CN113144890A - Waste gas purification system and method containing high-concentration laughing gas - Google Patents
Waste gas purification system and method containing high-concentration laughing gas Download PDFInfo
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- CN113144890A CN113144890A CN202110514239.0A CN202110514239A CN113144890A CN 113144890 A CN113144890 A CN 113144890A CN 202110514239 A CN202110514239 A CN 202110514239A CN 113144890 A CN113144890 A CN 113144890A
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- 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
- B01D53/8631—Processes characterised by a specific device
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- 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
- B01D53/869—Multiple step processes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/402—Dinitrogen oxide
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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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)
Abstract
The invention relates to a waste gas purification system and method containing high-concentration laughing gas, which comprises at least one two-section type removal reaction tower, wherein the reaction tower sequentially comprises a gas inlet, a first reaction section, a first heat exchanger and a second reaction section from top to bottom. The removal treatment process of the michelia gas tail gas is improved subversively, and the tail gas does not need to be diluted based on the removal process, so that the processing and maintenance costs of the reactor of the whole treatment process are greatly reduced. In the prior art, because air is needed to dilute the tail gas, the dilution ratio is 1 part of the tail gas to 3 parts of the air, so that the volume of the treatment equipment is overlarge, the processing cost is high, the safety is poor, and the maintenance cost is also high.
Description
Technical Field
The invention relates to the fields of atmosphere environmental protection and carbon neutralization, in particular to a waste gas purification system and method containing high-concentration laughing gas.
Background
Laughing gas (chemical formula N)2O) is the third largest greenhouse gas, the potential greenhouse effect of which is CO2310 times of, CH421 times of, simultaneously, N2O is also a source of nitrogen oxides in the stratosphere, which can cause ozone holes, and is one of the gases that severely pollute the environment.
With the rise of the technology in the related fields of chips and integrated circuits in the production of electronic chemicals in China, the waste gas of michelia gas becomes an important index for polluting the atmosphere. Removing N in tail gas2The O method mainly comprises a high-temperature decomposition method, a selective catalytic reduction method and a catalytic decomposition elimination method.
The pyrolysis method is to make N2O and fuel gas are reacted and decomposed at high temperature (1200-1500 ℃), the technical process is simple, no catalyst is needed, the operation cost is high, a large amount of fuel gas is consumed, and the maintenance difficulty of high-temperature reaction equipment is high. Thus removing N in the chemical tail gas by using a pyrolysis method2The O component may be limited in practical use. This process has been used in adipic acid plants by Asahi and by DuPont, a well-known chemical company, Japan.
The selective catalytic reduction method generally selects ammonia or natural gas as a reducing agent, adds a supported noble metal catalyst, and adjusts a proper reaction temperature (generally 200-600 ℃) according to the difference of the reducing agent and the catalyst, thereby realizing N2And removing O. Pd/FeAlPO-5 is taken as a catalyst, and CH is researched under the conditions of different active component contents, temperature and the like4Reduction of N2The effect of O. Studies indicate that PdAlPO-5 is used as a catalyst, and N is obtained at 373 DEG C2The conversion rate of O can reach 90 percent.
The catalytic cracking elimination method refers to that N is reacted under the action of catalyst2Direct decomposition of O to O2And N2. The method does not need to introduce other substances participating in the removal reaction, has low cost and does not cause secondary pollution, thereby causing extensive attention of researchers. N is a radical of2The activation energy required for the O decomposition process is high (250kJ/mol), and the process is difficult to carry out under the condition without the participation of a catalyst, so the research focus is mainly focused on the development of a novel low-temperature high-activity cracking catalyst.
CN109353999A discloses a device and method for recovering and purifying electronic grade laughing gas in industrial tail gas. The system comprises a water washing tower, a reaction tower, an amine liquid absorption tower, a regenerative decarbonization tower, an alkaline washing water washing tower, an adsorption tower, a compressor and two-stage rectifying towers which are sequentially arranged, wherein a liquid outlet of a tower kettle of the amine liquid absorption tower is connected with a liquid inlet of the regenerative decarbonization tower through a heat exchanger, and a liquid outlet of the tower kettle of the regenerative decarbonization tower is connected with a liquid inlet of the amine liquid absorption tower through a heat exchanger. The invention recovers and purifies nitrous oxide in industrial waste gas by absorption, reaction, adsorption, rectification and other modes, and further obtains 99.999 percent of laughing gas product. However, the treatment process in the patent is complex, brings more cost pressure and potential safety hazard to production enterprises, and is not beneficial to large-scale popularization and implementation.
In the prior art, during the treatment process of the laughing gas waste gas, an oxide catalyst and a molecular sieve catalyst are mainly adopted to decompose industrial laughing gas, and because the decomposition reaction of laughing gas is a powerful heat release process, the temperature of a catalyst bed layer is continuously increased along with the direction of a streamline, a metal catalyst is easy to sinter, the activity is reduced, and the glue removal efficiency of laughing gas is seriously influenced; the supported molecular sieve catalyst has better heat-resistant sintering phenomenon, but the removal efficiency is also influenced by the large pressure drop of the bed layer, the bed layer filling is not uniform enough and the channeling phenomenon is serious because the prior process mainly adopts a packed bed.
Therefore, a system and a method for simply and efficiently treating michelia gas waste gas are provided in a targeted manner, and a technical problem to be solved is formed.
Disclosure of Invention
To solve the above-mentioned drawbacks, the present invention provides a system and a method for purifying exhaust gas containing laughing gas at a high concentration. The invention relates to a method for treating waste gas containing high-concentration laughing gas, which comprises the following steps: carrying out catalytic removal reaction of laughing gas on waste gas to be treated under the catalytic action, heating the waste gas to form hot waste gas due to heat generated by catalytic reaction of laughing gas, cooling the waste gas through heat exchange treatment, and repeatedly repeating the catalytic removal of laughing gas and the heat exchange cooling of the hot waste gas until the content of laughing gas in the waste gas to be treated reaches the normal discharge standard;
the method does not need to dilute the waste gas, and directly finishes removing laughing gas in the waste gas.
Further, controlling the reaction conditions to reduce the concentration of laughing gas in the waste gas to be treated by 7-15% each time of catalytic removal reaction, simultaneously, increasing the temperature of the waste gas by 150-;
and repeating the catalytic removal of the laughing gas and the heat exchange and temperature reduction operation of the hot waste gas repeatedly when necessary until the content of the laughing gas in the waste gas to be treated reaches the emission standard.
In order to realize the method, reaction devices such as catalytic removal reaction of laughing gas, heat exchange cooling of hot waste gas, preheating step and the like can be reasonably arranged and installed based on the method and the requirements of actual working conditions, for example, the existing catalytic removal reactor is adopted for catalytic removal reaction, the existing heat exchange cooling reactor is adopted for heat exchange cooling of hot waste gas, the existing preheating device is adopted for preheating step and the like, the devices can be singly connected in series according to the method, and can be combined, connected in parallel and installed in various ways based on the requirements of actual sites, and the invention is within the protection scope of the invention as long as the operation process of the method can be satisfied.
The invention also provides a waste gas purification system containing high-concentration laughing gas, which comprises at least one two-section type removal reaction tower, wherein the reaction tower sequentially comprises a gas inlet, a first reaction section, a first heat exchanger and a second reaction section from top to bottom; and after the temperature of tail gas containing high-concentration laughing gas is raised through a first preheater, the tail gas enters the two-section type removal reaction tower from the gas inlet, a first catalytic removal reaction is carried out in the first reaction section, then the gas after the reaction in the first reaction section is subjected to heat exchange and temperature reduction through the first heat exchanger and then enters the second reaction section for a second catalytic removal reaction, and the purified tail gas obtained after the second catalytic removal reaction is used for subsequent processes.
Further, the first preheater uses the gas from the second reaction section for heat exchange.
Further, when the system comprises a first two-section type removal reaction tower and a second two-section type removal reaction tower, the gas discharged from the second reaction section is cooled by a second heat exchanger, then continuously enters from the top of the second two-section type removal reaction tower, is subjected to a third catalytic removal reaction in the third reaction section, is cooled by a third heat exchanger, and then is subjected to a fourth catalytic removal reaction in the fourth reaction section, and the obtained purified tail gas is used for subsequent processes. Preferably, the first preheater and/or the second preheater exchange heat using the cleaned off-gas discharged from the fourth reaction section.
Furthermore, the system can be equipped with sufficient quantity of two-section desorption reaction tower, heat exchanger and pre-heater in proper order based on the needs of operational aspect, the system gets into every two-section desorption reaction tower, heat exchanger and pre-heater in proper order according to exhaust-gas treatment's flow direction, finally realizes relying on laughing gas desorption reaction heat to carry out the energy supply of whole desorption system, need not additionally for the system is equipped with the external heating source again.
The invention further provides a method for decomposing high-concentration laughing gas by adopting the system, which comprises the following steps:
1) heating tail gas containing high-concentration laughing gas from industrial gas generation through a preheater to reach the catalytic reaction activity temperature, and then raising the temperature of the tail gas;
2) carrying out the first catalytic removal reaction on the tail gas from the first reaction section of the first two-section removal reaction tower, wherein the temperature of the tail gas is further increased due to reaction heat;
3) the gas after the first catalytic removal reaction is subjected to heat exchange and temperature reduction through a first heat exchanger, and then the cooled gas enters a second reaction section to be subjected to a second catalytic removal reaction, and the temperature of the gas is raised again due to reaction heat;
4) and gas after the second catalytic removal reaction is discharged from the first two-section reaction tower, and purified tail gas is discharged from the first two-section reaction tower.
Further, the purified tail gas is passed into the preheater for preheating of the initial tail gas.
Further, when the system comprises a first two-section type removal reaction tower and a second two-section type removal reaction tower, the gas discharged from the second reaction section is cooled by a second heat exchanger and then continuously enters from the top of the second two-section type removal reaction tower, a third removal reaction is carried out in the third reaction section, the gas is heated by the reaction, then the gas is cooled by a third heat exchanger and then enters a fourth reaction section for a fourth catalytic removal reaction, and the obtained purified tail gas is used for supplying a heat source of the preheater.
Further, the method of decomposition comprises:
1) heating tail gas containing high-concentration laughing gas from industrial gas generation through a preheater to reach 330-;
2) carrying out the first catalytic removal reaction on the tail gas from the first reaction section of the first two-section removal reaction tower, so that the concentration of laughing gas in the tail gas is reduced to 13-26%, and the temperature of the tail gas is further increased to 500-550 ℃ due to reaction heat;
3) the gas after the first catalytic removal reaction is subjected to heat exchange through a first heat exchanger and cooled to 350-420 ℃, and then the cooled gas enters a second reaction section to be subjected to a second catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced to 9-17%, and the gas temperature is increased to 500-550 ℃ again due to the reaction heat;
4) the gas after the second catalytic removal reaction is discharged from the first two-section reaction tower, conveyed to a second heat exchanger to reduce the temperature to 350 ℃, continuously enters from the top of the second two-section removal reaction tower, and is subjected to a third catalytic removal reaction in the third reaction section, so that the concentration of laughing gas in the tail gas is reduced to 5-9%, and the gas temperature is increased to 500-;
the tail gas is continuously cooled to 330-.
Preferably, the off-gas at the outlet is used to supply heat to the preheater. More preferably, the purified exhaust gas is discharged directly from the stack after the temperature of the exhaust gas is reduced to 100 ℃ (preferably 80 ℃) or lower after the supply of heat to the preheater is achieved.
Preferably, more levels of two-stage removal reactors, preheaters and heat exchangers can be added based on the actual requirements of the use scenario of the system and method of the present invention.
Further, the sources of the tail gas comprise tail gas produced in adipic acid production and tail gas produced in caprolactam production.
The invention has the beneficial effects that:
1. the removal treatment process of the michelia gas tail gas is improved subversively, and the tail gas does not need to be diluted based on the removal process, so that the processing and maintenance costs of the reactor of the whole treatment process are greatly reduced. In the prior art, because air is needed to dilute the tail gas, the dilution ratio is 1 part of the tail gas to 3 parts of the air, so that the volume of the treatment equipment is overlarge, the processing cost is high, the safety is poor, and the maintenance cost is also high. The process can realize the direct treatment of the michelia gas tail gas, the volume of the reactor is greatly reduced, the pressure drop of the layer of the catalyst is obviously reduced, the cost of equipment addition, maintenance and repair is greatly reduced, the large-scale popularization and use are facilitated, and the investment and operation cost can be obviously reduced;
2. the invention adopts a sectional heat removal mode to remove the heat generated by the decomposition reaction, thereby not only reducing the temperature of a reaction outlet and protecting a catalyst bed layer to be always in an active and effective temperature range, but also avoiding the high-temperature sintering and inactivation phenomena caused by the extremely high temperature of the catalyst bed layer, prolonging the service life of the catalyst, ensuring the more stable exertion of the catalytic performance of the catalyst and realizing high-grade heat;
3. the invention adopts multi-stage reaction, can be beneficial to utilizing the catalyst, can change and adjust the temperature of the inlet of the reaction section and adjust the working temperature of the catalyst based on the requirement of actual working conditions, and simultaneously fully utilizes the activity performance of the catalyst and prolongs the service life of the catalyst;
4. the decomposition process has wide adaptability, a plurality of sectional reactors and corresponding heat exchangers and preheaters can be added according to specific use scenes, the whole system and the decomposition process are more flexible, and the method can be suitable for treatment processes of tail gas with different scenes, different concentrations and even different tail gases.
Drawings
FIG. 1 is a schematic diagram of one embodiment of a system according to the present invention;
FIG. 2 is a schematic view of another embodiment of the system of the present invention.
1-a first two-stage stripping reaction tower; 2-a first heat exchanger; c1-first reaction stage; c2-second reaction stage; 3-a preheater; 4-a second two-section type removal reaction tower; 5-a third heat exchanger; 6-a second heat exchanger; c3-third reaction stage; c4-fourth reaction stage.
Detailed Description
In one embodiment of the present invention, as shown in fig. 1, the system of the present invention comprises a first two-stage removal reaction tower 1, wherein a gas material inlet, a first reaction stage C1, a first heat exchanger 2 and a second reaction stage C2 are arranged in the first two-stage removal reaction tower 1 from top to bottom, and the purified gas discharged from the second reaction stage C2 enters a preheater 3 to be treated and contains high concentration N2And (4) preheating the tail gas of the O, and discharging the purified gas after cooling.
Further, the off-gas is preferably an adipic acid production off-gas and/or a caprolactam production off-gas, wherein N is2The content of O is 17-40%, preferably, N2The content of O is more than 35 percent. Wherein the tail gas is preheated by a preheater to reach the temperature of catalytic reaction activity, 330-; preferably up to 330 deg.c.
Further, the tail gas enters from the inlet of the first two-stage removal reaction tower 1, and then undergoes a first catalytic removal reaction in the first reaction stage C1, so that N in the tail gas is converted into N2The concentration of O is reduced to 13-26%, preferably to 16%.
The temperature of the gas after the first catalytic removal reaction is raised to 500-550 ℃, and the temperature of the gas after the temperature rise is lowered to 350-420 ℃ through heat exchange by a first heat exchanger 2; preferably, the temperature is reduced to 350 ℃.
And then the cooled gas enters the second reaction section C2 to perform a second catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced to 9-17%, preferably to 9%.
The gas after the second catalytic removal reaction is heated to 550 ℃ again, the heated purified tail gas is subjected to heat exchange with the tail gas to be treated in the preheater 3, and the temperature is further reduced to below 100 ℃ for emission or subsequent processes; and the tail gas to be treated is heated to the catalytic reaction temperature and continuously enters the first two-section removal reaction tower 1 to continuously carry out the removal reaction of laughing gas. Preferably, the temperature of the cleaned tail gas is reduced to below 80 ℃ after heat exchange in the preheater 3.
In another embodiment, as shown in fig. 2, the system includes a first two-stage removal reaction tower 1 and a second two-stage removal reaction tower 4, the exhaust gas to be treated is heated by the preheater 3 and enters from the inlet of the first two-stage removal reaction tower 1, then a first catalytic removal reaction is performed in the first catalytic reaction stage C1, the reaction raises the temperature of the gas, the heated gas is subjected to heat exchange and cooling in the first heat exchanger 2, and then continues to undergo a second catalytic removal reaction in the second catalytic reaction stage C2, the reaction calls for reheating the obtained gas, the warmed gas is discharged from the first two-stage removal reaction tower through a pipeline, then enters the second heat exchanger and is cooled again, enters from the inlet of the second two-stage removal reaction tower, and a third catalytic removal reaction is performed in the third catalytic reaction stage C3, and the reaction causes the gas to be heated again, the heated gas is subjected to heat exchange and cooling in the third heat exchanger 5, then the fourth catalytic removal reaction is continuously carried out in the fourth catalytic reaction section, and the purified gas enters the preheater to be exchanged with the tail gas to be treated so as to preheat the tail gas to be treated.
Further, the processing method comprises the following steps: taking tail gas produced in adipic acid production as an example, the concentration of laughing gas in the tail gas is more than 35%, and the tail gas is preheated by a preheater 3 to be heated to 330 ℃; the tail gas after being heated enters the first catalytic reaction section C1 to carry out a first catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced to 26%, and the temperature of the tail gas is increased to 550 ℃ due to reaction heat;
the temperature of the tail gas after being heated is reduced to 330 ℃ through the first heat exchanger, and then the tail gas enters the second catalytic removal reaction section C2 to carry out a second catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced from 26% to 17%, and the temperature of the tail gas is increased to 550 ℃ again due to reaction heat;
the tail gas after being heated enters the second heat exchanger 6, is cooled to 350 ℃, then enters a third catalytic removal reaction section C3 to carry out a third catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced from 17% to 9%, and the temperature of the tail gas is raised to 550 ℃ again due to reaction heat;
the tail gas after temperature rise is cooled to 330 ℃ after passing through a third heat exchanger 5, and then continuously enters a fourth catalytic removal reaction section C4 to carry out a fourth catalytic removal reaction, so that laughing gas in the tail gas is completely purified, and the outlet temperature of the tail gas reaches 550 ℃ due to reaction heat;
and conveying the tail gas at the outlet of the second two-section catalytic removal reaction tower to the preheater 3 to preheat the low-temperature tail gas to be treated at the inlet, and cooling the tail gas at the outlet to 80 ℃ after heat transfer and then discharging the tail gas through a chimney.
Furthermore, based on the difference of the content of laughing gas in the tail gas to be treated, a plurality of two-section removal reaction towers can be continuously added behind the second two-section removal reaction tower, and the tail gas temperature is increased by matching the index of the reduction of the concentration of laughing gas in the gas treatment process and the index control caused by the reaction heat, so that the operation of directly, simply and conveniently purifying the tail gas to be treated without an external heating source or the steps of diluting the tail gas to be treated is realized. In the reaction process, the heat generated by the reaction heat can be recycled to any other unit or process needing heat supply.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, but any modifications or equivalent variations made according to the technical spirit of the present invention are within the scope of the present invention as claimed.
Claims (12)
1. A method for treating exhaust gas containing a high concentration of laughing gas, the method comprising: carrying out catalytic removal reaction of laughing gas on waste gas to be treated under the catalytic action, heating the waste gas to form hot waste gas due to heat generated by catalytic reaction of laughing gas, cooling the waste gas through heat exchange treatment, and repeatedly repeating the catalytic removal of laughing gas and the heat exchange cooling of the hot waste gas until the content of laughing gas in the waste gas to be treated reaches the normal discharge standard;
the method does not need to dilute the waste gas, and directly finishes removing laughing gas in the waste gas.
2. The method as claimed in claim 1, wherein the reaction conditions are controlled such that the concentration of laughing gas in the exhaust gas to be treated decreases by 7-15% each time the catalytic removal reaction is performed, and simultaneously the temperature of the exhaust gas increases by 150-;
and repeating the catalytic removal of the laughing gas and the heat exchange and temperature reduction operation of the hot waste gas repeatedly when necessary until the content of the laughing gas in the waste gas to be treated reaches the emission standard.
3. A waste gas purification system containing high-concentration laughing gas is characterized by comprising at least one two-section type removal reaction tower, wherein the reaction tower sequentially comprises a gas inlet, a first reaction section, a first heat exchanger and a second reaction section from top to bottom; and after the temperature of tail gas containing high-concentration laughing gas is raised through a first preheater, the tail gas enters the two-section type removal reaction tower from the gas inlet, a first catalytic removal reaction is carried out in the first reaction section, then the gas after the reaction in the first reaction section is subjected to heat exchange and temperature reduction through the first heat exchanger and then enters the second reaction section for a second catalytic removal reaction, and the purified tail gas obtained after the second catalytic removal reaction is used for subsequent processes.
4. The system of claim 3, wherein the first preheater uses gas from the second reaction zone for heat exchange.
5. The system according to claim 3, wherein when the system comprises a first two-stage removal reaction tower and a second two-stage removal reaction tower, the gas discharged from the second reaction stage is cooled by a second heat exchanger, then continuously enters from the top of the second two-stage removal reaction tower, is subjected to a third catalytic removal reaction in the third reaction stage, is cooled by a third heat exchanger, and then is subjected to a fourth catalytic removal reaction in the fourth reaction stage, and the obtained purified tail gas is used for subsequent processes; preferably, the first preheater and/or the second preheater exchange heat using the cleaned off-gas discharged from the fourth reaction section.
6. The system of claim 3, wherein the system is sequentially provided with a sufficient number of two-stage removal reaction towers, heat exchangers and preheaters according to the requirement of working conditions, the system sequentially enters each two-stage removal reaction tower, heat exchanger and preheater according to the flowing direction of waste gas treatment, and finally the energy supply of the whole removal system by virtue of the laughing gas removal reaction heat is realized without additionally providing an external heating source for the system.
7. The system according to claim 5, further comprising a plurality of two-stage removal reaction towers and a plurality of heat exchangers in sequence for matching tail gas treatment processes under different working conditions.
8. A method for high concentration laughing gas decomposition using the system of claim 3 or 4, comprising:
1) heating tail gas containing high-concentration laughing gas from industrial gas generation through a preheater to reach the catalytic reaction activity temperature, and then raising the temperature of the tail gas;
2) carrying out the first catalytic removal reaction on the tail gas from the first reaction section of the first two-section removal reaction tower, wherein the temperature of the tail gas is further increased due to reaction heat;
3) the gas after the first catalytic removal reaction is subjected to heat exchange and temperature reduction through a first heat exchanger, and then the cooled gas enters a second reaction section to be subjected to a second catalytic removal reaction, and the temperature of the gas is raised again due to reaction heat;
4) and gas after the second catalytic removal reaction is discharged from the first two-section reaction tower, and purified tail gas is discharged from the first two-section reaction tower.
9. The method of claim 8, wherein the cleaned tail gas is passed to the preheater for preheating of initial tail gas.
10. The method according to claim 8, wherein when the system comprises a first two-stage removal reaction tower and a second two-stage removal reaction tower, the gas discharged from the second reaction stage is cooled by a second heat exchanger, then enters the second two-stage removal reaction tower from the top, a third removal reaction is performed in the third reaction stage, the temperature of the gas is raised by the reaction, and then the gas is cooled by a third heat exchanger and then enters the fourth reaction stage for a fourth catalytic removal reaction, and the obtained purified tail gas is used for supplying the heat source of the preheater.
11. A method for high concentration laughing gas decomposition using the system of claim 4 or 6, wherein the method comprises:
1) heating tail gas containing high-concentration laughing gas from industrial gas generation through a preheater to reach 330-;
2) carrying out the first catalytic removal reaction on the tail gas from the first reaction section of the first two-section removal reaction tower, so that the concentration of laughing gas in the tail gas is reduced to 13-26%, and the temperature of the tail gas is further increased to 500-550 ℃ due to reaction heat;
3) the gas after the first catalytic removal reaction is subjected to heat exchange through a first heat exchanger and cooled to 350-420 ℃, and then the cooled gas enters a second reaction section to be subjected to a second catalytic removal reaction, so that the concentration of laughing gas in the tail gas is reduced to 9-17%, and the gas temperature is increased to 500-550 ℃ again due to the reaction heat;
4) the gas after the second catalytic removal reaction is discharged from the first two-section reaction tower, conveyed to a second heat exchanger to reduce the temperature to 350 ℃, continuously enters from the top of the second two-section removal reaction tower, and is subjected to a third catalytic removal reaction in the third reaction section, so that the concentration of laughing gas in the tail gas is reduced to 5-9%, and the gas temperature is increased to 500-;
the tail gas is continuously cooled to 330-.
12. The method according to claim 11, wherein the tail gas at the outlet is used to supply heat to the preheater; more preferably, the purified tail gas can be directly discharged from the chimney after the temperature of the tail gas is reduced to below 100 ℃ after the heat of the tail gas is supplied to the preheater.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114159969A (en) * | 2021-12-14 | 2022-03-11 | 北京工业大学 | System and method for cyclic catalytic decomposition of high-concentration laughing gas |
| CN114699911A (en) * | 2022-04-11 | 2022-07-05 | 苏州晶拓半导体科技有限公司 | Ozone destruction device based on heat recovery and ozone destruction method thereof |
| CN114832615A (en) * | 2022-04-01 | 2022-08-02 | 开滦能源化工股份有限公司 | Method and device for catalyzing decomposition of nitrous oxide |
| CN114984749A (en) * | 2022-06-08 | 2022-09-02 | 江苏航天惠利特环保科技有限公司 | Efficient and economical nitrous gas emission reduction process method |
| CN114984750A (en) * | 2022-06-08 | 2022-09-02 | 江苏航天惠利特环保科技有限公司 | Heat exchange reaction emission reduction method of nitrous gas fixed bed |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114159969A (en) * | 2021-12-14 | 2022-03-11 | 北京工业大学 | System and method for cyclic catalytic decomposition of high-concentration laughing gas |
| CN114159969B (en) * | 2021-12-14 | 2022-11-08 | 北京工业大学 | System and method for cyclic catalytic decomposition of high-concentration laughing gas |
| CN114832615A (en) * | 2022-04-01 | 2022-08-02 | 开滦能源化工股份有限公司 | Method and device for catalyzing decomposition of nitrous oxide |
| CN114699911A (en) * | 2022-04-11 | 2022-07-05 | 苏州晶拓半导体科技有限公司 | Ozone destruction device based on heat recovery and ozone destruction method thereof |
| CN114984749A (en) * | 2022-06-08 | 2022-09-02 | 江苏航天惠利特环保科技有限公司 | Efficient and economical nitrous gas emission reduction process method |
| CN114984750A (en) * | 2022-06-08 | 2022-09-02 | 江苏航天惠利特环保科技有限公司 | Heat exchange reaction emission reduction method of nitrous gas fixed bed |
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