Patent Application
20100092380
1. Field of the Invention
The present invention relates to a method for generating hydrogen, and particularly to a self-started OSRM process at room temperature for hydrogen production.
2. Description of the Prior Art
Fuel cells capable of converting chemical energy of the fuel into electricity and also satisfying the requirement of environmental protection are now being continuously developed. Hydrogen fuel cells (HFC) take advantage of lower operation temperature and are of great potential among those developing fuel cells. However, HFCs have disadvantages in storage and transportation of hydrogen. Hydrocarbon molecules are used as the external primary fuel in PEMFCs and converted into hydrogen rich gas (HRG) on site. HRG is gas mixture with high hydrogen content and one of environmentally friendly fuels applied in fuel cells.
Production of HRG from reforming of methanol has been widely studied because it is highly chemically active, abundant, and cheap. Many methanol reforming processes have been developed and published in literatures, for example, (1) “steam reforming of methanol” (SRM) and (2) “partial oxidation of methanol” (POM), which may be expressed by the following chemical formulas.
CH3OH+H2O→3H2+CO2 ΔH=49 kJ mol−1 (1)
CH3OH+1/2 O2→2H2+CO2 ΔH=−192 kJ mol−1 (2)
Reaction SRM has a high hydrogen yield (number of hydrogen molecule produced from each consumed methanol molecule) of RH2=3.0. However, SRM is an endothermic reaction which is not theoretically favored at low temperatures. According to Le Chatelier's Principle, SRM becomes efficient at high temperatures.
Comparatively, exothermic POM is favored at lower temperatures. However, compared to SRM theoretical value of RH2=3.0, a lower hydrogen yield of RH2=2.0, is produced.
A more advanced process is called “oxidative steam reforming of methanol” (OSRM). OSRM uses a mixture of water vapor and oxygen as oxidant. In other words, it is a combination of reactions (1) and (2) in an optional ratio. Theoretically, negligible reaction heat may occur at ratio 3.9/1. On one hand, a desirably high RH2 (about 2.75) may be generated by adding steam, and on the other hand, the CO content in HRG and the reaction temperature can be decreased due to the presence of oxygen in the OSRM reaction.
There are many OSRM-related prior art references. Some use supported copper catalysts such as Cu/ZnO—Al2O3 and Cu/ZrO2, as disclosed in WO publication No. 2004/083116 belonging to Schlogl et al., for example. The Cu—Al alloy and transition metal catalyst (containing no copper) disclosed in WO publication No. 2005/009612 A1 belonging to Tsai et al improves the stability of copper catalyst and lowers the cost; however, the reaction has to be initiated at a reaction temperature of TR>240° C. Furthermore, US publication No. 2006/0111457 A1 belonging to C H Lee et al adopts Pt/CeO2—ZrO2 catalysts instead of conventional Cu/ZnO—Al2O3 catalysts to improve stability; however, the reaction still has to be initiated at a reaction temperature of TR>300° C. Some use Pd/CeO2—ZrO2 catalyst, as disclosed in US publication No. 2001/0021469 A1 and 2001/0016188 A1 belonging to Kaneko et al. and Haga et al., or Pd—Cu/ZnO alloy catalyst, as disclosed in WO published patent 96/00186 belonging to Edwards et al. These catalysts require a reaction temperature of TR>200° C. to catalyze OSRM and the selectivity of CO in HRG is high (Sco>2). If copper catalyst dispersed on mixed zinc, aluminum and zirconium oxide is used, the CO selectivity may be decreased to Sco<1% (US publication No. 2005/0002858 belonging to Suzuki et al.), but a TR>200° is still required. The gold catalyst disclosed in US publication No. 2006269469 belonging to Yeh et al. may catalyze methanol at reaction temperature TR=150° C. to generate HRG with low Sco. However these OSRM process can not be initiated at room temperature and need external heat to initiate the hydrogen generating reaction.
Table 1 shows the comparisons of different catalyst systems for the OSRM disclosed in other known references. It is observed that all of the catalyst systems require a temperature of TR>200° C. to effectively catalyze the OSRM.
(1) Perez-Hernandez, R., Gutierrez-Martinez, A., Gutierrez-Wing, C. E., Int. J. Hydrogen Energy. 32, 2888-2894 (2007);
(2) Tetsuya Shishido, Yoshihiro Yamamotob, Hiroyuki Morioka, Katsuomi Takehira., J. Mol. Catal. A: Chem. 268, 185-194 (2007);
(3) Velu, S., Suzuki, K., Kapoor, M. P., Ohashi, F., and Osaki, T., Appl. Catal. A: 213, 47 (2001);
(4) Shen, J-P., and Song C., Catal. Today 77, 89 (2002);
(5) Velu, S., and Suzuki, K., Topics in Catal. 22, 235 (2003);
(6) Nobuhiro Iwasa, Masayoshi Yoshikawa, Wataru Nomura, Masahiko Arai., Appl. Catal., A 292, 215-222(2005)
(7) Lenarda, M., Storaro, L., Frattini, R., Casagrande, M., Marchiori, M., Capannelli, G., Uliana, C., Ferrari, F., Ganzerla, R., Catal. Commun. 8, 467-470 (2007)
(8) Liu, S., Takahashi, K., and Ayabe, M., Catal. Today 87, 247 (2003)°
To sum up, a self-started OSRM process at room temperature to obtain low Sco and high RH2 for hydrogen at TR<200° C. is highly desired.
The present invention is directed to provide a hydrogen production process at low temperature, wherein the RH2 for the process is greater than 2.
The present invention is also directed to provide a self-started OSRM process at room temperature for hydrogen production, and a catalyst thereof, wherein no external heat is required for initiating the OSRM process, and the generated hydrogen could be applied in fuel cells.
The self-started OSRM process at room temperature for hydrogen production according to an embodiment includes the following steps. An aqueous methanol and oxygen is pre-mixed to obtain a mixture. The mixture is fed to a fixed-bed reactor at room temperature, wherein the Cu/ZnO-based catalyst, a CuPd/ZnO catalyst or a CuRh/ZnO catalyst. An exothermic OSRM process is initiated at room temperature and the temperature of the mixture is raised. Hydrogen is measured at a reaction temperature equal to or greater than about 140, wherein the hydrogen contains smaller than or equal to 1% CO by mole.
The catalyst used in the self-started OSRM process at room temperature for hydrogen production according to an embodiment is disclosed. The catalyst includes a Cu/ZnO-based catalyst comprising a CuPd/ZnO catalyst or a CuRh/ZnO catalyst, wherein the Cu/ZnO-based catalyst is a supported copper catalyst prepared with a co-precipitation method, a Cu content in the Cu/ZnO-based catalyst is between about 10% and about 35% (w/w), and a ZnO content in the Cu/ZnO catalyst is greater than about 60.0% (w/w).
The foregoing aspects and many of the accompanying advantages of this invention will become more readily appreciated as the same becomes better understood by reference to the following detailed description, when taken in conjunction with the accompanying drawings, wherein:
FIGURE is a schematic diagram illustrating an embodiment of the present invention.
The present invention catalyzes an OSRM (oxidative steam reforming of methanol) process to generate a HRG (hydrogen rich gas) by taking advantage of a supported CuPd/ZnO catalyst or a supported CuRh/ZnO catalyst. The catalysts have higher methanol conversion rate (CMeOH) and lower CO selectivity (SCO) at a lower reaction temperature (TR≈140° C). The small amount of Cu and Pd or Rh particles are evenly distributed on a suitable support and provide good catalytic activity of the CuPd/ZnO or CuRh/ZnO catalyst.
Preparation of Catalyst
The supported Cu/ZnO-based catalyst used in the present invention is generally prepared with a co-precipitation method. In one example, a 70° C. mixture solution containing Cu(NO3)2, Pd(NO3)2, and Zn(NO3)2 is added to 1M NaHCO3 solution, and the pH value for the co-precipitation method is adjusted between 6 and 9 to generate a dark colored precipitate. The precipitate is then dried at 100° C. and calcined at 400° C. to obtain a fresh Cu/PdxZnO-y catalyst (in which x represents the percentage of oxidized Pd (w/w), and y represents the pH value of precipitation). The Cu content in the CuPd/ZnO catalyst prepared with the above co-precipitation method may vary from 10% to 35%.
OSRM Process System and Method for Testing Catalytic Reaction
FIGURE illustrates an OSRM process system for hydrogen production based on a self-started OSRM process at room temperature according to one embodiment of the present invention. A 0.1 g reduced catalyst sample (60˜80 mesh) is placed in a quartz tube with 4 mm inner diameter in which the catalyst is immobilized with silica wool in a fixed bed reactor or a thermally-insulated reactor 100. With regard to reacting gases, an aqueous methanol is evaporated with a pre-heater at a flow rate controlled by a liquid pump. Each flow rate of oxygen and carrier gas (e.g. Ar) is respectively controlled by a flow mass controller. The oxygen, Ar, and the gas evaporated from the aqueous methanol are charged into a mixing chamber and mixed homogeneously (2.89% O2, 15.02% H2O, 11.56% CH3OH, 70.53% Ar; nH2O/nMeOH=1.3, nO2/nMeOH=0.5) to obtain a mixture. The mixture (reactant 300) is then fed to a catalyst bed 200 in the thermally-insulated reactor 100 to generate product 400.
The product 400 is then subjected to a qualitative separation process via two GC (gas chromatography), in which the H2 and CO are separated by a Molecular Sieve 5A chromatography column, and H2O, CO2, and CH3OH are separated by a Porapak Q chromatography column, and a quantitative analysis carried out by a TCD (thermal conductivity detector).
After the quantitative analysis via TCD, a methanol conversion rate (CMeOH) and CO selectivity (SCO) are calculated as follows:
C
MeOH=(nMeOH,in−nMeOH,out)/nMeOH,in×100%
S
CO
=n
CO/(nCO2+nCO)×100%
R
H2
=n
H2/(nMeOH,on−nMeOH,out).
A higher CMeOH in the OSRM process represents the higher amount of reacted methanol in the whole process. The hydrogen may be generated from the OSRM process as well as oxidized with the oxygen in the reacting gases. A higher SCO represents that the carbon in the methanol is more likely desorbed in way of CO after the methanol is dehydrogenated; that is to say a less selectivity of CO2.
OSRM Process System and Method for Testing Catalytic Reaction
The test is performed by feeding the mixture to 100 mg catalyst sample at a fixed flow rate (1.2 ml/hr) in the fixed-bed reactor. A water/methanol molar ratio (w) in the aqueous methanol is controlled by a liquid feeding pump. An oxygen/methanol molar ratio (x) is controlled regulating a flow rate of the oxygen. A flow rate for overall reactant feeding is controlled to 100 ml/min via the carrier gas Ar. The contact time for the process is thus fixed approximately to Wcat/F=1×10−3 min g ml−1.
The reactant is evaporated using a pre-heater before being directed into the reactor. All catalysts applied in the process are activated with hydrogen reduction for 1 hour at 200° C. before the process and then applied. The experimental outcomes in the presence of different variants are listed in Table 2.
Influence of Adding Rh and Pd into the Cu/ZnO-Based Catalyst
The experiment 1 in the Table 2 is performed with Cu/ZnO-based catalyst without Pd loading under the condition of x=0.25 and w=1.3. It shows that CMeOH is lower than 40% when the reaction temperature is lower than 190° C. and the reaction couldn't be initiated at room temperature. In addition, the Cu/ZnO-based catalyst with Pd loading could initiate the process at room temperature according to experiment 2 to 7. In another example, another transition metal, Rh, with the same 4 d orbital is applied to form a CuRh/ZnO catalyst for catalyzing the process. In comparison with experiments 8 and 9, despite initiating the process at room temperature, the CuRh/ZnO catalyst has no significantly better CMeOH and SCO than the Cu/ZnO-based catalyst and lower RH2 than the ideal value for the POM process; therefore, the CuRh/ZnO catalyst is not as good as the CuPd/ZnO.
Influence of Water/Methanol Molar Ratio on OSRM Process
The water/methanol molar ratios (w) are varied to determine the influence of water/methanol molar ratio on the CMeOH, RH2 and SCO in the CuPd/ZnO-catalyzed OSRM process according to the experiments 1 to 7 in Table 2 in which the reaction temperature is set at 170° C. or 190° C. Here, a Cu30Pd2ZnO catalyst which contains 2% Pd is applied, and the oxygen/methanol molar ratio (x) is fixed to 0.25.
In comparison with experiment 3, 5 and 7 where x=0.25, SCO reaches 10% when w=1.0 and reaches 3% when w=1.5. Though the above Pd-containing Cu/ZnO-based catalysts initiate the process at room temperature, redundant CO may poison the platinum electrode in proton exchange membrane fuel cells and are therefore unable to meet the requirement of low CO content hydrogen gases in a hydrogen reformers. To sum up, w=1.3 is the preferred option.
Influence of Oxygen/Methanol Molar Ratio on the OSRM Process
The molar ratios of oxygen to methanol (x) are varied to determine the influence of oxygen/methanol molar ratio on the CMeOH, RH2 and SCO in the CuPd/ZnO-catalyzed OSRM process according to the experiments 4, 5 and 10 to 13 in Table 2 in which the reaction temperature is set at 170° C. or 190° C. Here, a Cu30Pd2ZnO catalyst which contains 2% Pd is applied, and the water/methanol molar ratio (w) is fixed to 1.3.
The outcome shows when x is equal to or smaller than 0.1, the processes tend to be endothermic SRM (steam reforming of methanol) processes and can not be initiated at room temperature even in the presence of Pd-containing Cu/ZnO-based catalyst. When x=0.25 or x=0.5, the process can be initiated with the assistance of exothermic POM (partial oxidation of methanol), and the CMeOH increases as the oxygen/methanol molar ratio increases. In addition, RH2 also increases as the oxygen/methanol molar ratio increases. That is to say a proper oxygen/methanol molar ratio may contribute to the optimization RH2 of methanol. As mentioned above, redundant CO would poison the platinum electrodes; however, it shows no significant SCO variation (2%˜3%), in which the SCO at x=0.5 is greater than the SCO at x=0.1, and the SCO at x=0.1 is greater than the SCO at x=0.25. According to experiment 14, at x=0.5 and w=1.3, the reaction temperature for OSRM process is 140° C., the CMeOH is 97%, and SCO is 2.5% though with relatively low RH2. Here, it should be noted that this OSRM process may be initiated at room temperature and reach the reaction temperature. In case of x=0.6 (experiment 15), the RH2 at 170° C. is much lower than 2, and the process would be initiated and reach the reaction temperature of 170° C. It shows that the process is prone to POM and completely oxidized methanol in this state; x=0.5 is thus the preferred option in consideration of the influence of initiation temperature on RH2.
A self-started OSRM process at room temperature for hydrogen production according to an embodiment includes the following steps. An aqueous methanol and oxygen is pre-mixed to obtain a mixture. The mixture is fed to a Cu/ZnO-based catalyst at room temperature, wherein the Cu/ZnO-based catalyst includes a CuPd/ZnO catalyst or a CuRh/ZnO catalyst. An OSRM process is catalyzed and raises the temperature of the catalyst bed. Hydrogen is yielded at a reaction temperature substantially equal to or greater than about 140, wherein the hydrogen contains substantially smaller than or equal to 1% CO by mole.
The catalysts used in a self-started OSRM process at room temperature for hydrogen production according to an embodiment are disclosed. The catalysts include a Cu/ZnO-based catalyst comprising a CuPd/ZnO catalyst or a CuRh/ZnO catalyst, wherein the Cu/ZnO-based catalyst is a supported copper catalyst prepared with a co-precipitation method, the Cu content in the Cu/ZnO-based catalyst is substantially between about 10% and about 35% (w/w), and the ZnO content in the Cu/ZnO-based catalyst is substantially greater than about 60.0% (w/w).
To sum up, the present invention provides a self-started OSRM process at room temperature for hydrogen production and a catalyst thereof. Firstly, an aqueous methanol and oxygen is pre-mixed to obtain a mixture, wherein a water/methanol molar ratio in the aqueous methanol is in a range between 1 and 1.5 and an oxygen/methanol molar ratio in the mixture is smaller than or equal to 0.5. The mixture is fed to a Cu/ZnO-based catalyst at room temperature for an OSRM process to be catalyzed. The temperature is spontaneously raised to the reaction temperature wherein no external heat is required for initiating the OSRM process. Ideal values of CMeOH and RH2 are then obtained.
According to a preferred example, the oxygen is provided with pure oxygen or air. The catalyst includes Cu particles on a support containing ZnO, wherein the Cu content is substantially between 10% and 35% (w/w), and the diameter of CuO is smaller than or equal to 5 nm. The Pd content is substantially between 1% and 4% (w/w), and the diameter of PdO is smaller than or equal to 10 nm.
The reaction temperature for OSRM process is about 140° C. and therefore compliant with the operating temperature of hydrogen fuel cells. Further, the present invention initiates the OSRM process at room temperature and raises the temperature to the reaction temperature without requiring any external heat supply.
To sum up, the CuPd/ZnO catalyst of the present invention plays an important role in the exemplified self-started OSRM process at room temperature for hydrogen production. The CuPd/ZnO catalyst enables the initiation of the OSRM process at room temperature and lower reaction temperature (TR≈140° C). of the OSRM process. Thus, the energy supply and start-up time in the hydrogen reformer is greatly decreased, and higher CMeOH as well as RH2 is then achieved. The application of present invention may influence the development of petroleum industry, fuel cell, and hydrogen economics. For example, the CuPd/ZnO catalyst of the present invention which catalyzes the OSRM process at room temperature to obtain high-yielding hydrogen may be applied in proton exchange membrane fuel cells which will be the potential power supply for notebooks, cellular phones, and digital camera.
While the invention is susceptible to various modifications and alternative forms, a specific example thereof has been shown in the drawings and is herein described in detail. It should be understood, however, that the invention is not to be limited to the particular form disclosed, but to the contrary, the invention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 97139301 | Oct 2008 | TW | national |
