Source: http://www.google.com/patents/US6808652?dq=inventor:%22Arthur+R.+Hair%22&ei=VAy0Tsa4NYTl0QGQiqWiBA
Timestamp: 2015-05-06 17:59:28
Document Index: 76009427

Matched Legal Cases: ['Application No. 99', 'Application No. 2000', 'Application No. 2000', 'Application No. 99', 'Application No. 2000', 'Application No. 2000', 'Application No. 99']

Patent US6808652 - Modified ⊖-alumina-supported nickel reforming catalyst and its use for ... - Google PatentsSearch Images Maps Play YouTube News Gmail Drive More »Sign inAdvanced Patent SearchPatentsA modified ⊖-Al2O3-supported nickel reforming catalyst and its use for producing synthesis gas from natural gas, more specifically to a nickel reforming catalyst expressed by the following formula 1, having improved coke resistance, high-temperature catalysis stability and catalytic activity, which...http://www.google.com/patents/US6808652?utm_source=gb-gplus-sharePatent US6808652 - Modified ⊖-alumina-supported nickel reforming catalyst and its use for producing synthesis gas from natural gasAdvanced Patent SearchPublication numberUS6808652 B2Publication typeGrantApplication numberUS 10/750,756Publication dateOct 26, 2004Filing dateJan 5, 2004Priority dateMay 18, 2001Fee statusPaidAlso published asUS6693060, US20030032554, US20040142817Publication number10750756, 750756, US 6808652 B2, US 6808652B2, US-B2-6808652, US6808652 B2, US6808652B2InventorsSang-Eon Park, Ki-Won Jun, Hyun-Seog Roh, Seung-Chan Baek, Young-Sam Oh, Young-Soon Baek, Ri-Sang Choi, Taek-Yong SongOriginal AssigneeKorea Research Institute Of Chemical Technology, Korea Gas Corporation, Kyoungdong Citygas Co., Ltd.Export CitationBiBTeX, EndNote, RefManPatent Citations (32), Referenced by (2), Classifications (26), Legal Events (7) External Links: USPTO, USPTO Assignment, EspacenetModified ⊖-alumina-supported nickel reforming catalyst and its use for producing synthesis gas from natural gas
US 6808652 B2Abstract
A modified ⊖-Al2O3-supported nickel reforming catalyst and its use for producing synthesis gas from natural gas, more specifically to a nickel reforming catalyst expressed by the following formula 1, having improved coke resistance, high-temperature catalysis stability and catalytic activity, which is prepared by coating nickel or mixture of nickel and cocatalyst (M1-M2-Ni) on a Al2O3 support modified with metal (M3-M4-ZrO2/⊖-Al2O3), and its use for producing synthesis gas from natural gas through steam reforming, oxygen reforming or steam-oxygen reforming,
M1-M2-Ni/M3-M4-ZrO2/⊖-Al2O3 (1) wherein M1 is an alkali metal; each of M2 and M3 is an alkaline earth metal; and M4 is a IIIB element or a lanthanide.
What is claimed is: 1. A method of producing a mixture of carbon monoxide and hydrogen from methane natural gas by steam reforming, oxygen reforming, or steam-oxygen reforming, comprising the steps of:
contacting said methane natural gas with a catalyst, wherein said catalyst consists essentially of a ⊖-Al2O3-supported nickel catalyst of the formula: M1-M2-Ni/M3-M4-ZrO2/⊖-Al2O3 (1) wherein M1 is an alkali metal; each of M2 and M3 is an alkaline earth metal; and M4 is a IIIB element or a lanthanide; wherein the nickel reforming catalyst is composed of: 3-20 wt. % of nickel (Ni) against ⊖-Al2O3; 0-0.2 molar equivalent of M1 and 0-4 molar equivalent of M2 cocatalysts against nickel; 0-1.0 molar equivalent of M3 and 0.01-1.0 molar equivalent of M4 against zirconium; and 0.01-1.0 molar equivalent of ZrO2 against ⊖-Al2O3; maintaining the methane natural gas-to-steam molar ratio in the range of from 0 to 6; maintaining the methane natural gas-to-oxygen molar ratio in the range of 0 to 1; maintaining the reaction temperature in the range of 600 to 1000� C.; maintaining the reaction pressure in the range of 0.5 to 20 atm; and maintaining the space velocity in the range of 1,000 to 1,000,000 cc/hr�g-cat. 2. The method of claim 1, wherein said method comprises steam reforming and the methane natural gas-to-steam molar ratio is in the range of from 1 to 6.
3. The method of claim 1, wherein said method comprises oxygen reforming and the methane natural gas-to-oxygen molar ratio is in the range of from 0.1 to 1.
4. The method of claim 1, wherein said method comprises steam-oxygen reforming and the methane natural gas-to-steam molar ratio is in the range of from 1 to 5, and the methane natural gas-to-oxygen molar ratio is in the range of from 0.1 to 1.
This is a division of application Ser. No. 10/143,669, filed May 13, 2002 now U.S. Pat. No. 6,693,060, which is incorporated herein by reference.
The present invention relates to a modified ⊖-Al2O3-supported nickel reforming catalyst and its use for producing synthesis gas from natural gas. More particularly, the present invention is to provide a nickel reforming catalyst expressed by the following formula 1, having improved coke resistance, high-temperature catalysis stability and catalytic activity, which is prepared by coating nickel or mixture of nickel and cocatalyst (M1-M2-Ni) on a ⊖-Al2O3 support modified with metal (M3-M4-ZrO2/⊖-Al2O3), and its use for producing synthesis gas from natural gas through steam reforming, oxygen reforming or steam-oxygen reforming,
Steam reforming, which produces a mixture (synthesis gas) of hydrogen and carbon monoxide from methane (natural gas), has become an important and fundamental chemical industrial process from long time ago. Synthesis gas produced by steam reforming of methane is widely used for producing methanol, hydrogen, ammonia, etc. Recently, it has been used for producing liquid fuel or oxygen-including compounds.
The biggest problem in the steam reforming is deactivation of reforming catalyst due to deposition of carbon. The carbon deposition can be calculated thermodynamically from molar ratios of hydrogen to carbon and oxygen to carbon in the product. Therefore, in steam reforming of methane, excess amount of steam is required to increase molar ratios of hydrogen to carbon and oxygen to carbon, in order to prevent deactivation of reforming catalyst. This promotes an aqueous gasification enough to obtain a synthesis gas with molar ratio of hydrogen to carbon monoxide larger than 3:1. Therefore, this process may be suitable for producing ammonia or high-concentration hydrogen. The current industrial steam reforming process of methane is being carried out under the condition of 730-860� C. of a temperature, 20-40 atm of a pressure and 1:4-6 of methane-to-steam molar ratio.
And, for the industrial catalyst for the steam reforming, nickel catalyst is used dominantly. A superior industrial reforming catalyst should have coke resistance and thermal and mechanical stability. For this purpose, selection of suitable support such as α-alumina is very important.
The inventors suggested reforming, reactions using modified zirconia-supported nickel catalyst. [Korea Patent Application No. 99-50013; Korea Patent Application No. 2000-0054443; & Korea Patent Application No. 2000-0057688]. Korea Patent Application No. 99-50013 discloses a modified zirconia-supported nickel catalyst and carbon dioxide reforming using it. Korea Patent Application No. 2000-0054443 discloses a cerium-modified zirconia-supported nickel catalyst and steam reforming using it. Further, Korea Patent Application No. 2000-0057688 discloses a modified zirconia-supported nickel catalyst and steam-oxygen reforming using it. The modified zirconia-supported nickel catalyst showed better activity and stability than those of conventional reforming catalysts when used in carbon dioxide reforming, steam reforming, and steam-oxygen reforming even under severe condition (high space velocity and low steam-to-methane ratio) and at high temperature. Despite of good activity and stability, zirconia is not suitable to be used in reforming catalyst, because it is more expensive than alumina. Accordingly, it is required to use the more cost-effective ⊖-Al2O3 support and modify it with zirconia. Then, if it is coated with nickel catalyst, an inexpensive catalyst with good activity and stability can be obtained.
Inventors have developed a nickel reforming catalyst by coating ⊖-Al2O3 base support with zirconia modified with alkaline earth metal (M3) and IIIB element or lanthanide metal (M4), and coating nickel and alkali metal (M1) or alkaline earth metal (M2) cocatalyst. When this reforming, catalyst was used in various reforming reactions of natural gas, i.e., steam reforming, oxygen reforming or steam-oxygen reforming, it has showed equal or superior activity and stability compared with the modified zirconia-supported nickel catalyst we had suggested in Korea Patent Application No. 99-50013.
Accordingly, an object of the present invention is to provide a nickel reforming catalyst using ⊖-Al2O3 as base support, and its use for producing synthesis gas through reforming reaction.
The present invention is to provide a nickel reforming catalyst expressed by the following formula 1, which is used for producing synthesis gas mixture of carbon monoxide and hydrogen from natural gas,
M1-M2Ni/M3-M4-ZrO2/⊖-Al2O3 (1) wherein M1 is an alkali metal; each of M2 and M3 is an alkaline earth metal; and M4 is a IIIB element or a lanthanide.
Synthesis gas mixture of carbon monoxide and hydrogen may be produced from methane in the presence of the nickel reforming catalyst by steam reforming, oxygen reforming or steam-oxygen reforming, under the condition of 0-6 of methane-to-steam molar ratio, 0-1 of methane-to-oxygen molar ratio, 600-1000� C. of a reaction temperature, 0.5-20 atm of a reaction pressure and 1,000-1,000,000 cc/hr�g-cat of a space velocity.
Hereunder is given a more detailed description of the present invention. This invention relates to a reforming catalyst expressed by formula 1 and its use for producing synthesis gas by steam reforming, oxygen reforming or steam-oxygen reforming of natural gas.
The modified ⊖-Al2O3-supported nickel reforming catalyst according to the present invention is prepared by coating a modified zirconia (M3-M4-ZrO2) on ⊖-Al2O3 base support and coating nickel and cocatalyst (M1-M2-Ni) on it. Here, nickel is added preferably in the range of 3 to 20 wt. % based to ⊖-Al2O3. Each of M1 and M2 cocatalysts is added preferably in the range of 0 to 0.2 and 0 to 4 molar ratios based to nickel, respectively. Each of M3 and M4 is added preferably in the range of 0 to 1.0 and 0.01 To 1.0 molar ratios based to zirconium (Zr), respectively. Zirconia (ZrO2) is added preferably in the range of 0.01 to 1.0 molar ratio based to ⊖Al2O3.
M1 is an alkali metal chosen from sodium, potassium and cesium; each of M2 and M3 is an alkaline earth metal chosen from calcium, magnesium and strontium; and M4 is a IIIB element chosen from yttrium, lanthanum and cerium, or lanthanide, wherein M3 and M4 are cocatalysts for enhancing coke resistance and catalytic activity.
The reforming catalyst according to the present invention may be prepared by coprecipitation, precipitation, sol-gel method, molten-salt or impregnation method. When ⊖-Al2O3 is modified with zirconia to obtain support, coprecipitation or sol-gel method is preferable. When nickel and cocatalyst are coated on the support, molten-salt and impregnation methods are preferable.
Preparation of modified ⊖-Al2O3 support through coprecipitation is as follows. 1M zirconyl chloride aqueous solution is purified by recrystallization from hydrochloric acid. 1M nitrate solution of the metal to be modified on the ⊖-Al2O3 base support is added to this solution. After strongly stirring the mixture at 50-70� C. for 4-8 hr, 29.8% ammonia water is added until pH reaches 10. The precipitate is filtered and washed with 5% ammonia water until no chloride ion is observed. It is further washed with distilled water. The filtered precipitate is placed in a drying oven and dried at 90-100� C. for 10-12 hr. Then, it is put in a furnace and calcined in 700-900� C. of air for 7-9 hr to obtain the modified ⊖-Al201 support.
Preparation of nickel- and cocatalyst-supported modified ⊖-Al2O3 support through impregnation is as follows. Modified ⊖-Al2O3 support powder is added in distilled water and stirred to obtain a slurry. 1M nitrate solution of nickel and the metal used as cocatalyst is added to this slurry. The mixture is stirred at 25� C. for 5-7 hr. Then, the flask containing this mixture solution is connected to a rotary vacuum evaporator in order to evaporate water under pressure of 90-120 Torr and temperature of 70-90� C. The obtained catalyst precursor powder is dried in a drying oven at 100� C. for 12 hr. and calcined at 400-500� C. in air for about 4 hr to obtain the nickel reforming catalyst.
Preparation of nickel- and cocatalyst-supported modified ⊖-Al2O3 support through molten-salt method is as follows. The fact that nickel and cocatalyst metal precursor have low melting temperature is used. In order to obtain uniform and thin coating of metal component on the modified ⊖-Al2O3 support the support powder and the metal precursor powder is finely around and mixed well at room temperature. Then, the metal precursor component is decomposed through a well-defined heat treatment process to obtain the catalyst. The heat treatment process is as follows. All nitrates in the catalyst precursor powder are melt by heating it at 2� C./min from room temperature to 400� C. under argon flow of 100 mL/min in a furnace. The nitrates are decomposed at 400� C. for 4 hr. Then, after changing argon flow to dry air flow, the temperature is increased to 650� C. at 5� C./min. The product is treated for 4 hr at 650� C. The typical catalyst obtained from this method is Ni�Ca/Ce�ZrO2/⊖-Al2O3 catalyst, which is prepared by using nitrates of nickel (melting point: 56.7� C.) and calcium (melting point: 39.7� C.) as metal precursor.
The above methods are only examples of preparing modified ⊖-Al2O3-supported nickel reforming catalysts according to the present invention. Other known preparing methods may be used if necessary.
Reaction condition of producing synthesis gas from natural gas using the nickel reforming catalyst according to the present invention is as follows.
The nickel reforming catalyst expressed by formula 1 can be used in steam reforming, oxygen reforming or steam-oxygen reforming to prepare synthesis gas mixture of carbon monoxide and hydrogen from methane. In the reforming reactions, methane-to-steam molar ratio is preferred to be 0-6, and methane-to oxygen molar ratio is preferred to be 0-1. To be more specific, in the steam reforming, the methane-to-steam molar ratio is preferred to be 1-6; in the oxygen reforming, the methane-to-oxygen molar ratio is preferred to be 0.1-1; and in the steam-oxygen reforming, the methane-to-steam molar ratio is preferred to be 1-5 and the methane-to-oxygen molar ratio is preferred to be 0.1-1. The reaction temperature is 600-1000� C. and the reaction pressure is 0.5-20 atm. The reaction gas is injected at 1,000-1,000,000 cc/hr�g-cat of space velocity.
As described above, the present invention provides a new industrial catalyst, which has equal or superior activity and stability compared to the expensive conventional modified zirconia-supported nickel reforming catalyst, by coating modified zirconia on ⊖-Al2O3 support and supporting nickel or mixture of nickel and cocatalyst on the support.
The following examples are intended to be illustrative of the present invention. However, they should not be construed as limiting the scope of this invention.
Preparation of ⊖-Al2O3 Support Modified With Alkaline Earth Metal and Zirconia
Modified ⊖-Al2O3 support was prepared by coprecipitation using alkaline earth metal, such as calcium and magnesium, and zirconia.
Firstly, zirconyl chloride (Aldrich, 98%) was diluted to 1M aqueous solution and purified by recrystallization from hydrochloric acid: After mixing the result with 1M alkaline earth metal nitrate solution, the mixture was strongly stirred at 60� C. for 6 hr. After adding ⊖-Al2O3 support and 29.8% ammonia water (Fisher Scientific) until pH reaches 10, the precipitate was filtered and washed with 5% ammonia water until no chloride ion was detected. Then, it was washed with distilled water. The filtered precipitate was dried at 100� C. for 12 hr in a drying oven. The obtained powder was finely ground in mortar, and calcined in 900� C. of air for in a furnace to obtain modified ⊖-Al2O3 supports. The obtained modified ⊖-Al2O3 supports were Ca�ZrO2/⊖-Al2O3 (Ca/Zr=�) and Mg�ZrO2/⊖-Al2O3 (Mg/Zr=�). The content of Ca�ZrO2 and Mg�ZrO2 was 5 wt. % relative to ⊖-Al2O3.
Preparation of ⊖-Al2O3 Support Modified With IIIB Element or Lanthanide and Zirconia
Modified ⊖-Al2O3 support was prepared by sol-gel method using IIIB element or lanthanide, such as yttrium, lanthanum and cerium, and zirconia.
Nitrate of the metal component to be modified was added to 1 L of distilled water at 20� C., so that its molar ratio against zirconia is 1:4. After dissolving uniformly for 5 hr, ⊖-Al2O3 support was added and molar equivalent of citric acid (against the metal nitrate) was added at the same temperature. After completely dissolving for 6 hr, molar equivalent of ethylene glycol was added and the mixture was stirred for 6 hr. Then, the mixture solution was condensed to highly viscous phase by suction-filtering at 80-100� C., and was dried in a microwave oven. The dry support powder was finely round in mortar, and was calcined in 300� C. of air for 5 hr, and then in 900� C. of air for 5 hr in a furnace. The obtained modified ⊖-Al2O3 supports were Ce�ZrO2 (1:4)/⊖-Al2O3, La�ZrO2 (1:4)/⊖-Al2O3 and Y�ZrO2 (1:4)/⊖-Al2O3. The content of ⊖-Al2O3 modifying, component was set to be 5 wt. %.
Preparation of ⊖-Al2O3 Support Modified With Alkaline Earth Metal, IIIB Element or Lanthanide and Zirconia
⊖-Al2O3 support modified with an alkaline earth metal, IIIB element or lanthanide and zirconia was prepared by coprecipitation as in Preparing Example 2. The obtained modified ⊖-Al2O3 support was Ce−Mg�ZrO2/⊖-Al2O3, and metal content was 20 mol % against zirconia. The content of Ce�Mg�ZrO2 was set to be 5 wt. % against ⊖-Al2O3.
Preparation of Nickel Reforming Catalyst by Impregnation
Nickel and cocatalyst were impregnated on the modified ⊖-Al2O3 supports prepared in Examples 2 & 3.
Firstly, 20 g of modified ⊖-Al2O3 support powder was put in a 500 mL round-bottom flask containing 200 mL of distilled water. After making zirconia slurry by stirring this mixture, 1M nickel nitrate solution and cocatalyst component was added and stirred for 6 hr at 25� C. Then, the flask containing the solution was connected to a rotary vacuum evaporator. The rotary vacuum evaporator was rotated under 100 Torr and 80� C. to evaporate water. The obtained catalyst precursor powder was dried in 100� C. of drying, oven for 12 hr. Then, it was calcined in 500� C. of air in a furnace for 4 hr to obtain the modified ⊖-Al2O3-supported nickel reforming catalyst.
In Ni/Ce�ZrO2 (1:4)/⊖-Al2O3 obtained from the impregnation, Ce�ZrO2 content was 5 wt. % against ⊖-Al2O3 support, and the nickel content was 3 wt. % (Example 1), 6 wt. % (Example 2), 12 wt. % (Example 3) and 15 wt. % (Example 4) against ⊖-Al2O3. Other than Ni/Ce�ZrO2 (1:4)⊖-Al2O3, Ni/La�ZrO2 (1:4)⊖-Al2O3 (Example 5), Ni�Ca (1:1)/Ce�ZrO2 (1:4)/⊖-Al2O3 (Example 6), Ni�Mg (1:1)/La�ZrO2 (1:4)/⊖-Al2O3 (Example 7), Ni�Ca (1:1)/Y�ZrO2 (1:4)/⊖-Al2O3 (Example 8), Ni�Ca (1:1)/Ce�Mg�ZrO2 (1:1:3)/⊖-Al2O3 (Example 9) and Ni�Ca�Cs (1:1:0.1)/La�ZrO2 (1:4)/⊖-Al2O3 (Example 10) were prepared. In these catalysts, the nickel content was set to be 12 wt. % against ⊖-Al2O3.
Preparation of Ni/Ce�ZrO2 (1:4)/⊖-Al2O3, Ni/⊖-Al2O3, Ni/α-Al2O3 and Ni/MgAl2O4 Catalysts
As catalysts for comparing reforming activity and catalytic stability against those of the catalyst according to the present invention, Ni/Ce�ZrO2 (1:4)/⊖-Al2O3 (Comparative Example 1), Ni/⊖-Al2O3 (Comparative Example 2), Ni/α-Al2O3 (Comparative Example 3) and Ni/MgAl2O4 (Comparative Example 4) were prepared.
Ni/Ce�ZrO2 (1:4)/⊖-Al2O3 of Comparative Example 1 was prepared by the method of Example 2, and the nickel content was 2 wt. % against ⊖-Al2O3. Ni/⊖-Al2O3 of Comparative Example 2 was prepared by precipitation, and, the nickel content was 3 wt. % against ⊖-Al2O3. Ni/α-Al2O3 of Comparative Example 3 and Ni/MgAl2O4 of Comparative Example 4 were prepared by impregnation, and the nickel content was 15 wt. % against ⊖-Al2O3. α-Alumina was purchased from Strem Chemical (US) and magnesium aluminate was purchased from Alpha Chemical. In these catalysts, nickel was supported through impregnation and they were calcined in 500� C. of air for 4 hr.
Determination of Reforming Activity of Nickel Reforming Catalyst in Steam Reforming of Methane
Steam reforming of methane was performed in order to compare nickel reforming catalysts of Examples 1-10 with the catalysts of Comparative Examples 1-4. Catalytic activity was determined by the following method and the result is summerized in Table 1.
Typical fixed bed catalytic reaction equipment manufactured at laboratory was used in catalytic activity determination. Firstly, catalyst was made to pellet having 1-2 mm particle size. After grinding the pellet in mortar, catalyst particles of 20-40 mesh was sieved and filled in a reactor. It was reduced with 5% hydrogen at 700� C. for 2 hr. 1:1 Mixture of methane and steam was injected into the reactor. The temperature of the reactor was regulated by an electric heater and a programmable thermostat (Hanyoung Electronics, HY P-100) to 600-1,000� C. Unless stated otherwise, gas was injected at 72,000 cc/hr�g-cat of space velocity when considering methane and steam only, using a mass flow controller. Composition of gas before and after synthesis was production was analyzed with GC (Chrompack, CP 9001) directly connected to the reactor. A column (Chrompack, CarboPLOT P7) was used for gas separation. Activity of the reforming catalyst was measured with time at 750� C. and atmospheric pressure in order to determine its activity and thermal stability at high temperature. Initial activity and activity after 12 hr were determined from hydrogen yield in the product and methane conversion. The hydrogen yield was obtained from ratio of theoretical hydrogen concentration when 1 mol of methane reacts with 1 mol of steam to produce 3 mol of hydrogen and the actual hydrogen concentration. The result is shown in Table 1.
The catalytic activity ratio was determined by Equation 1. A = Methane   conversion   after   15   hr   at   750 �   C . Initial   methane   conversion   at   750 �   C .   B = Hydrogen   yield   after   15   hr   at   750 �   C . Initial   hydrogen   yield   at   750 �   C . Equation   1 TABLE 1
750� C. Initial
750� C. After
(CH4)*
Ni/Ce�ZrO2/
θ-Al2O3 Ex. 2
θ-Al2O3 Ex. 3
θ-Al2O3 Ex. 4
θ-Al2O3 Ex. 5
Ni/La�ZrO2/
θ-Al2O3 Ex. 6
Ni�Ca/Ce�ZrO2/
θ-Al2O3 Ex. 7
Ni�Mg/La�ZrO2/
θ-Al2O3 Ex. 8
Ni�Ca/Y�ZrO2/
0.96/0.97
θ-Al2O3 Ex. 9
Ni�Ca/Ce�Mg�
ZrO2/θ-Al2O3 Ex. 10
Ni�Ca�Cs/La�
ZrO2/θ-Al2O3 Com. Ex. 1
θAl2O3 Com. Ex. 2
Ni/θ-Al2O3 3
Ni/α-Al2O3 15
Ni/MgAl2O4 15
0.51/0.58
Note: *Nickel Content (wt. %): against θ-Al2O3 **X (CH4): methane conversion As shown in Table 1, Ni/Ce�ZrO2/⊖-Al2O3 showed initial methane conversion as large as 71-82% when the nickel content was in the range of 3 wt. % (Example 1)-15 wt. % (Example 4). And, the methane conversion was maintained almost after 15 hr. The initial hydrogen yield of larger than 71% was also maintained almost after 15 hr. Because these activity and stability is for a severe condition where methane-to-steam ratio is 1, higher methane conversion is expected for actual steam reforming operation, where excess steam is used. Further, much better stability is expected in the presence of excess steam. All of Ni/La�ZrO2/⊖-Al2O3 (Example 5), Ni�Ca/Ce�ZrO2/⊖-Al2O3 (Example 6), Ni�Mg/La�ZrO2/⊖-Al2O3 (Example 7), Ni�Ca/Y�ZrO2/⊖-Al2O3 (Example 8), Ni�Ca/Ce�Mg�ZrO2/⊖-Al2O3 (Example 9) and Ni�Ca�Cs/La�ZrO2/⊖-Al2O3 (Example 10) showed initial methane conversion larger than 69% and initial hydrogen yield larger than 70%. Also, they showed good stability with time. Therefore, they make good steam reforming catalysts.
On the contrary, Ni/Ce�ZrO2/⊖-Al2O3 (Comparative Example 1) with 2 wt. % of nickel showed initial methane conversion and hydrogen yield lower than 3%, and showed no activity after 15 hr. It is shown that high activity is obtained only when the nickel content is larder than 3 wt. % for steam reforming. Also, Ni/⊖-Al2O3 (Comparative Example 2) with 3 wt. % of nickel showed initial methane conversion and hydrogen yield lower than 2%. Therefore only modified ⊖-Al2O3 shows good activity. Ni/α-Al2O3 of Comparative Example 3 and Ni/MgAl2O4 of Comparative Example 4 showed initial methane conversion lower than 62% and the activity decreased below 50% after 15 hr. Considering that Ni/MgAl2O4 is a widely used catalyst, the catalyst according to the present invention, which shows much superior activity and stability, will be able to replace it. The catalyst according to the present invention is also advantageous in terms of cost, because only 5 wt. % of modifying component is applied on ⊖-Al2O3 base support.
Determination of reforming activity of Nickel Catalyst in Oxygen Reforming of Methane
Oxygen reforming, activity of nickel reforming catalysts prepared in Examples 1-10 and catalysts prepared in Comparative Example 1-4 was determined as follows.
The catalytic activity was determined as in Testing Example 1. However, oxygen was used instead of steam. Methane-to-oxygen molar ratio was set to 0.5. Gas was injected at 54,000 cc/hr�g-cat of space velocity using a mass flow controller (MKS Instrument).
Activity and thermal stability of the reforming catalyst at high temperature were determined at 750� C. and atmospheric pressure. Initial activity and activity after 200 min were determined by hydrogen yield in the product and methane conversion. The catalyst activity ratio was determined by Equation 2. The methane conversion and hydrogen yield are summerized in Table 2. The hydrogen yield in Table 2 is expressed in percentage of hydrogen partial pressure against 2 equivalents of methane partial pressure before reaction. A = Methane   conversion   after   2  00   min   at   750 �   C . Initial   methane   conversion   at   750 �   C .   B = Hydrogen   yield   after   2  00   min   at   750 �   C . Initial   hydrogen   yield   at   750 �   C . Equation   2 TABLE 2
(CH4)**
Ni/Ce�ZrO2/θ-
Al2O3 Ex. 2
Al2O3 Ex. 3
Al2O3 Ex. 4
Al2O3 Ex. 5
Ni/La�ZrO2/θ-
Al2O3 Ex. 6
Ni�Ca/Ce�Mg�ZrO2/
θ-Al2O3 Ex. 10
Ni�Ca�Cs/La�ZrO2/
θ-Al2O3 Com. Ex. 1
Al2O3 Com. Ex. 2
1.01/1.01
Ni/u-Al2O3 15
0.82/0.75
*Nickel Content (wt. %): against θ-Al2O3 **X (CH4): methane conversion As shown in Table 2, the reforming catalysts according to the present invention showed better activity and stability than those of Comparative Examples. Also, they have similar trend to that of Table 1.
Ni/Ce�ZrO2/⊖-Al2O3 with 3 wt. % (Example 1) to 15 wt. %(Example 4) of nickel showed initial methane conversion as high as 87-89%. And, the methane conversion was maintained almost after 200 min. The initial hydrogen yield was larger than 82%, and was maintained almost after 200 min. Also, all of Ni/La�ZrO2/⊖-Al2O3 (Example 5), Ni�Ca/Ce�ZrO2/⊖-Al20, (Example 6), Ni�Mg/La�ZrO2/⊖-Al2O3 (Example 7), Ni�Ca/Y�ZrO2/⊖-Al2O3 (Example 8), Ni�Ca/Ce�Mg�ZrO2/⊖-Al2O3 (Example 9) and Ni�Ca�Cs/La�ZrO2/⊖-Al2O3 (Example 10) showed initial methane conversion larger than 80% and initial hydrogen yield larger than 74%. And, they were stable after 200 min. Therefore, they have superior property as oxygen reforming catalysts.
On the contrary, Ni/Ce�ZrO2/⊖-Al2O3 (Comparative Example 1) with 2 wt. % of nickel had initial methane conversion and hydrogen yield as low as 10%. They showed significant oxygen reforming activity only when the nickel content was larger than 3 wt. %. Ni/⊖-Al2O3 with 3 wt. % of nickel (Comparative Example 2) had 75% of initial methane conversion and 68% of hydrogen yield, which are about 15% lower than those of Example 1 with the same nickel content. Therefore, modified ⊖-Al2O3 support showed better oxygen reforming activity. Ni/α-Al2O3 of Comparative Example 3 and Ni/MgAl2O4 of Comparative Example 4 showed poor stability with time. In Comparative Example 3, activity after 200 min dropped to 82% of the initial activity, and in Comparative Example 4 to 95%. Consequently, the catalyst according to the present invention has superior activity and stability in oxygen reforming, as well as in steam reforming.
Determination of Reforming Activity of Nickel Catalyst in Steam-Oxygen Reforming of Methane
Steam-oxygen reforming activity of catalysts was determined as follows. The result is summerized in Table 3.
Other conditions were the same as those of Testing Example 1. For the reactant, 2:1:1 mixture of methane:oxgyen:steam was injected into the reactor. The temperature of the reactor was set to 750� C. The space velocity of the gas was controlled to 90,000 cc/hr�g-cat with a mass flow controller (MKS Instrument).
Initial activity and activity after catalytic activity 200 min were determined at 750� C. and atmospheric pressure by methane conversion and hydrogen yield, as in Testing Example 2. The catalyst activity ratio for methane conversion was determined by Equation 2.
θ-Al2O3[[3 m]]
1.02/1.01
Ni/Ca�Y�ZrO2/
Ni/Ca/Ce�Mg�ZrO2/
0.56/0.58
θ-Al2O3 Com. Ex. 2
0.82/0.92
Note: *Nickel Content (wt. %): against θ-Al2O3 **X (CH4): methane conversion As shown in Table 3, the reforming catalysts according to the present invention showed better activity and stability than those of Comparative Examples. Also, they have similar trend to that of steam reforming and oxygen reforming.
Ni/Ce�ZrO2/⊖-Al2O3 with 3 wt. % (Example 1) to 15 wt. % (Example 4) of nickel showed initial methane conversion larger than 90%. And, the methane conversion was maintained after 200 min without deactivation. The initial hydrogen yield larger than 100% was maintained after 200 min. The hydrogen yield larger than 100% is due to hydrogen production through water gas shift reaction by carbon monoxide and steam, other than hydrogen production through oxygen reforming: Also, all of Ni/La�ZrO2/⊖-Al2O3 (Example 5), Ni�Ca/Ce�ZrO2/⊖-Al2O3 (Example 6), Ni�Mg/La�ZrO2/⊖-Al2O3 (Example 7), Ni�Ca/Y�ZrO2/⊖-Al2O3 (Example 8), Ni�Ca/Ce�Mg�ZrO2/⊖-Al2O3 (Example 9) and Ni�Ca�Cs/La�ZrO2/⊖-Al2O3 (Example 10) showed initial methane conversion larger than 88% and initial hydrogen yield larger than 97%. And, they were stable after 200 min. Therefore, they have superior property as steam-oxygen reforming catalysts.
On the contrary, Ni/Ce�ZrO2/⊖-Al2O3 (Comparative Example 1) with 2 wt. % of nickel had initial methane conversion and hydrogen yield lower than 5%. They showed significant steam-oxygen reforming activity only when the nickel content was larger than 3 wt. %. Ni/⊖-Al2O3 with 3 wt. % of nickel (Comparative Example 2) had initial methane conversion and hydrogen yield lower than 5%, which are much lower than those of Example 1 with the same nickel content. Therefore, only modified ⊖-Al2O3 support shows good steam-oxygen reforming activity. Ni/α-Al2O3 of Comparative Example 3 and Ni/MgAl2O4 of Comparative Example 4 showed poor stability with time. In Comparative Example 3, activity after 200 min dropped to 85% of the initial activity, and in Comparative Example 4 to 98%. Consequently, the catalyst according to the present invention has superior activity and stability in steam-oxygen reforming.
As explained above, modified ⊖-Al2O3-supported nickel reforming catalyst according to the present invention is a new-concept nickel reforming catalyst, and if it is used for producing synthesis gas from methane natural gas, methane conversion can be increased in steam reforming, oxygen reforming and steam-oxygen reforming. Also, it has good catalytic stability. And, because inexpensive ⊖-Al2O3 is used as base support and only small amount of expensive zirconia or other metal components are used, it is very cost-effective.
Patent CitationsCited PatentFiling datePublication dateApplicantTitleUS3644198May 11, 1970Feb 22, 1972Universal Oil Prod CoHydrogen-consuming process and catalyst thereforUS4046715Feb 5, 1976Sep 6, 1977Universal Oil Products CompanyNonacidic multimetallic dehydrogenation catalystUS4079097Aug 27, 1976Mar 14, 1978Uop Inc.Normal paraffin hydrocarbon dehydrogenation with a nonacidic multimetallic catalytic compositeUS4471144Dec 13, 1982Sep 11, 1984Uop Inc.Theta-alumina as a hydrothermally stable support in hydrogenationUS4529718Jun 11, 1984Jul 16, 1985Rhone-Poulenc Specialites ChimiquesAlumina coating compositions for catalyst supports and process for their formulationUS4722920Feb 3, 1987Feb 2, 1988Kabushiki Kaisha Toyota Chuo KenyushoAlumina catalyst supportsUS4891350Oct 27, 1987Jan 2, 1990Rhone-Poulenc ChimieCatalyst supports and process for their preparationUS4918042Jul 8, 1988Apr 17, 1990Toyota Jidosha Kabushiki KaishaExhaust gas purifying catalystUS4920089May 3, 1988Apr 24, 1990Unilever Patent Holdings B.V.Hydrogenation catalystUS4962280Feb 1, 1989Oct 9, 1990Engelhard De Meern B. V.Carrier material for a catalyst and a process for making such a carrier materialUS4968660Feb 1, 1989Nov 6, 1990Veg-Gasinstituut N.V.Catalyst-on-carrier for the non-selective oxidation of organic compoundsUS5002909May 2, 1988Mar 26, 1991Montedison S.P.A.Mixed oxides of alumina and zirconia consisting essentially of spherical particles having a narrow granulometric distribution and process for their preparationUS5081095Sep 10, 1990Jan 14, 1992General Motors CorporationMethod of making a support containing an alumina-ceria washcoat for a noble metal catalystUS5102850Oct 17, 1990Apr 7, 1992W. R. Grace & Co. - Conn.Catalyst supports having promoter oxide gradient, resulting catalyst and method of making the supportsUS5155085Jun 27, 1991Oct 13, 1992Sumitomo Chemical Company, LimitedHeat resistant transition alumina and process for producing the sameUS5338488 *Sep 10, 1992Aug 16, 1994Council Of Scientific ResearchProcess for the production of synthesis gas by oxidative converson of methane (or natural gas) using composite catalyst containing transitional and alkine earth metal oxidesUS5368835 *Mar 16, 1993Nov 29, 1994Council Of Scientific & Industrial ResearchProcess for production of synthesis gas by oxidative conversion of methane or natural gas using composite catalystsUS5399537 *Aug 20, 1993Mar 21, 1995Amoco CorporationMethod for preparing synthesis gas using nickel catalystsUS5411927 *Aug 14, 1992May 2, 1995Council Of Scientific & Industrial ResearchProcess of preparing composite catalysts for production of synthesis gas by oxidative conversion of methane or natural gasUS5545602Apr 20, 1995Aug 13, 1996Texaco Inc.Catalyst with specified pore size distributionUS5597771Jun 24, 1994Jan 28, 1997Engelhard CorporationLayered catalyst compositeUS5756421 *Sep 20, 1995May 26, 1998Council Of Scientific & Industrial ResearchComposite catalysts containing transitional and alkaline earth metal oxides useful for oxidative conversion of methane (or natural gas) to carbon monoxide and hydrogen (or synthesis gas)US5849977Apr 10, 1996Dec 15, 1998UopMetal cation-modified alkylation catalystsUS5877106Jan 3, 1997Mar 2, 1999Asec ManufacturingStabilized crystalline alumina compositionsUS5972820Jan 19, 1999Oct 26, 1999Asec Manufacturing, A General PartnershipMethods of making stabilized crystalline alumina compositions, and alumina compositions and catalyst supports made therefromUS5980596 *Apr 25, 1997Nov 9, 1999Exxon Research And Engineering Co.Multi-injector autothermal reforming process and apparatus for producing synthesis gas (law 565).US6293979 *Feb 6, 1998Sep 25, 2001Council Of Scientific & Industrial ResearchProcess for the catalytic conversion of methane or natural gas to syngas or a mixture of carbon monoxide and hydrogenUS6326329Feb 20, 1997Dec 4, 2001Asec ManufacturingHighly dispersed substantially uniform mixed-metal-oxide composite supports for exhaust conversion catalystsUS6514904May 22, 2002Feb 4, 2003Uop LlcHydrocarbon conversion catalyst and process of using thereofKR20010046300A Title not availableKR20020021721A Title not availableKR20020026074A Title not available* Cited by examinerReferenced byCiting PatentFiling datePublication dateApplicantTitleUS6984371 *Oct 20, 2004Jan 10, 2006Sud-Chemie Inc.Process for catalytic reformingCN101829577A *Apr 23, 2010Sep 15, 2010浙江大学Composite catalyst, preparation and application thereof* Cited by examinerClassifications U.S. Classification252/373, 518/702, 518/715International ClassificationB01J23/755, C10G11/12, C01B3/40, B01J21/04, B01J23/83, B01J23/78, B01J21/06Cooperative ClassificationC01B3/40, B01J21/04, C01B2203/0233, B01J23/78, C01B2203/1052, C01B2203/1241, C01B2203/0261, B01J21/066, C01B2203/1082, C01B2203/0244, B01J23/83European ClassificationB01J21/06W, B01J23/78, B01J21/04, B01J23/83, C01B3/40Legal EventsDateCodeEventDescriptionApr 19, 2012FPAYFee paymentYear of fee payment: 8Dec 16, 2008FPExpired due to failure to pay maintenance feeEffective date: 20081026Dec 3, 2008FPAYFee paymentYear of fee payment: 4Dec 3, 2008SULPSurcharge for late paymentDec 1, 2008PRDPPatent reinstated due to the acceptance of a late maintenance feeEffective date: 20081203Oct 26, 2008REINReinstatement after maintenance fee payment confirmedMay 5, 2008REMIMaintenance fee reminder mailedRotateOriginal ImageGoogle Home - Sitemap - USPTO Bulk Downloads - Privacy Policy - Terms of Service - About Google Patents - Send FeedbackData provided by IFI CLAIMS Patent Services