以噴霧方式強化甲醇部份氧化產生氫氣之技術開發

科技部補助產學合作研究計畫成果精簡報告

以噴霧方式強化甲醇部份氧化產生氫氣之技術開發

計 畫 類 別 ： 技術及知識應用型

計 畫 編 號 ： MOST 107-2622-E-006-016-CC3 執 行 期 間 ： 107年06月01日至108年05月31日

執 行 單 位 ： 國立成功大學航空太空工程學系（所）

計 畫 主 持 人 ： 陳維新

計畫參與人員： 碩士班研究生-兼任助理：余俊鋒 碩士班研究生-兼任助理：盧貞聿 碩士班研究生-兼任助理：鄭靖霖

處 理 方 式 ： 公開方式：立即公開

中　華　民　國　108　年　07　月　07　日

中 文 摘 要 ： 本研究主要以噴霧作為進料系統，並搭配雙觸媒床用以進行甲醇部 分氧化（Partial oxidation of methanol ，POM）製造氫氣。本實 驗中，主要使用低Pt和Pd含量（0.2wt％）兩種不同之h-BN-

Pt/Al2O3和h-BN-Pd/Al2O3催化劑，探討不同預熱溫度（100、150、

200、250及300℃），O2與甲醇莫耳（O2 / C）比（0.4-0.8）和Pt / Pd比（0:1, 1:2, 1:4, 1:9）對於甲醇部分氧化反應效能之影響

。研究結果發現，當預熱溫度100℃即可使使Pd催化劑觸發甲醇部分 氧化反應。然而，隨著預熱溫度的增加，對整體反映性能沒有顯著 影響。由於Pt觸媒在甲醇部分氧化反應時的自熱特性，可用於替代 本研究中之預熱系統。本研究將Pt觸媒置於觸媒床上層，用以提供 下層Pd觸媒熱量。在O2/C = 0.6的操作條件下，可觀察到最大之氫 氣產率(1.61 mol (mol methanol)-1)。本研究中亦發現，減少Pt觸 媒之使用，對於POM反應性能影響不大，甲醇轉化率均接近

100％，氫氣產率為1.55-1.57mol(1.61 mol (mol methanol)-1)。

整體而言，POM可以藉由預熱後之h-BN-Pd / Al2O3或雙觸媒床（h- BN-Pd / Al2O3和h-BN-Pt / Al2O3）以冷啟動方式進行反應而產生 氫氣。另外，值得注意的是，在雙觸媒床中以少量（3g）Pt觸媒進 行的POM，可與使用單一Pd觸媒並進行預熱之操作條件達到相同的甲 醇轉化率和氫氣產量。

中 文 關 鍵 詞 ： 甲醇部分氧化；噴霧；雙觸媒床；貴金屬觸媒；氫氣製造。

英 文 摘 要 ： This study presents the hydrogen production from partial oxidation of methanol (POM) under sprays and dual-bed

catalysts. In the experiment, two different catalysts of h- BN-Pt/Al2O3 and h-BN-Pd/Al2O3 with low Pt and Pd contents (0.2 wt%) are utilized. The effects of different preheating temperatures (100, 150, 200, 250, 300 °C), O2-to-methanol molar (O2/C) ratios (0.4-0.8), and Pt/Pd ratios (0:1, 1:2, 1:4, 1:9) on POM are also examined. The results show that a preheating temperature as low as at 100 °C can lead the Pd catalyst to trigger a POM reaction. Nevertheless, there is no significant effect on performance with increasing

preheating temperature. Because of the autothermal property from the Pt catalyst during POM, it can be used to replace the preheating system in this study. The Pt catalyst is placed as the upper layer to provide heat for the Pd catalyst layer. The maximum H2 yield (1.61 mol (mol methanol)-1) is observed at O2/C=0.6. In this study, reducing the amount of the Pt catalyst does not significantly affect POM performance. The methanol

conversions are close to 100% and H2 yield is from 1.55 to 1.57 mol (mol methanol)-1. Overall, POM can be triggered by preheated h-BN-Pd/Al2O3 or by a dual-bed catalyst (h-BN- Pd/Al2O3 and h-BN-Pt/Al2O3) without preheating to produce hydrogen. It is noteworthy that the POM performed by a duel-bed catalyst together with a small amount (3g) of Pt catalyst can achieve a similar CH3OH conversion and

hydrogen production to that which use a full Pd catalyst with preheating.

英 文 關 鍵 詞 ： Partial oxidation of methanol (POM); Sprays; Dual-bed;

Noble-metal catalyst; hydrogen production.

以噴霧方式強化甲醇部份氧化產生氫氣之技術開發

Development of hydrogen production technology from methanol partial oxidation enhanced by sprays

計畫編號：MOST 107－2622－E－006－016－CC3 執行期限：107 年 6 月 1 日至 108 年 5 月 31 日 主持人：陳維新 國立成功大學 航空太空工程學系

Email：[email protected] 中文摘要

本研究主要以噴霧作為進料系統，並搭配雙觸媒床用以進行甲醇部分氧化（Partial oxidation of methanol ，POM）製造氫氣。本實驗中，主要使用低 Pt 和 Pd 含量（0.2wt％）兩種不同之 h-BN-Pt/Al

2

3

和 h-BN-Pd/Al

2

3

2

2

當預熱溫度≥100℃即可使使 Pd 催化劑觸發甲醇部分氧化反應。然而，隨著預熱溫度的增加，對整體

反映性能沒有顯著影響。由於 Pt 觸媒在甲醇部分氧化反應時的自熱特性，可用於替代本研究中之預熱

系統。本研究將 Pt 觸媒置於觸媒床上層，用以提供下層 Pd 觸媒熱量。在 O

2

可觀察到最大之氫氣產率(1.61 mol (mol methanol)

^-1

^-1

整體而言，POM 可以藉由預熱後之 h-BN-Pd / Al

2

3

2

3

2

3

關鍵詞：甲醇部分氧化（POM）；噴霧;雙觸媒床；貴金屬觸媒；氫氣製造。

Abstract

This study presents the hydrogen production from partial oxidation of methanol (POM) under sprays and dual-bed catalysts. In the experiment, two different catalysts of h-BN-Pt/Al

2

3

2

3

2

2

2

^-1

2

conversions are close to 100% and H

2

^-1

2

3

2

3

2

3

3

Keywords: Partial oxidation of methanol (POM); Sprays; Dual-bed; Noble-metal catalyst; hydrogen

1. Introduction

Nowadays, more and more studies have been focused on clean energy production using renewable resources such as hydrogen, which produces only water vapor when combusted. It is also considered a viable solution to environmental problems with its use in clean fuel cells. In fuel applications, hydrogen has the advantage of having zero greenhouse gas emissions and a high energy content (Abdalla et al., 2018). There are many kinds of feedstock used in the industrial hydrogen production from hydrocarbons such as methane, methanol, propane, butane, petroleum, and diesel (Basile et al., 2015). Methanol is one of the most suitable feedstock options for hydrogen production due to the following benefits: high H/C ratio, low risk, low cost, no sulfur dioxide generation, no carbon bond reduction of carbon deposition rate, and multiple regeneration manufacturing routes. The advantages of the catalyst is characterized by its rapid, low temperature (200-300°C) conversion conditions (Tang et al., 2015).

Thermochemical processes are common methods used to produce hydrogen from methanol, which include direct decomposition (Li et al., 2018), steam reforming (Chen et al., 2017; Lei et al., 2018), partial oxidation (Chen & Guo, 2018; Chen et al., 2015), and autothermal reforming (Chen & Syu, 2011; Ipsakis et al., 2017). Partial oxidation is an exothermic reaction, meaning that the reaction can be triggered without additional heating. The reaction does not require installation of an external heater and steam generator, as is necessary for steam reforming reactions. When the platinum-based (Pt-based) catalysts are used, partial oxidation of methanol can be cold started (Chen & Guo, 2018). Partial oxidation reactions have the advantage of requiring a shorter start-up time for reaction in the reactor.

The partial oxidation of methanol (POM) is expressed as

The POM reactions are often combined with catalysts. Copper supported catalyst is often adapted in POM reactions (Araiza et al., 2017; Gupta et al., 2018). Ag/ZnO was used in Sun et al. (Sun et al., 2018), the result showed high CH

3

2

CH

3

2

2

2

₂₉₈ ⁰

⁻¹

reduce the activation energy of methanol combustion and steam reforming reactions in POM (Schuyten et al., 2009). Agrell et al. (Agrell et al., 2003) showed that the palladium played a key role in determining product distribution. Previous studies also showed the combination of POM with catalysts under spray reaction systems (Chen & Guo, 2018; Chen & Shen, 2016). In terms of spray reaction systems, when the liquid is ejected from the nozzle, the liquid disintegrates and forms many droplets due to the turbulence in the liquid, cavitation in the nozzle, and aerodynamic interactions with the surrounding air. The system can spray methanol evenly on the reaction bed, and with the uniform and high contact area. The reaction is stable and goes to completion.

A dual-bed set-up was used to enhance the H

2

The results indicated that CO production was effectively reduced up to around 80% compared to single reactor and the average conversion of ethanol could be achieved up to 90%. Tong et al. (Tong et al., 2005) compared two separate dual catalyst beds (Pt/Ni and Ni/Pt) to a single catalyst bed (Pt or Rh). The results demonstrated that the dual-bed achieved higher CH

4

2

From the literature, it is found that both the Pd and Pt catalysts have been applied in POM for hydrogen production. However, the related information about the effects of the preheating and different ratios of Pt/Pd in duel-bed is still not sufficient, especially in a spray system. For that, a comprehensive study of POM with sprays by a h-BN-Pd/Al

2

3

The influence of preheating temperature of the h-BN-Pd/Al

2

3

2

3

2

3

2

3

2

3

Meanwhile, because of the high cost of Pt compared to Pd, the study also aims to reduce the amount of h-BN-Pt/Al

2

3

2. Experimental 2.1. Reaction system

The overall experimental system was divided into four units: the feeding unit, the reaction unit, the gas treatment unit, and the gas analysis unit. The feeding unit was employed with both N

2

2

Moreover, the h-BN-Pt/Al

2

3

2

3

layer to substitute the heating tape. In the gas treatment unit, a condenser (YIHDER, BL710) and a dryer were used for removing the moisture in the product gas. The gas analysis unit was made up of a gas analyzer (GA, Fuji ZRJF5Y23-AERYR-YKLYYCY-A) and a gas chromatography unit (GC, SRI 8610C) to measure the gas concentrations.

2.2.Experimental procedure

Two commercial catalysts (Green Hydrotech Inc.) of h-BN-Pt/Al

2

3

2

3

2

3

h-BN-Pt/Al

2

3

2

3

2

3

2

2

3

2

2

Table 1. Volumetric flow rates of feed gas, air, and N 2

O 2 /C Feed gas (Air+N 2 )

(mL min ^-1 )

Air

(mL min ^-1 )

N 2

(mL/min ^-1 )

0.4 5417 1167 4250

0.5 1458 3959

0.6 1750 3667

0.7 2042 3375

0.8 2333 3084

In this study, the amount of catalyst for POM is fixed at 30 g. Four catalyst ratios (Pt:Pd) 0:1, 1:2, 1:4, 1:9 were considered in the different catalyst ratio cases. In all experiments, a mixture of air and N

2

^-1

^-1

2

4

2

^-1

The flow rate of the product gas was measured by flow rate meter. Based on the flow rate and the concentrations of CO, CO

2

4

CH

₃

= �𝑛𝑛̇

𝐶𝐶𝑂𝑂 _2, 𝑜𝑜𝑜𝑜𝑜𝑜

𝐶𝐶𝑂𝑂,𝑜𝑜𝑜𝑜𝑜𝑜

𝐶𝐶𝐻𝐻 _4, 𝑜𝑜𝑜𝑜𝑜𝑜

𝑛𝑛̇

𝐶𝐶𝐻𝐻 ₃ 𝑂𝑂𝐻𝐻,𝑖𝑖𝑖𝑖

where 𝑛𝑛̇ stands for the molar flow rate (mol min

^-1

2

^-1

𝐻𝐻 ₂

H

₂

₃

𝐻𝐻 ₂

𝑛𝑛̇

_{𝐶𝐶𝐻𝐻 3 𝑂𝑂𝐻𝐻}

3. Results and discussion

3.1. POM via h-BN-Pd/Al 2

3 catalyst 3.1.1. Temperature distributions

Fig. 1 shows the profiles of temporal distribution of reaction temperature in preheated h-BN-Pd/Al 2

3

catalyst beds at O

2

2

3

According to this observation, it is suggested that preheating is required to provide energy for chemical reaction to reach the initial energy required while using Pd catalyst alone. The higher the preheating temperature, the higher the energy is provided to activate POM in the beginning. The reaction time can be reduced from beginning to stabilization of POM. By preheating, the h-BN-Pd/Al

2

3

Fig. 1

2

3

2

Time(min) T e m p e ra tu re (

C )

0 10 20 30 40

0 100 200 300 400 500 600

100(

C)

150(

C)

200(

C)

250(

C)

300(

C)

Fig. 2 shows the profiles of H 2

3

2

^-1

2

^-1

3

3

CH

3

2

₂₉₈ ⁰

⁻¹

The highest CH

3

2

3

3

2

Fig. 2

2

3

3.2. POM via dual-bed catalyst

As the experimental results in 3.1, the Pd catalyst is unable to trigger POM under cold start. For that, h-BN-Pt/Al

2

3

2

3

2

3

2

3

Fig. 3 shows the profiles of reaction temperature with O 2

Preheat temperature ( ^o C)

H 2 y ie ld (m o l/ m o l C H 3 O H ) C H 3 O H c o n v e rs io n (% )

50 100 150 200 250 300 350

0 0.5 1 1.5 2

0 20 40 60 80 100 120

H

yield (mol/mol CH

OH) 140

CH

OH conversion (%)

0.4-0.8 in dual-bed catalyst. In Fig. 3a, the reaction temperature of h-BN-Pt/Al

2

3

2

The reaction temperature was varied from 275 °C to 599 °C. Shown in Fig. 3b, the heat generation from the Pt catalyst autothermally provides the Pd catalyst with sufficient energy to trigger the POM in the lower layer.

The reaction temperature of Pd catalyst is from 275 °C to 540 °C. Overall, the reaction temperature is higher when the O

2

2

3

2

3

layer. According to this result, the Pt catalyst can replace the preheating tape completely for POM, also reducing the cost and experimental procedure.

Fig. 3

2

3

2

3

2

Fig. 4 shows the profiles of H 2

3

2

2

^-1

2

2

2

Time (min) T e m p e ra tu re ( o C )

0 10 20 30 40

0 100 200 300 400 500 600 700 800

O₂/C=0.4 O₂/C=0.5 O₂/C=0.6 O₂/C=0.7 O₂/C=0.8

(a) h-BN-Pt/Al

O

Time (min) T e m p e ra tu re ( o C )

0 10 20 30 40

0 100 200 300 400 500 600 700 800

(b) h-BN-Pd/Al

O

methanol) at O

2

3

2

2

Fig. 4

2

3

2

3.3. Effects of Pt/Pd ratio in duel-bed on POM

Fig. 5 shows the profiles of reaction temperature in Pt and Pd catalyst beds at different Pt/Pd ratios. In Fig. 5a, the reaction temperature of the Pt

°C; any change in Pt quantity does not have significant effect on the reaction temperature of Pd (Fig. 5b).

Therefore, only 3 g of Pt catalyst can provide enough energy for the activation of POM on 27 g of Pd catalyst.

O ₂ /C

H 2 y ie ld (m o l/ m o l C H 3 O H ) C H 3 O H c o n v e rs io n (% )

0.3 0.4 0.5 0.6 0.7 0.8 0.9

0 0.5 1 1.5 2

0 20 40 60 80 100 120

H

yield (mol/mol CH

OH) 140

CH

OH conversion (%)

Fig. 5

2

3

2

3

Fig. 6

2

3

2

^-1

2

^-1

3

Time (min) T e m p e ra tu re (

C )

0 10 20 30 40

0 200 400 600 800

Pt/Pd=1:0 Pt/Pd=1:2 Pt/Pd=1:4 Pt/Pd=1:9

(a) h-BN-Pt/Al

O

Time (min) T e m p e ra tu re (

C )

0 10 20 30 40

0 200 400 600 800

(b) h-BN-Pd/Al

O

Fig. 6

2

3

4. Conclusions

The h-BN-Pd/Al

2

3

2

3

2

2

3

2

^-1

3

2

3

2

3

2

3

2

2

3

2

2

2

yield and CH

3

2

^-1

3

Pt/Pd

H 2 y ie ld (m o l/ m o l C H 3 O H ) C H 3 O H c o n v e rs io n (% )

0 0.5 1 1.5 2

0 20 40 60 80 100 120 CH

OH conversion (%) 140

H

yield (mol/mol CH

OH)

1:0 1:2 1:4 1:9

Reference

Abdalla, A.M., Hossain, S., Nisfindy, O.B., Azad, A.T., Dawood, M., Azad, A.K. 2018. Hydrogen production, storage, transportation and key challenges with applications: A review. Energy

Conversion and Management, 165, 602-627.

Agrell, J., Germani, G., Järås, S.G., Boutonnet, M. 2003. Production of hydrogen by partial oxidation of methanol over ZnO-supported palladium catalysts prepared by microemulsion technique. Applied

Catalysis A: General, 242(2), 233-245.

Araiza, D.G., Gómez-Cortés, A., Díaz, G. 2017. Partial oxidation of methanol over copper supported on nanoshaped ceria for hydrogen production. Catalysis Today, 282, 185-194.

Basile, A., Iulianelli, A., Tong, J. 2015. 6 - Membrane reactors for the conversion of methanol and ethanol to hydrogen. in: Membrane Reactors for Energy Applications and Basic Chemical Production, (Eds.) A.

Basile, L. Di Paola, F.l. Hai, V. Piemonte, Woodhead Publishing, pp. 187-208.

Batista, M.S., Assaf, E.M., Assaf, J.M., Ticianelli, E.A. 2006. Double bed reactor for the simultaneous steam reforming of ethanol and water gas shift reactions. International Journal of Hydrogen Energy, 31(9), 1204-1209.

Chen, C.-C., Tseng, H.-H., Lin, Y.-L., Chen, W.-H. 2017. Hydrogen production and carbon dioxide enrichment from ethanol steam reforming followed by water gas shift reaction. Journal of Cleaner

Production, 162, 1430-1441.

Chen, W.-H., Guo, Y.-Z. 2018. Hydrogen production characteristics of methanol partial oxidation under sprays with ultra-low Pt and Pd contents in catalysts. Fuel, 222, 599-609.

Chen, W.-H., Shen, C.-T. 2016. Partial oxidation of methanol over a Pt/Al2O3 catalyst enhanced by sprays.

Energy, 106, 1-12.

Chen, W.-H., Shen, C.-T., Lin, B.-J., Liu, S.-C. 2015. Hydrogen production from methanol partial oxidation over Pt/Al2O3 catalyst with low Pt content. Energy, 88, 399-407.

Chen, W.-H., Syu, Y.-J. 2011. Thermal behavior and hydrogen production of methanol steam reforming and autothermal reforming with spiral preheating. International Journal of Hydrogen Energy, 36(5), 3397-3408.

Demiral, İ., Ayan, E.A. 2011. Pyrolysis of grape bagasse: Effect of pyrolysis conditions on the product yields and characterization of the liquid product. Bioresource Technology, 102(4), 3946-3951.

Gupta, S., Kua, H.W., Low, C.Y. 2018. Use of biochar as carbon sequestering additive in cement mortar.

Cement and Concrete Composites, 87, 110-129.

Ipsakis, D., Ouzounidou, M., Papadopoulou, S., Seferlis, P., Voutetakis, S. 2017. Dynamic modeling and control analysis of a methanol autothermal reforming and PEM fuel cell power system. Applied

Energy, 208, 703-718.

Lei, Y., Luo, Y., Li, X., Lu, J., Mei, Z., Peng, W., Chen, R., Chen, K., Chen, D., He, D. 2018. The role of samarium on Cu/Al2O3 catalyst in the methanol steam reforming for hydrogen production. Catalysis

Today, 307, 162-168.

Li, G., Gu, C., Zhu, W., Wang, X., Yuan, X., Cui, Z., Wang, H., Gao, Z. 2018. Hydrogen production from methanol decomposition using Cu-Al spinel catalysts. Journal of Cleaner Production, 183, 415-423.

Lv, X., Xiao, J., Du, Y., Shen, L., Zhou, Y. 2014. Experimental study on biomass steam gasification for hydrogen-rich gas in double-bed reactor. International Journal of Hydrogen Energy, 39(36),

20968-20978.

Schuyten, S., Guerrero, S., Miller, J.T., Shibata, T., Wolf, E.E. 2009. Characterization and oxidation states of Cu and Pd in Pd–CuO/ZnO/ZrO2 catalysts for hydrogen production by methanol partial oxidation.

Applied Catalysis A: General, 352(1), 133-144.

Sun, Q., Men, Y., Wang, J., Chai, S., Song, Q. 2018. Support effect of Ag/ZnO catalysts for partial oxidation of methanol. Inorganic Chemistry Communications, 92, 51-54.

Tang, H.-Y., Greenwood, J., Erickson, P. 2015. Modeling of a fixed-bed copper-based catalyst for reforming methanol: Steam and autothermal reformation. International Journal of Hydrogen Energy, 40(25), 8034-8050.

Tong, G.C.M., Flynn, J., Leclerc, C.A. 2005. A dual catalyst bed for the autothermal partial oxidation of methane to synthesis gas. Catalysis Letters, 102(3), 131-137.

Ubago-Pérez, R., Carrasco-Marín, F., Moreno-Castilla, C. 2007. Methanol partial oxidation on carbon-supported Pt and Pd catalysts. Catalysis Today, 123(1), 158-163.

107年度專題研究計畫成果彙整表

計畫主持人：陳維新 計畫編號：107-2622-E-006-016-CC3

計畫名稱：以噴霧方式強化甲醇部份氧化產生氫氣之技術開發

成果項目 量化 單位

質化

（說明：各成果項目請附佐證資料或細 項說明，如期刊名稱、年份、卷期、起 訖頁數、證號...等） 　　　　　　　

國 內

學術性論文

期刊論文 0

研討會論文 2 篇

1. Guo YZ, Chen WH，“Comparison of hydrogen production over Pt and Pd catalysts from methanol partial oxidation using sprays”，第十二屆 全國氫能與燃料電池學術研討會

，2017年10月12-13日，國立東華大學。

2. Chen HH, Chen WH, Guo YZ.

“Hydrogen production from methanol partial oxidation under sprays and dual-bed catalysts”，中華民國第 28屆燃燒與能源學術研討會，2018年4月 27-28日，國立中央大學。

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件

陳維新、邱國倫，“噴霧產氫系統

（Hydrogen production system using sprays）” ，中華民國發明專利（Reg.

no. 108123318）。

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外 學術性論文 期刊論文 1 篇

Chen WH*, Guo YZ. 2018. Hydrogen production performance of methanol partial oxidation under sprays with ultra-low Pt and Pd contents in catalysts. Fuel. Vol. 222, pp.599- 609.

研討會論文 1

Chen WH, Chen KH, Guo YZ. Hydrogen production characteristics from catalytic methanol partial oxidation in sprays. The 14th International Conference on Liquid Atomization and Spray Systems (ICLASS 2018), Chicago, USA, July 22-26, 2018.

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2018科技部傑出研究獎

Web of Science (Clarivate Analytics) 2018 Highly Cited Researcher

李國鼎金質獎

2018 Bioresource Technology Award for Highly Cited Review Article

本產學合作計畫研發成果及績效達成情形自評表

成果項目 本產學合作計畫預估研究成果及績效指標

（作為本計畫後續管考之參據） 計畫達成情形

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之具體績效 新公司或衍生公司 0 家 設立新公司或衍生公司(名稱)：

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：請以文字敘述計 畫非量化產出之技 術應用具體效益。

（限600字以內）

本研究以噴霧作為進料系統，並搭配雙觸媒床用以進行甲醇部分氧化製造氫氣

，其中雙觸媒床包含h-BN-Pt/Al2O3和h-BN-Pd/Al2O3催化劑。Pt觸媒可進行冷起 動甲醇部分氧化反應，但其成本較高；Pd 觸媒則需預熱才可進行甲醇部分氧化反 應。因此，本計畫進行兩種觸媒組合策略之研究，以降低進行甲醇部分氧化反應 之成本。其中觸媒組合之策略為Pt觸媒置於觸媒床上層，用以提供下層Pd觸媒熱 量。本研究中亦發現，減少Pt觸媒之使用，對於POM反應性能影響不大，甲醇轉化 率均接近100％，氫氣產率為1.55-1.57 mol (mol methanol)-1。整體而言，Pt / Pd比為1:9即可達成組合策略之目標。本研究對於工業以噴霧方式進行甲醇部分氧 化製造氫氣將有所幫助。

請就研究內容與原 計畫相符程度、達 成預期目標情況作 一綜合評估　　　

■達成目標

□未達成目標（請說明，以100字為限）

　　□實驗失敗 　　□因故實驗中斷 　　□其他原因 說明：

本研究具有政策應 用參考價值　　　

■否

□是，建議提供機關

（勾選「是」者，請列舉建議可提供施政參考之業務主管機關）

本研究具影響公共 利益之重大發現　

□否

□是

說明：（以150字為限）