CN1506300A - A kind of ruthenium-based ammonia decomposition hydrogen-nitrogen mixed gas catalyst and preparation method thereof - Google Patents
A kind of ruthenium-based ammonia decomposition hydrogen-nitrogen mixed gas catalyst and preparation method thereof Download PDFInfo
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 56
- 239000007789 gas Substances 0.000 title claims abstract description 43
- 239000003054 catalyst Substances 0.000 title claims abstract description 37
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 26
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 15
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 title claims description 30
- 229910052707 ruthenium Inorganic materials 0.000 title claims description 30
- 238000002360 preparation method Methods 0.000 title description 16
- 238000000034 method Methods 0.000 claims abstract description 21
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910004298 SiO 2 Inorganic materials 0.000 claims abstract description 8
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 229910052788 barium Inorganic materials 0.000 claims abstract description 5
- 229910010413 TiO 2 Inorganic materials 0.000 claims abstract description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000011068 loading method Methods 0.000 claims abstract description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 3
- 229910052761 rare earth metal Inorganic materials 0.000 claims abstract description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims abstract 4
- 239000007864 aqueous solution Substances 0.000 claims description 20
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 13
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 11
- 150000001875 compounds Chemical class 0.000 claims description 7
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 6
- 229910052684 Cerium Inorganic materials 0.000 claims description 4
- 239000008367 deionised water Substances 0.000 claims description 4
- 229910021641 deionized water Inorganic materials 0.000 claims description 4
- 229910052746 lanthanum Inorganic materials 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 229910052700 potassium Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 229910052727 yttrium Inorganic materials 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 2
- 229910052779 Neodymium Inorganic materials 0.000 claims description 2
- 229910052777 Praseodymium Inorganic materials 0.000 claims description 2
- 239000012670 alkaline solution Substances 0.000 claims description 2
- 229910052791 calcium Inorganic materials 0.000 claims description 2
- 229910052733 gallium Inorganic materials 0.000 claims description 2
- 229910052738 indium Inorganic materials 0.000 claims description 2
- 229910052744 lithium Inorganic materials 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- 229910052718 tin Inorganic materials 0.000 claims description 2
- 239000000654 additive Substances 0.000 claims 2
- 239000003638 chemical reducing agent Substances 0.000 claims 2
- 229910019891 RuCl3 Inorganic materials 0.000 claims 1
- 238000001354 calcination Methods 0.000 claims 1
- 238000002386 leaching Methods 0.000 claims 1
- YBCAZPLXEGKKFM-UHFFFAOYSA-K ruthenium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Ru+3] YBCAZPLXEGKKFM-UHFFFAOYSA-K 0.000 claims 1
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 abstract description 5
- 230000002829 reductive effect Effects 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 2
- 230000007797 corrosion Effects 0.000 abstract description 2
- 229910052759 nickel Inorganic materials 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 19
- 206010013786 Dry skin Diseases 0.000 description 6
- 239000002585 base Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000007598 dipping method Methods 0.000 description 3
- 238000005470 impregnation Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000002671 adjuvant Substances 0.000 description 2
- AYJRCSIUFZENHW-UHFFFAOYSA-L barium carbonate Chemical compound [Ba+2].[O-]C([O-])=O AYJRCSIUFZENHW-UHFFFAOYSA-L 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000003421 catalytic decomposition reaction Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 239000001095 magnesium carbonate Substances 0.000 description 2
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 2
- 235000014380 magnesium carbonate Nutrition 0.000 description 2
- 229960001708 magnesium carbonate Drugs 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 235000015320 potassium carbonate Nutrition 0.000 description 2
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 description 1
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- HGSHBQLEBLRBJS-UHFFFAOYSA-N N.[Mo].[Ni] Chemical compound N.[Mo].[Ni] HGSHBQLEBLRBJS-UHFFFAOYSA-N 0.000 description 1
- 235000009470 Theobroma cacao Nutrition 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 244000240602 cacao Species 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000005329 float glass Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000004663 powder metallurgy Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- KUBYTSCYMRPPAG-UHFFFAOYSA-N ytterbium(3+);trinitrate Chemical compound [Yb+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O KUBYTSCYMRPPAG-UHFFFAOYSA-N 0.000 description 1
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
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- Catalysts (AREA)
Abstract
一种氨分解制氢氮混合气催化剂，其特征在于催化剂由Ru、载体和活性炭组成。催化剂的主活性组份为Ru。载体为CaO、MgO、TiO2、SiO2、Al2O3或活性炭中的一种，较佳的催化剂载体为SiO2、Al2O3或活性炭，最佳的载体为活性炭。助剂为IA、IIA、IIIA、IVA、IIIB或稀土元素中的一种或几种，其中以Mg和Ba为最佳。按本发明所提供的方法制备的催化剂，与目前工业使用的镍基催化剂相比，氨分解温度可降低150℃～250℃，相同产气量时催化剂装量及设备体积大大减小，氨分解耗电量显著降低，设备腐蚀可得到一定缓解。A catalyst for producing hydrogen-nitrogen mixed gas by decomposing ammonia is characterized in that the catalyst is composed of Ru, a carrier and activated carbon. The main active component of the catalyst is Ru. The carrier is one of CaO, MgO, TiO 2 , SiO 2 , Al 2 O 3 or activated carbon, the preferred catalyst carrier is SiO 2 , Al 2 O 3 or activated carbon, and the best carrier is activated carbon. The auxiliary agent is one or more of IA, IIA, IIIA, IVA, IIIB or rare earth elements, among which Mg and Ba are the best. Compared with the nickel-based catalysts currently used in industry, the catalyst prepared by the method provided by the present invention can reduce the ammonia decomposition temperature by 150°C to 250°C, and the catalyst loading and equipment volume are greatly reduced when the gas production is the same. The power is significantly reduced, and the corrosion of equipment can be alleviated to a certain extent.
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)
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|---|---|---|---|
| CNA021559449A CN1506300A (en) | 2002-12-12 | 2002-12-12 | A kind of ruthenium-based ammonia decomposition hydrogen-nitrogen mixed gas catalyst and preparation method thereof |
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|---|---|---|---|
| CNA021559449A CN1506300A (en) | 2002-12-12 | 2002-12-12 | A kind of ruthenium-based ammonia decomposition hydrogen-nitrogen mixed gas catalyst and preparation method thereof |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100493700C (en) * | 2005-10-28 | 2009-06-03 | 厦门大学 | A kind of preparation method of ruthenium-based ammonia synthesis 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 | Ammonia oxidation method |
| 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 | A kind of Ru-based ammonia decomposition hydrogen production catalyst and preparation method thereof |
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