CN1506300A - Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn - Google Patents
Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn Download PDFInfo
- Publication number
- CN1506300A CN1506300A CNA021559449A CN02155944A CN1506300A CN 1506300 A CN1506300 A CN 1506300A CN A021559449 A CNA021559449 A CN A021559449A CN 02155944 A CN02155944 A CN 02155944A CN 1506300 A CN1506300 A CN 1506300A
- Authority
- CN
- China
- Prior art keywords
- catalyzer
- ruthenium
- carrier
- auxiliary agent
- ammonia
- 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
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The catalyst includes Ru as main active component; carrier CaO, MgO, TiO2, SiO2, Al2O3 or active carbon, preferably active carbon; and one or several selected from IA, IIA, IIIA, IVA, IIIB or RE elements, preferably Mg or Ba and assistant. Compared with available industrial Ni-base catalyst, the present invention has ammonia discomposing temperature lowered by 150-250 deg.c, greatly lowered catalyst loading amount, greatly reduced apparatus volume, obviously lowered power consumption, and less corrosion of apparatus.
Description
Technical field
The present invention relates to a kind of preparing hydrogen by ammonia decomposition nitrogen mixed gas catalyzer, relate in particular to a kind of ruthenium base preparing hydrogen by ammonia decomposition nitrogen mixed gas catalyzer.
The invention still further relates to a kind of method for preparing above-mentioned catalyzer.
The invention still further relates to the application of above-mentioned catalyzer in the preparing hydrogen by ammonia decomposition nitrogen mixed gas.
Background technology
Ammonia decomposition catalyzer is mainly used in field of environment protection and reducing gas, protection gas field.At field of environment protection, usually the purpose that alleviates environmental pollution to reach is recycled or discharged to the gas mixture that makes wherein contained ammonia be decomposed into nontoxic hydrogen and nitrogen by ammonia decomposition catalyzer refinery gas and coke(oven)gas; In reducing gas, protection gas field, the hydrogen nitrogen mixed gas that is produced through catalytic decomposition by ammonia can further separate produces pure hydrogen, also can directly be widely used in industries such as float glass, powder metallurgy, electronics as reducing gas or protection gas.
Described in Chinese patent CN 1031636C, though the ferrum-based catalyst decomposition temperature that use in early stage ammonia decomposition field is lower, catalyst stability is bad, and the life-span had only about one month.What generally used at present domestic and international ammonia catalytic decomposition hydrogen manufacturing nitrogen mixed gas field is traditional nickel-base catalyst.The use temperature of this catalyzer is about 800 ℃ to 900 ℃, and the charging air speed of raw material ammonia is generally 600h
-To 1000h
-Described in Chinese patent CN 1031636C, this catalyst series generally under 800 ℃ temperature of reaction in the reaction end gas residual ammonia content be about 800ppm.Though existing Ni-based ammonia decomposition catalyzer is compared the advantage with good stability with ferrum-based catalyst, but still have that ammonia decomposition temperature height, energy consumption are big, per volume of catalyst treatment capacity introductory note plays that equipment is huge, running cost and device fabrication cost height, the decomposition temperature height causes that equipment energy consumption is big, shortcoming such as perishable
Chinese patent CN 1245737A has introduced a kind of Al
2O
3Or MgO is the molybdenum nickel ammonia decomposition catalyzer of carrier, is 650 ℃ in temperature of reaction, and the ammonia air speed is 900h
-The time tail gas in residual ammonia concentration can reach 700ppm; In temperature of reaction is 700 ℃, and the ammonia air speed is 1800h
-The time tail gas in residual ammonia concentration can reach 600ppm; In temperature of reaction is 650 ℃, and the ammonia air speed is 1800h
-The time tail gas in residual ammonia concentration can reach 3300ppm.This catalyzer is compared with traditional nickel above-mentioned is catalyst based, and the ammonia decomposition temperature decreases, and the ammonia air speed also increases to some extent.
Summary of the invention
The object of the present invention is to provide a kind of ruthenium base preparing hydrogen by ammonia decomposition nitrogen mixed gas catalyzer.
Another object of the present invention is to provide a kind of above-mentioned Preparation of catalysts method.
For achieving the above object, ruthenium base preparing hydrogen by ammonia decomposition nitrogen mixed gas catalyzer provided by the invention is made up of main active constituent ruthenium, one or more auxiliary agents and carrier.Ruthenium weight percentage in the catalyzer is 0.1-10%, and best ruthenium weight percentage is 1-5%; Used carrier can be CaO, MgO, TiO
2, SiO
2, Al
2O
3Or a kind of in the gac, preferable support of the catalyst is SiO
2, Al
2O
3Or gac, best carrier is a gac.Adjuvant used is in IA, IIA, IIIA, IVA, IIIB or rare earth element such as Li, Na, K, Mg, Ca, Ba, B, Ga, In, Sn, Y, La, Ce, Pr, Nd and the compound thereof one or more, preferable auxiliary agent is Mg, Ba, K, Y, La or Ce and compound thereof, is the best with Mg and Ba wherein.Preferable adjuvant component weight percentage is: 0.1-30%, best auxiliary agent weight percentage is: 1-8%.
Method for preparing catalyst provided by the present invention can be undertaken by following step:
(a) contain the solution impregnating carrier of Ru;
(b) carrier drying or the roasting that step a is obtained;
(c) carrier that step b is obtained is put into alkaline solution and is soaked, and makes the compound of Ru and alkali reaction generate Ru (OH)
3, Ru can not run off with ionic species during reduction; Can stir in the process of soaking;
(d) carrier that step c the is obtained aqueous solution of putting into formaldehyde or hydrazine soaks, and can stir in the process of immersion;
(e) carrier that steps d is obtained is put into deionized water and is soaked, and can stir in the process of immersion; Soak the certain hour hypsokinesis phase of anhydrating;
(f) repeating step e repeatedly;
(g) carrier drying that is loaded with ruthenium or the roasting that step f is obtained;
(h) aqueous solution that will contain auxiliary agent is supported on the carrier that is loaded with ruthenium that step g obtains;
(i) the catalyzer drying or the roasting that are loaded with ruthenium and auxiliary agent that step h are obtained.
Among the above-mentioned preparation method, can support auxiliary agent behind the first supported ruthenium, also can support supported ruthenium behind the auxiliary agent earlier, also ruthenium component and auxiliary agent can be supported on the carrier simultaneously, wherein to support the method best results of auxiliary agent behind the first supported ruthenium.
Above-mentioned Ru as catalyzer master active constituent can derive from compound and the solution thereof of any Ru of containing, and preferable ruthenium source is RuCl
3The aqueous solution.
Among the above-mentioned preparation method, the preferable source of compounding agent solution is the aqueous solution of carbonate.
Drying was carried out under 20-200 ℃ 1-24 hour usually in the above-mentioned catalyst preparation process, and roasting was carried out under 200-900 ℃ 1-24 hour usually.
Catalyzer provided by the present invention is active for improving, and can before use or before supporting auxiliary agent the ruthenium on the carrier be reduced.Reduction can be adopted the method for vapour phase reduction, also can adopt the method for liquid-phase reduction.Vapour phase reduction can be made reductive agent with hydrogen or hydrogeneous gas mixture.Liquid-phase reduction can adopt formaldehyde or hydrazine and the aqueous solution thereof to make reductive agent.
Catalyzer provided by the present invention is active for improving, and need adopt in catalyst preparation process or before using and with the method for deionized water wash the part or all of chlorine on the catalyzer be removed.
Catalyzer provided by the invention is applied in the preparing hydrogen by ammonia decomposition nitrogen mixed gas, the catalyzer that provides than patent present industrial use and above-mentioned is provided has lower ammonia decomposition temperature, higher ammonia charging air speed and the lower residual ammonia content of tail gas.
Embodiment
Below by example technology of the present invention is described further.
Example 1
The preparation method of catalyzer " A ":
Catalyzer " A " consists of Ru/Mg/Al
2O
3, Ru: Mg: Al
2O
3=4: 4: 92 (weight ratio).The preparation process of catalyzer " A " is as follows:
(a) to contain the RuCl of 0.4g Ru
3Aqueous solution 12ml dipping 9.2g carrier A l2O3, then in 110 ℃ of dryings 4 hours, then roasting 6 hours in 600 ℃ of air atmospheres;
(b) carrier that is soaked with Ru that obtains with the magnesiumcarbonate aqueous solution 12ml impregnation steps (a) that contains 0.4gMg;
(c) catalyzer that step (b) is obtained is in 110 ℃ of dryings 4 hours, and then roasting 6 hours in 600 ℃ of air atmospheres obtains catalyzer " A ".
Example 2
Catalyzer " B " consists of Ru/Mg/SiO
2, Ru: Mg: SiO
2=4: 4: 92 (weight ratio).The preparation process of catalyzer " B " is identical with catalyzer " A ".
Example 3
Catalyzer " C " consists of the Ru/Mg/ gac, Ru: Mg: gac=4: 4: 92 (weight ratio).The preparation process of catalyzer " C " is as follows:
(a) to contain the RuCl of 0.4g Ru
3Aqueous solution 18ml dipping 9.2g carrier active carbon, then in 110 ℃ of dryings 4 hours;
(b) carrier that is soaked with Ru that obtains with the magnesiumcarbonate aqueous solution 18ml impregnation steps (a) that contains 0.4gMg;
(c) catalyzer that step (b) is obtained obtains catalyzer " C " in 110 ℃ of dryings 4 hours.
Example 4
Catalyzer " D " consists of the Ru/K/ gac, Ru: K: gac=4: 4: 92 (weight ratio).The source of K is a salt of wormwood, and the preparation process of catalyzer " D " is identical with catalyzer " C ".
Example 5
Catalyzer " E " is formed identical with catalyzer " C ".The preparation process of catalyzer " E " is as follows:
(a) to contain the RuCl of 0.4g Ru
3Aqueous solution 18ml dipping 9.2g carrier active carbon;
What (b) step (a) is obtained is soaked with RuCl
3The carrier of the aqueous solution in 110 ℃ of dryings 4 hours;
(c) carrier that is loaded with the Ru component that step (b) is obtained is put into 80 ℃ the NaOH aqueous solution and stir to be soaked 1 hour.
(d) carrier that is loaded with the Ru component that step (c) the is obtained aqueous solution of putting into 80 ℃ formaldehyde stir to soak 1 hour.
(e) carrier that is loaded with the Ru component that step (d) is obtained is put into 80 ℃ deionized water for stirring and was soaked the phase of anhydrating of inclining then 1 hour.
(f) on the gac that is loaded with ruthenium that obtains with the aqueous solution 18ml impregnation steps (e) of the salt of wormwood that contains 0.4g K, and obtained catalyzer " E " in 4 hours in 110 ℃ of dryings.
Example 6
Catalyzer " F " consists of the Ru/Ba/ gac, Ru: Ba: gac=4: 4: 92 (weight ratio).The source of Ba is a barium carbonate.The preparation process of catalyzer " F " is identical with catalyzer " E ".
Example 7
Catalyzer " G " consists of the Ru/Y/ gac, Ru: Y: gac=4: 4: 92 (weight ratio).The source of Y is a ytterbium nitrate.The preparation process of catalyzer " G " is identical with catalyzer " E ".
The catalytic performance such as the table 1 of above-mentioned catalyzer.
Table 1 different catalysts is to the catalytic performance of preparing hydrogen by ammonia decomposition nitrogen mixed gas
Catalyst A B C D E F G
The residual ammonia 6,740 3,350 1,270 2,160 920 800 1210 of tail gas
Content
/ppm(V)
Annotate: temperature of reaction: 550 ℃; Reaction pressure: normal pressure; Ammonia charging air speed 3000h
-
Example 8
Table 2 has provided catalyzer " F " at different ammonia decomposition temperatures residual ammonia content in the tail gas during with different ammonia charging air speed.
Table 2:
| Decomposition temperature/℃ | ??520 | ????550 | ??580 | ??630 | ??650 |
| Ammonia air speed/h -1 | ??2000?300 ???????0 | ??300??350??430 ??0????0????0 | ??3800?600 ???????0 | ??1700 ??0 | ??2000 ??0 |
| Residual ammonia/the ppm of tail gas | ??1650?180 ???????0 | ??800??105??285 ???????0????0 | ??650??230 ???????0 | ??1350 | ??490 |
Annotate: reaction pressure: normal pressure
Example 9
Table 3 has provided the ammonia decomposed tail gas residual ammonia content of catalyzer " F " in 720 hours reaction times.
Table 3:
| Residual of tail gas during reaction when ammonia (little)/ppm | Residual of tail gas during reaction when ammonia (little)/ppm | Residual of tail gas during reaction when ammonia (little)/ppm | Residual of tail gas during reaction when ammonia (little)/ppm |
| ??24????660 ??48????620 ??72????715 ??96????775 ??120???700 ??144???615 ??168???705 ??192???850 | 216?????735 240?????755 264?????945 288?????810 312?????750 336?????810 360?????730 384?????715 | 432?????795 456?????765 480?????725 504?????835 528?????950 552?????705 600?????855 624?????935 | 648 920 672 780 696 670 720 830 average 800 |
Annotate: temperature of reaction: 550 ℃; Reaction pressure: normal pressure; Ammonia air speed: 3000h
-
By above-mentioned description and example explanation to catalyzer and preparation process thereof, catalyzer provided by the invention has characteristics such as ammonia decomposition temperature ammonia charging air speed height, the residual ammonia content of tail gas low, that allow are low.If use by catalyzer provided by the present invention, compare with the nickel-base catalyst that present industry is used, the ammonia decomposition temperature can reduce 150-250 ℃, catalyzer loading amount and equipment volume will reduce greatly during identical gas production rate, electricity consumption of equipment amount, manufacturing cost and running cost will significantly reduce, and the equipment corrosion cocoa obtains alleviation to a certain degree.By Ru/Ba/ activated-carbon catalyst provided by the present invention, be 550 ℃ in temperature of reaction for example, ammonia charging air speed is 3000h
-Reaction conditions under, residual ammonia content can be controlled at about 800ppm in the tail gas; In temperature of reaction is 650 ℃, and ammonia charging air speed is 20000h
-Reaction conditions under, residual ammonia content can be controlled at 500ppm in the tail gas.
Claims (18)
1, a kind of ruthenium base preparing hydrogen by ammonia decomposition nitrogen mixed gas catalyzer is made up of main active constituent ruthenium, one or more auxiliary agents and carrier; Main active constituent ruthenium weight percentage is 0.1-10% in the described catalyzer; Used carrier is CaO, MgO, TiO
2, SiO
2, Al
2O
3Or gac; Adjuvant used is one or more of IA, IIA, IIIA, IVA, IIIB and rare earth element, and the weight percentage of adjuvant component is 0.1-30%.
2, catalyzer as claimed in claim 1 is characterized in that, described main active constituent ruthenium weight percentage is 1-5%.
3, catalyzer as claimed in claim 1 is characterized in that, described support of the catalyst is SiO
2, Al
2O
3Or gac.
As claim 1 or 3 described catalyzer, it is characterized in that 4, described carrier is a gac.
5, catalyzer as claimed in claim 1 is characterized in that, described auxiliary agent is one or more in Li, Na, K, Mg, Ca, Ba, B, Ga, In, Sn, Y, La, Ce, Pr, Nd and the compound thereof.
As claim 1 or 5 described catalyzer, it is characterized in that 6, described auxiliary agent is one or more in Mg, Ba, K, Y, La or Ce and the compound thereof.
As claim 1,5 or 6 described catalyzer, it is characterized in that 7, described auxiliary agent is Mg or Ba.
As claim 1,5,6 or 7 described catalyzer, it is characterized in that 8, described auxiliary agent weight percentage is 1-8%.
9, a kind of method for preparing the described catalyzer of claim 1, its key step is:
A) supported ruthenium: with the solution impregnating carrier that contains ruthenium;
B) support auxiliary agent: the carrier that soaks step a preparation in Zhen with the aqueous solution that contains auxiliary agent;
C) ruthenium on the carrier that step b is obtained reduces with gas phase or liquid-phase reduction method;
D) carrier that step c is made is in 20-200 ℃ of dry 1-24 hour, 200-900 ℃ roasting 1-24 hour;
Described vapour phase reduction is with hydrogen or to contain hydrogen mixed gas be reductive agent;
Described liquid-phase reduction is a reductive agent with the formaldehyde or the hydrazine aqueous solution.
10, method as claimed in claim 9 is characterized in that, described step a is for supporting auxiliary agent, step b supported ruthenium.
As claim 9 or 10 described methods, it is characterized in that 11, the solution of described step a is the aqueous solution that contains ruthenium and auxiliary agent.
12, method as claimed in claim 9 is characterized in that, the carrier that described step b obtains is put into alkaline solution and soaked after 0.5-10 hour, continues step c and steps d.
13, method as claimed in claim 9 is characterized in that, described steps d reduction nail is to carry out behind step a.
14, method as claimed in claim 9 is characterized in that, the carrier that steps d is obtained is put into deionized water and soaked.
As claim 9,10 or 12 described methods, it is characterized in that 15, described ruthenium is any compound and solution thereof that contains ruthenium.
As right 9,10,12 or 15 described methods, it is characterized in that 16, described ruthenium is RuCl
3The aqueous solution.
As claim 9,10 or 11 described methods, it is characterized in that 17, described compounding agent solution is the aqueous solution of carbonate.
18, as each the described catalyzer application in the preparing hydrogen by ammonia decomposition nitrogen mixed gas of above-mentioned claim.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA021559449A CN1506300A (en) | 2002-12-12 | 2002-12-12 | Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA021559449A CN1506300A (en) | 2002-12-12 | 2002-12-12 | Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1506300A true CN1506300A (en) | 2004-06-23 |
Family
ID=34236085
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA021559449A Pending CN1506300A (en) | 2002-12-12 | 2002-12-12 | Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1506300A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100493700C (en) * | 2005-10-28 | 2009-06-03 | 厦门大学 | Preparation method of ruthenium-base ammonia synthetic catalyst |
| CN103301837A (en) * | 2013-06-07 | 2013-09-18 | 苏州市泰力达科技有限公司 | Method for preparing aluminum oxide loaded ruthenium catalyst |
| WO2019188219A1 (en) * | 2018-03-26 | 2019-10-03 | 昭和電工株式会社 | Ammonia decomposition catalyst and method for producing same, and method for producing hydrogen gas |
| CN110694623A (en) * | 2019-10-28 | 2020-01-17 | 福州大学 | Preparation method of ruthenium-based ammonia synthesis catalyst with cerium oxide-silicon dioxide composite material as carrier |
| US20200062590A1 (en) * | 2018-08-21 | 2020-02-27 | University Of South Carolina | Ammonia Decomposition Catalyst Systems |
| CN111051238A (en) * | 2017-11-29 | 2020-04-21 | 住友化学株式会社 | Process for oxidation of ammonia |
| JP2020082079A (en) * | 2018-11-22 | 2020-06-04 | ナショナル エンジニアリング リサーチ センター オブ ケミカル ファーティライザー キャタリスト、フージョウ ユニバーシティ | Ruthenium-based catalyst for hydrogen production from ammonia decomposition, preparation method therefor and application thereof |
| CN113058595A (en) * | 2021-03-31 | 2021-07-02 | 福州大学 | Ru-based ammonia decomposition hydrogen production catalyst and preparation method thereof |
| CN114471549A (en) * | 2020-11-12 | 2022-05-13 | 中国科学院大连化学物理研究所 | Catalyst and preparation method and application thereof |
| CN115193430A (en) * | 2021-04-06 | 2022-10-18 | 三星工程株式会社 | Ammonia decomposition catalyst and ammonia decomposition method using same |
| CN115364884A (en) * | 2021-11-12 | 2022-11-22 | 福州大学 | Preparation method of ruthenium-based catalyst and application of ruthenium-based catalyst in mild ammonia synthesis |
-
2002
- 2002-12-12 CN CNA021559449A patent/CN1506300A/en active Pending
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100493700C (en) * | 2005-10-28 | 2009-06-03 | 厦门大学 | Preparation method of ruthenium-base ammonia synthetic catalyst |
| CN103301837A (en) * | 2013-06-07 | 2013-09-18 | 苏州市泰力达科技有限公司 | Method for preparing aluminum oxide loaded ruthenium catalyst |
| CN111051238B (en) * | 2017-11-29 | 2023-06-16 | 住友化学株式会社 | Method for oxidizing ammonia |
| CN111051238A (en) * | 2017-11-29 | 2020-04-21 | 住友化学株式会社 | Process for oxidation of ammonia |
| JP7264154B2 (en) | 2018-03-26 | 2023-04-25 | 株式会社レゾナック | Ammonia decomposition catalyst, method for producing the same, and method for producing hydrogen gas |
| WO2019188219A1 (en) * | 2018-03-26 | 2019-10-03 | 昭和電工株式会社 | Ammonia decomposition catalyst and method for producing same, and method for producing hydrogen gas |
| JPWO2019188219A1 (en) * | 2018-03-26 | 2021-03-11 | 昭和電工株式会社 | Ammonia decomposition catalyst and its production method, and hydrogen gas production method |
| US20200062590A1 (en) * | 2018-08-21 | 2020-02-27 | University Of South Carolina | Ammonia Decomposition Catalyst Systems |
| US11891301B2 (en) * | 2018-08-21 | 2024-02-06 | University Of South Carolina | Ammonia decomposition catalyst systems |
| US11110434B2 (en) | 2018-11-22 | 2021-09-07 | National Engineering Research Center Of Chemical Fertilizer Catalyst, Fuzhou University | Ruthenium-based catalyst for hydrogen production from ammonia decomposition, preparation method therefor and application thereof |
| JP2020082079A (en) * | 2018-11-22 | 2020-06-04 | ナショナル エンジニアリング リサーチ センター オブ ケミカル ファーティライザー キャタリスト、フージョウ ユニバーシティ | Ruthenium-based catalyst for hydrogen production from ammonia decomposition, preparation method therefor and application thereof |
| CN110694623A (en) * | 2019-10-28 | 2020-01-17 | 福州大学 | Preparation method of ruthenium-based ammonia synthesis catalyst with cerium oxide-silicon dioxide composite material as carrier |
| CN114471549A (en) * | 2020-11-12 | 2022-05-13 | 中国科学院大连化学物理研究所 | Catalyst and preparation method and application thereof |
| CN113058595A (en) * | 2021-03-31 | 2021-07-02 | 福州大学 | Ru-based ammonia decomposition hydrogen production catalyst and preparation method thereof |
| CN115193430A (en) * | 2021-04-06 | 2022-10-18 | 三星工程株式会社 | Ammonia decomposition catalyst and ammonia decomposition method using same |
| CN115364884A (en) * | 2021-11-12 | 2022-11-22 | 福州大学 | Preparation method of ruthenium-based catalyst and application of ruthenium-based catalyst in mild ammonia synthesis |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1506300A (en) | Ruthenium-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas and its prepn | |
| CN1080585C (en) | Photocatalyst, method for preparing the same, and production of hydrogen using the same | |
| CN1108866C (en) | ZnS photocatalyst, preparation thereof and use thereof the producing hydrogen | |
| CN1044416A (en) | Produce oxyethane catalyzer and method for making thereof | |
| CN100336735C (en) | Method and apparatus for treating high concentrated organic wastewater by hydrothermal electrical catalytic oxidation | |
| CN1017597B (en) | Process for production desulfurization agent | |
| CN1511632A (en) | Carrier for producing silver catalyst for epoxy ethane production, its preparing method and use | |
| CN111203281A (en) | Regeneration method of acetylene hydrochlorination non-mercury catalyst | |
| US20230191371A1 (en) | Photocatalyst and application thereof in environmentally friendly photocatalytic treatment of power battery | |
| CN1506299A (en) | Prepn and application of nickel-based catalyst for decomposing ammonia to prepare mixed H2-N2 gas | |
| CN1850329A (en) | Load-type nickel-metal catalyst and its use | |
| CN1141213A (en) | Catalyst for purifying exhaust gases process for producing same | |
| CN113117684A (en) | Preparation method of ternary oxide ozone catalyst for advanced wastewater treatment | |
| CN1274409C (en) | Preparation method of highly active titanium dioxide membrane photocatalyst | |
| CN1401426A (en) | Ammonia synthesis ruthenium based catalyst and preparing process thereof | |
| CN1915476A (en) | Catalyst in use for treating industrial waste gas containing chloro methanem and preparation method | |
| CN1310703C (en) | Ethylene oxide catalyst carrier preparation | |
| CN1206158C (en) | Fractional oil desulfurizing and adsorption agent and its preparation method | |
| CN1144861C (en) | Saturated loaded noble metal catalyst for distilling oil arenes and its prep. | |
| CN1270081A (en) | Efficient catalyst for synthesizing ammonia and its preparing process | |
| CZ307989B6 (en) | A process for preparing a catalyst to remove nitrous oxide from industrial waste gases and a catalyst prepared by this process | |
| CN1015875B (en) | Catalytic agent for preparing isoprene by isobutylene-methanal gas phase condensation | |
| CN101691254B (en) | Method for preparing modified bauxite catalyst in ozone heterogeneous catalysis water treatment technology | |
| CN1162416C (en) | Silver catalyst for epoxyethane production, its preparation method and application | |
| CN110302778B (en) | Carbon-loaded ruthenium-based ammonia synthesis catalyst and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |