrile apparatus absorbing tower tail gas by using Pd-CeO2/Me-SAPO molecular sieve |
| CN105605595A (en) * | 2016-01-12 | 2016-05-25 | 北京化工大学 | Integrated purification method and system for industrial waste gas containing cyanogen, hydrocarbon and NOx |
| CN107118293A (en) * | 2017-05-22 | 2017-09-01 | 北京华福工程有限公司 | A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust |
| CN108654369A (en) * | 2018-07-03 | 2018-10-16 | 王氏港建贸易（上海）有限公司 | A kind of scaling powder processing system and the reflow oven comprising it |
| CN109550388A (en) * | 2017-09-25 | 2019-04-02 | 重展(上海)实业有限公司 | House exhaust processing unit |
| CN113617224A (en) * | 2021-08-23 | 2021-11-09 | 湖州乙戈环保设备有限公司 | Treatment device and treatment method for nitrogen oxide waste gas for high-speed wire enamelling machine |
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