CN111530281A - Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis - Google Patents
Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis Download PDFInfo
- Publication number
- CN111530281A CN111530281A CN202010407669.8A CN202010407669A CN111530281A CN 111530281 A CN111530281 A CN 111530281A CN 202010407669 A CN202010407669 A CN 202010407669A CN 111530281 A CN111530281 A CN 111530281A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- ddbd
- reactor
- temperature plasma
- low
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000006555 catalytic reaction Methods 0.000 title abstract description 7
- 230000002153 concerted effect Effects 0.000 title abstract description 6
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000012494 Quartz wool Substances 0.000 claims abstract description 5
- -1 polytetrafluoroethylene Polymers 0.000 claims abstract description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims abstract description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000010453 quartz Substances 0.000 claims description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 229910052593 corundum Inorganic materials 0.000 claims description 6
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 4
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 239000011889 copper foil Substances 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 2
- 239000011521 glass Substances 0.000 claims description 2
- 239000006227 byproduct Substances 0.000 abstract description 18
- 229910003158 γ-Al2O3 Inorganic materials 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 210000002381 plasma Anatomy 0.000 description 38
- 229910021529 ammonia Inorganic materials 0.000 description 28
- 239000001301 oxygen Substances 0.000 description 19
- 229910052760 oxygen Inorganic materials 0.000 description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 18
- 239000007789 gas Substances 0.000 description 13
- 230000004888 barrier function Effects 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- WJCNZQLZVWNLKY-UHFFFAOYSA-N thiabendazole Chemical compound S1C=NC(C=2NC3=CC=CC=C3N=2)=C1 WJCNZQLZVWNLKY-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 239000003989 dielectric material Substances 0.000 description 1
- 238000010891 electric arc Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
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
- B01D53/8634—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/2073—Manganese
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/209—Other metals
- B01D2255/2092—Aluminium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/80—Employing electric, magnetic, electromagnetic or wave energy, or particle radiation
- B01D2259/818—Employing electrical discharges or the generation of a plasma
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention belongs to the technical field of low-temperature plasma and the field of malodorous pollution treatment, and particularly relates to a method and equipment for removing ammonia gas by low-temperature plasma concerted catalysis, wherein a DDBD low-temperature plasma reactor comprises: the plasma reactor has a double-layer tubular structure and comprises an inner tube, an outer tube, a discharge electrode and a grounding electrode; the discharge electrode covers the outer surface of the outer pipe, the grounding electrode is arranged on the inner side of the inner pipe, and the outer pipe and the inner pipe are fixed through a polytetrafluoroethylene plug; the two ends of the outer pipe are provided with an air inlet and an air outlet, and the gap part between the outer pipe and the inner pipe is completely or partially filled with a catalyst; the catalyst is gamma-Al2O3Catalyst or MnO2And the catalyst is supported and fixed by quartz wool. By using the plasma reactor, the ammonia gas removal rate and the system energy efficiency are higher, and O can be obviously inhibited3By-products and NOxThe production of by-products has good industrial applicability.
Description
Technical Field
The invention belongs to the technical field of low-temperature plasmas and the field of malodorous pollution treatment, and particularly relates to a method and equipment for removing ammonia gas by low-temperature plasma concerted catalysis.
Background
Ammonia gas is a common inorganic malodorous substance in atmospheric environment and mainly comes from domestic garbage landfill sites, composting plants, wastewater treatment centers, animal husbandry, pig farms and the like. Emission of ammonia gas without proper treatment causes malodor nuisance and threatens human health, and thus facilities or sites of relevant emission sources of ammonia gas are often complained by residents of neighboring communities. Many technologies, including solution absorption, adsorption, pyrolysis, biofiltration, etc., have been developed and applied so far to reduce ammonia emission, but these technologies are often limited by operating conditions or economic cost.
In recent years, low temperature plasma deodorization has attracted much attention and is considered to be a clean and effective method for removing atmospheric pollutants. The low-temperature plasma technology generates a large amount of active substances (ozone, hydroxyl radical, oxygen radical and the like) and various atoms to decompose and oxidize malodorous gases through high-voltage discharge. Among the related devices applied in the environmental protection field, low-temperature plasma is mainly generated by means of corona discharge, glow discharge, spark discharge, arc discharge, dielectric barrier discharge, and the like, wherein dielectric barrier discharge and corona discharge are the most common. The Dielectric Barrier Discharge is classified into Single Dielectric Barrier Discharge (SDBD) and Double Dielectric Barrier Discharge (DDBD) according to the number of dielectrics, in which DDBD Discharge is more uniform, generation of arc can be prevented, and contamination of the inner electrode by corrosive gas can be prevented, thereby having more engineering practicability. Although the DDBD low-temperature plasma has a high ammonia removal rate, a high voltage is often required to be applied to ensure the high ammonia removal rate in the actual operation process, so that the system energy efficiency is low, and O is inevitably generated in the ammonia removal process of the DDBD3And NOxAnd the like, which limits the industrial application of the technology.
Disclosure of Invention
Technical problem to be solved by the invention
The invention is based on DDBD low-temperature plasma, and two different catalysts (gamma-Al)2O3And MnO2) Respectively combined with DDBD low-temperature plasmas to remove ammonia gas, compared with a single DDBD plasma system, the plasma catalytic system has higher ammonia gas removal rate and energy efficiency, and simultaneously obviously inhibits O3And NOxEtc. by-product generation.
Means for solving the technical problem
In order to solve the problems, the invention provides a DDBD low-temperature plasma reactor and a DDBD low-temperature plasma ammonia gas removal method.
A DDBD low temperature plasma reactor, comprising: the plasma reactor has a double-layer tubular structure and comprises an inner tube, an outer tube, a discharge electrode and a grounding electrode, wherein the discharge electrode covers the outer surface of the outer tube, the grounding electrode is arranged on the inner side of the inner tube, the outer tube and the inner tube are fixed through polytetrafluoroethylene plugs, air inlets and air outlets are formed in two ends of the outer tube, and a catalyst is filled in all or part of a gap between the outer tube and the inner tube.
In one embodiment, the inner tube and the outer tube are made of quartz tubes, glass tubes or ceramic tubes, each quartz tube being in contact with one electrode.
One embodiment is that, the inner tube and the outer tube are cylindrical quartz tubes, and the discharge gap between the inner tube and the outer tube is 3-5 mm.
In one embodiment, the catalyst is γ -Al2O3Catalyst or MnO2A catalyst.
One embodiment is wherein the discharge electrode is made of copper foil and the ground electrode is made of copper threaded rod.
According to a second aspect of the present invention, there is provided a DDBD low temperature plasma reaction device, comprising a voltage regulator, a high voltage high frequency ac power supply and the above DDBD low temperature plasma reactor.
According to a third aspect of the present invention, there is provided a method of plasma removing ammonia gas, wherein the plasma removing is carried out in the presence of a catalyst.
In one embodiment, the catalyst is γ -Al2O3Catalyst or MnO2The catalyst is supported and fixed by quartz wool.
According to a fourth aspect of the present invention, there is provided a method for removing ammonia gas by using plasma, wherein the plasma reaction apparatus is used, ammonia gas with a specified concentration is introduced through the gas inlet, a voltage regulator and a high-voltage high-frequency ac power supply are controlled to generate stable low-temperature plasma in the plasma reactor, and the treated gas is discharged through the gas outlet.
The invention has the advantages of
Compared with the technology of removing ammonia gas by using a single DDBD reactor, the method has the following advantages:
1. higher removal rate and energy efficiency
As shown in FIGS. 2 and 3, under the conditions of an initial ammonia concentration of 100ppm, an ammonia flow rate of 2L/min and an input power of 28.98w, when the oxygen content is 0%, the DDBD is combined with gamma-Al2O3The removal rate of ammonia gas is 70.68 percent, and the energy efficiency of the system is 3.58 × 10-6mol/KJ is 1.7 times of that of single DDBD; DDBD combined MnO2The removal rate of ammonia gas is 58.00 percent, and the energy efficiency of the system is 2.78 × 10-6mol/KJ, which is 1.3 times of that of DDBD alone.
2. Obviously inhibit O while ensuring high ammonia gas removal rate3The production of by-products.
As shown in FIGS. 2 and 3, under the conditions of an initial ammonia concentration of 100ppm, an ammonia flow rate of 2L/min and an input power of 28.98w, when the oxygen content is 5-20%, the DDBD is combined with gamma-Al2O3DDBD combined MnO2The removal rate of the DDBD alone to the ammonia gas is 100 percent, and the energy efficiency of the system is 4.79 × 10-6mol/KJ. As shown in FIG. 4, when the oxygen content is 5-20%, O3The byproduct production amount is DDBD combined with gamma-Al2O3Association MnO of DDBD2DDBD alone. Wherein, when the oxygen content is 20%, the single DDBD produces O3At a concentration of 525ppm, and DDBD in combination with MnO2O of (A) to (B)3DDBD combined with gamma-Al at a concentration of 45ppm2O3O of (A) to (B)3Concentrations of 12ppm were all significantly lower than the DDBD alone system.
3. The formation of NOx by-products is significantly suppressed.
As shown in FIG. 5, when the oxygen content is 5-20% under the conditions of an initial ammonia concentration of 100ppm, an ammonia flow rate of 2L/min and an input power of 28.98w, the amount of NOx by-product production is DDBD combined with γ -Al2O3 less than DDBD combined with MnO2 less than DDBD alone. Wherein, at an oxygen content of 20%, DDBD alone produced a NOx concentration of 442ppm, while DDBD in combination with MnO2 produced a NOx concentration of 41ppm and DDBD in combination with γ -Al2O3 produced a NOx concentration of 23ppm, all significantly lower than the DDBD alone system.
Further features of the present invention will become apparent from the following description of exemplary embodiments.
Drawings
FIG. 1 is a device for removing ammonia gas by low-temperature plasma concerted catalysis;
FIGS. 2-3 are the removal rate and energy efficiency of low temperature plasma in conjunction with catalytic removal of ammonia;
FIG. 4 shows the formation of O in the co-catalysis of low temperature plasma to remove ammonia3Concentration;
FIG. 5 shows the generation of NO when ammonia is removed by low temperature plasma concerted catalysisxAnd (4) concentration.
1-a voltage regulator; 2-high voltage high frequency alternating current power supply; 3-double dielectric barrier discharge plasma reactor; 4-quartz wool; 5-catalyst
Detailed Description
One embodiment of the present disclosure will be specifically described below, but the present disclosure is not limited thereto.
The invention aims to solve the problems of low energy efficiency and O generation in the process of removing ammonia gas by DDBD low-temperature plasma3And NOxAnd waiting for the problem of byproducts, and specifically implementing the following steps:
establishment of DDBD Low-temperature plasma reaction System
The DDBD low-temperature plasma reaction system used in the present invention includes a voltage regulator, a high-voltage high-frequency ac power supply, and a DDBD low-temperature plasma reactor, as shown in fig. 1. The plasma reactor had a double-layered tubular structure using two cylindrical quartz tubes each in contact with one electrode as a dielectric. The inner tube (external diameter 8mm, thickness 1mm, length 450mm) is close to telluric electricity field, and the surface of outer tube (19mm, thickness 1.5mm, length 360mm) contacts with the discharge electrode who is connected the power, and the discharge clearance of inner tube and outer tube is 4 mm. The discharge electrode is made of copper foil (thickness 0.1mm, length 200mm), the grounding electrode is made of copper threaded rod (4mm x 500mm), and the two ends of the outer tube are designed with an air inlet and an air outlet.
Establishment of a catalyst System combining DDBD with Gamma-Al 2O3
2 g of gamma-Al2O3The catalyst is uniformly added into a plasma discharge area (between the outer tube and the inner tube) and is supported and fixed by quartz wool.
Establishment of a catalyst System for DDBD in combination with MnO2
The method is the same as the step 2, and the catalyst is replaced by MnO2。
Removal of ammonia gas by DDBD combined catalyst system
Respectively in combination with gamma-Al on DDBD2O3Catalyst system and DDBD in combination with MnO2Introducing ammonia gas with specified concentration into the catalyst system, controlling a pressure regulator and a high-voltage high-frequency alternating-current power supply to generate stable low-temperature plasma in a plasma reactor, measuring the concentration change of the ammonia gas before and after reaction, calculating the removal rate and energy efficiency of the ammonia gas, and measuring O in the reaction process3And NOxThe formation concentration of (2).
Examples
The present invention is described in more detail by way of examples, but the present invention is not limited to the following examples.
Example 1
Low temperature plasma was generated in the DDBD reactor using a voltage regulator (0-250V) and a high voltage high frequency ac power supply (CTP-2000K, suhman electronics, tokyo). Selecting ammonia as experimental gas, wherein the initial concentration of the ammonia is 100ppm, and adopting N2As an equilibrium gas. The ammonia concentration is detected in real time by an ammonia detector (LH-901), and a reaction byproduct O is generated3NO measured by ozone Analyzer (ECO UV-100)xOn-line detection was performed by a smoke analyzer (TESTO 350). At a constant frequency of 9.125KHz and a fixed flow rate of 2L/min, the O is added to the gas distribution system2Selecting 5 different oxygen contents of 0%, 5%, 10%, 15% and 20%, respectively comparing ammonia gas in single DDBD reactor and DDBD combined gamma-Al2O3Removal rate between catalyst systems, energy efficiencyAnd the difference between the formation of byproducts.
The ammonia gas removal rate calculation formula is as follows:
the system energy efficiency calculation formula is as follows:
wherein [ NH ]3]inIs the ammonia concentration at the inlet, ppm; [ NH ]3]outThe concentration of ammonia gas at the gas outlet is ppm; q is the flow rate of ammonia gas, L/min; p is input power, w; vmIs the gas molar volume, L/mol.
As shown in FIGS. 2 and 3, at an input power of 28.98w, when the oxygen content is 0%, the DDBD is combined with gamma-Al2O3The ammonia removal rate of the catalyst system was 70.68%, and the energy efficiency was 3.58 × 10-6mol/KJ, ammonia removal rate of 43.86% for DDBD reactor alone, and energy efficiency of 2.10 × 10-6mol/KJ, DDBD combined with gamma-Al2O3The ammonia removal rate and energy efficiency of the catalyst system are significantly higher than the DDBD alone.
As shown in FIG. 4, DDBD combined with γ -Al when the oxygen content was 5-20%2O3By-product O of the catalyst system3The concentration was significantly lower than in the DDBD reactor alone. O production from DDBD reactor alone when oxygen content was 20%3The concentration was 525ppm and DDBD combined with gamma-Al2O3O produced by the catalyst system3The concentration was 12 ppm.
As shown in FIG. 5, DDBD combined with γ -Al when the oxygen content was 5-20%2O3By-product NO produced by the catalyst systemxThe concentration was significantly lower than in the DDBD reactor alone. NO produced by DDBD reactor alone when oxygen content was 20%xThe concentration was 442ppm, and DDBD was associated with gamma-Al2O3NO produced by the catalyst systemxThe concentration was 23 ppm.
Example 2
Low temperature plasma was generated in the DDBD reactor using a voltage regulator (0-250V) and a high voltage high frequency ac power supply (CTP-2000K, suhman electronics, tokyo). Selecting ammonia as experimental gas, wherein the initial concentration of the ammonia is 100ppm, and adopting N2As an equilibrium gas. The ammonia concentration is detected in real time by an ammonia detector (LH-901), and a reaction byproduct O is generated3NO measured by ozone Analyzer (ECO UV-100)xOn-line detection was performed by a smoke analyzer (TESTO 350). At a constant frequency of 9.125KHz and a fixed flow rate of 2L/min, the O is added to the gas distribution system2Selecting 5 different oxygen contents of 0%, 5%, 10%, 15% and 20%, respectively comparing ammonia gas in single DDBD reactor and DDBD combined MnO2The difference between the removal rate, energy efficiency and by-product formation between catalyst systems. The ammonia removal rate and system energy efficiency calculation method were the same as in example 1.
As shown in FIGS. 2 and 3, at an input power of 28.98w, when the oxygen content is 0%, the DDBD is combined with MnO2The ammonia removal rate of the catalyst system was 58.00%, and the energy efficiency was 2.78 × 10-6mol/KJ, ammonia removal rate of 43.86% for DDBD reactor alone, and energy efficiency of 2.10 × 10-6mol/KJ, DDBD combined MnO2The ammonia removal rate and energy efficiency of the catalyst system are significantly higher than the DDBD alone.
As shown in FIG. 4, DDBD combined with MnO when oxygen content was 5-20%2By-product O of the catalyst system3The concentration was significantly lower than in the DDBD reactor alone. O production from DDBD reactor alone when oxygen content was 20%3At a concentration of 525ppm, and DDBD in combination with MnO2O produced by the catalyst system3The concentration was 45 ppm.
As shown in FIG. 5, DDBD combined with MnO when oxygen content was 5-20%2By-product NO produced by the catalyst systemxThe concentration was significantly lower than in the DDBD reactor alone. NO produced by DDBD reactor alone when oxygen content was 20%xAt a concentration of 442ppm, and DDBD in combination with MnO2NO produced by the catalyst systemxThe concentration was 41 ppm.
Industrial applicability
The plasma reactor has higher removal rate and energy efficiency, obviously inhibits the generation of O3 byproducts and NOx byproducts while ensuring high ammonia gas removal rate, and has good industrial practicability.
The present invention is not limited to the above embodiments, and any changes or substitutions that can be easily made by those skilled in the art within the technical scope of the present invention are also within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (9)
1. A DDBD low-temperature plasma reactor, comprising: the plasma reactor has a double-layer tubular structure and comprises an inner tube, an outer tube, a discharge electrode and a grounding electrode, wherein the discharge electrode covers the outer surface of the outer tube, the grounding electrode is arranged on the inner side of the inner tube, the outer tube and the inner tube are fixed through polytetrafluoroethylene plugs, air inlets and air outlets are formed in two ends of the outer tube, and a catalyst is filled in all or part of a gap between the outer tube and the inner tube.
2. The reactor of claim 1, wherein the inner and outer tubes are quartz, glass or ceramic tubes, each quartz tube being in contact with one electrode.
3. The reactor of claim 1, wherein the inner tube and the outer tube are cylindrical quartz tubes, and a discharge gap between the inner tube and the outer tube is 3-5 mm.
4. The reactor of claim 1, wherein the catalyst is γ -Al2O3Catalyst or MnO2A catalyst.
5. The reactor of claim 1, wherein the discharge electrode is made of copper foil and the ground electrode is made of copper threaded rod.
6. A DDBD low temperature plasma reaction device comprising a voltage regulator, a high voltage high frequency ac power supply and a DDBD low temperature plasma reactor according to any one of claims 1-5.
7. A method for plasma removal of ammonia gas, characterized in that the plasma removal is carried out in the presence of a catalyst.
8. The process of claim 7, wherein the catalyst is γ -Al2O3Catalyst or MnO2The catalyst is supported and fixed by quartz wool.
9. A method for removing ammonia gas by plasma is characterized in that the plasma reaction device of claim 6 is used, ammonia gas with specified concentration is introduced through a gas inlet, a voltage regulator and a high-voltage high-frequency alternating-current power supply are controlled to generate stable low-temperature plasma in a plasma reactor, and the treated gas is discharged through a gas outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010407669.8A CN111530281A (en) | 2020-05-14 | 2020-05-14 | Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010407669.8A CN111530281A (en) | 2020-05-14 | 2020-05-14 | Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111530281A true CN111530281A (en) | 2020-08-14 |
Family
ID=71969285
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010407669.8A Pending CN111530281A (en) | 2020-05-14 | 2020-05-14 | Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111530281A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113440989A (en) * | 2021-08-11 | 2021-09-28 | 河南三棵树新材料科技有限公司 | Dielectric barrier discharge reactor for in-situ purification of pollutants by carbon nano tube and application |
| CN113444549A (en) * | 2021-07-08 | 2021-09-28 | 重庆大学 | Low-temperature plasma reactor, and device and method for producing hydrogen by concerted catalysis |
| CN113828252A (en) * | 2021-09-22 | 2021-12-24 | 湖南大学 | Novel efficient reaction device for preparing ammonia by low-temperature plasma concerted catalysis |
| CN114918242A (en) * | 2022-05-07 | 2022-08-19 | 浙江大学 | Micro-plastic contaminated soil remediation device and method based on coaxial DBD plasma technology |
-
2020
- 2020-05-14 CN CN202010407669.8A patent/CN111530281A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113444549A (en) * | 2021-07-08 | 2021-09-28 | 重庆大学 | Low-temperature plasma reactor, and device and method for producing hydrogen by concerted catalysis |
| CN113440989A (en) * | 2021-08-11 | 2021-09-28 | 河南三棵树新材料科技有限公司 | Dielectric barrier discharge reactor for in-situ purification of pollutants by carbon nano tube and application |
| CN113828252A (en) * | 2021-09-22 | 2021-12-24 | 湖南大学 | Novel efficient reaction device for preparing ammonia by low-temperature plasma concerted catalysis |
| CN114918242A (en) * | 2022-05-07 | 2022-08-19 | 浙江大学 | Micro-plastic contaminated soil remediation device and method based on coaxial DBD plasma technology |
| CN114918242B (en) * | 2022-05-07 | 2023-06-23 | 浙江大学 | Microplastic polluted soil restoration device and method based on coaxial DBD plasma technology |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111530281A (en) | Method and equipment for removing ammonia gas through low-temperature plasma concerted catalysis | |
| Mizuno | Industrial applications of atmospheric non-thermal plasma in environmental remediation | |
| Bahri et al. | Impact of design parameters on the performance of non-thermal plasma air purification system | |
| KR930008083B1 (en) | Reactive bed plasma air purification | |
| RU2711203C2 (en) | Air filtration and disinfection system by means of plasma injection | |
| Du et al. | Decomposition of volatile organic compounds using corona discharge plasma technology | |
| Liang et al. | Experimental studies of removing typical VOCs by dielectric barrier discharge reactor of different sizes | |
| US11285234B2 (en) | Exhaust air odor removal system | |
| Ma et al. | Decomposition of benzene using a pulse-modulated DBD plasma | |
| CN110624372A (en) | Method for treating VOCs (volatile organic chemicals) by using low-temperature plasma jet | |
| US6576573B2 (en) | Atmospheric pressure plasma enhanced abatement of semiconductor process effluent species | |
| US6905577B1 (en) | Method for oxidation of volatile organic compounds contained in gaseous effluents and device thereof | |
| JP2010137212A (en) | Apparatus for generating plasma | |
| KR20180129490A (en) | High-voltage pulsed power, Plasma reactor, apparatus and method for removing contamination air | |
| JP2006187766A (en) | Gas treatment apparatus and gas treatment cartridge | |
| Du et al. | Plasma purification of halogen volatile organic compounds | |
| Yamamoto et al. | Nonthermal plasma processing for controlling volatile organic compounds | |
| US6395144B1 (en) | Method for treating toxic compounds-containing gas by non-thermal plasma | |
| US20060119278A1 (en) | Gas decomposition apparatus and gas treatment cartridge | |
| KR101817907B1 (en) | Apparatus for eliminating stink and harzardous gas | |
| JP2002177734A (en) | Ultra-short pulse high voltage applying-type gas cleaning apparatus | |
| Chaichanawong et al. | High-temperature simultaneous removal of acetaldehyde and ammonia gases using corona discharge | |
| CN108970363B (en) | Interval type low-temperature plasma generator filled with ozone decomposer | |
| KR101174137B1 (en) | A device treating air pollutants with plasma | |
| Li et al. | Decomposition of toluene by using a streamer discharge reactor combined with catalysts |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |