WO2014092482A1 - 수증기-이산화탄소 개질에 의한 합성가스 제조용 란탄함유 촉매 및 이를 이용한 합성가스 제조방법 - Google Patents
수증기-이산화탄소 개질에 의한 합성가스 제조용 란탄함유 촉매 및 이를 이용한 합성가스 제조방법 Download PDFInfo
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- WO2014092482A1 WO2014092482A1 PCT/KR2013/011531 KR2013011531W WO2014092482A1 WO 2014092482 A1 WO2014092482 A1 WO 2014092482A1 KR 2013011531 W KR2013011531 W KR 2013011531W WO 2014092482 A1 WO2014092482 A1 WO 2014092482A1
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- catalyst
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- lanthanum
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/755—Nickel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
- B01J21/04—Alumina
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0027—Powdering
- B01J37/0036—Grinding
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1052—Nickel or cobalt catalysts
- C01B2203/1058—Nickel catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1082—Composition of support materials
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a catalyst for syngas production from natural gas using carbon dioxide, in particular a lanthanum-containing catalyst useful for syngas production by steam-carbon dioxide reforming (SCR) and a process for producing the same.
- SCR steam-carbon dioxide reforming
- the reforming process for producing a mixture of hydrogen and carbon monoxide, so-called syngas, from methane, which is the main component of natural gas, using a catalyst and an oxidant has been industrialized a long time ago and has become an important basic process of the chemical industry.
- Synthetic gas produced by the methane reforming process is the basis of C1 chemistry and is applied to the process of producing methanol, hydrogen, ammonia, etc. Recently, the production of liquid fuels and oxygen-containing compounds through the synthesis gas production It is emerging as an important method of using natural gas.
- Oxygen, water vapor, carbon dioxide, or a mixed gas thereof has been used as an oxidant for preparing synthesis gas from hydrocarbons, and many studies have been conducted to develop catalysts having different characteristics according to the type of oxidant.
- Reforming methods for producing syngas from methane include steam reforming, carbon dioxide reforming, partial oxidation reforming, autothermal reforming, and triple reforming.
- the steam reforming reaction proceeds according to the following Scheme 1, and mainly a nickel-based catalyst is used.
- Some supported zirconia supported catalysts are known as steam reforming catalysts. That is, a zirconia-supported nickel catalyst in which cobalt is added to nickel has been disclosed as a steam reforming catalyst for hydrocarbons (US Pat. No. 4,026,823 (1975)). In another method, a titration of a metal such as lanthanum, cerium, and silver to a nickel catalyst A catalyst in which the ratio is added as a cocatalyst supported on common carriers such as alumina, silica, magnesia, zirconia and the like has been disclosed (US Pat. No. 4,060,498).
- Korean Patent Registration No. 10-0394076 Ni-based reforming catalyst for syngas production and a method for producing syngas from natural gas by steam reforming using the same
- the nickel-based reforming catalyst (Ni / Ce-Zr 2 ) for syngas production is characterized in that 5 to 20% by weight of nickel is supported on a zirconia carrier modified with cerium.
- the catalyst was prepared by preparing a zirconia carrier or a zirconia carrier modified with cerium using a co-precipitation method or a sol-gel method and then supporting nickel by an impregnation method or a melting method.
- the present invention provides a nickel-based reforming catalyst for syngas production which can produce syngas or hydrogen with high yield while maintaining long life by preventing catalyst deactivation due to coke formation because of excellent activity and stability of the steam-carbon dioxide reforming reaction catalyst. I would like to.
- the present invention provides a method for producing a synthesis gas by steam-carbon dioxide reforming reaction using the catalyst.
- the catalyst according to the present invention is effective in minimizing carbon deposition and producing synthetic petrochemical products (wax, naphtha, diesel, etc.) in preparing syngas by steam-carbon dioxide reforming reaction (SCR) of methane (2.0). Syngas having a ⁇ 0.2) can be produced, thereby reducing the production cost of the synthetic material.
- the catalyst and the process using the same according to the present invention can be applied to gas to liquid (GTL) floating production, storage and offloading (FPSO), and moreover, DME FPSO to facilitate various industrial applications in the future. You can expect that.
- GTL gas to liquid
- FPSO floating production, storage and offloading
- FIG. 1 is a graph showing the molar ratio of hydrogen and carbon monoxide in the components of the synthesis gas prepared according to the conditions of Examples 1 and 6 of the present invention.
- Figure 2 is a graph showing the conversion rate of methane produced from natural gas during the synthesis gas manufacturing process according to Examples 1 and 6 conditions of the present invention.
- the present invention relates to a nickel-based reforming catalyst prepared using nickel and lanthanum series which are relatively excellent in carbon deposition in a reforming catalyst by steam.
- the reforming catalyst (NiO-La / Ce-ZrO 2 / Al 2 O 3 ) may be contained in the lanthanum and cerium-modified zirconia / alumina carrier 1 to 7% by weight of lanthanum.
- the firing of step 2) can be carried out in air at a temperature of 700 ⁇ 1200 °C.
- step 2) may be carried out by a dry ball mill or a wet mixing and then drying to extrude and extrude.
- the reforming catalyst NiO-La / Ce-ZrO 2 / Al 2 O 3
- the reforming catalyst is supported by 5 to 20% by weight of nickel in the lanthanum and cerium-modified zirconia / alumina support. If the supported amount is out of the above range, it may be difficult to produce a synthesis gas in which the hydrogen / carbon monoxide ratio is close to two.
- the reforming catalyst may be a weight ratio of lanthanum and cerium 1: 2 to 10. Outside the above range, it may be difficult to produce a synthesis gas having a hydrogen / carbon monoxide ratio close to two.
- the present invention is also characterized in that the reforming reaction is carried out by supplying carbon dioxide, water vapor and methane under the conditions of reaction temperature 700 ⁇ 950 °C, reaction pressure 10 ⁇ 20 bar, space velocity 3000 ⁇ 4000 h -1 using the catalyst It provides a method for producing a synthesis gas. It is preferable to supply at 0.4 mol mol of carbon dioxide and 1-3 mol mol of water with respect to 1 mol of methane. Since the molar ratio of hydrogen / carbon monoxide of the synthesis gas produced through the reforming reaction is 2.0 ⁇ 0.2, it is possible to easily provide an efficient synthesis gas for producing synthetic petrochemical products (wax, naphtha, diesel, etc.).
- a nickel reforming catalyst is prepared by supporting nickel metal on a zirconia / alumina carrier modified with lanthanum and cerium to prepare a nickel reforming catalyst. Synthesis gas, which is a mixture of carbon monoxide and hydrogen, can be produced in high yield.
- the nickel reforming catalyst used in the steam-carbon dioxide reforming reaction of methane natural gas according to the present invention is a reforming catalyst (NiO-La / Ce-ZrO 2 / Al 2 O 3 ). If the supported amount of nickel is out of the above range and less than 5% by weight, there is a problem of low activity. If the amount of nickel exceeds 20% by weight, deactivation of the catalyst due to the deposition of coke is undesirable.
- the zirconia / alumina carrier modified lanthanum and cerium used as a carrier is a mixture of zirconia / alumina, lanthanum and cerium, and the weight ratio of lanthanum (La) and cerium (Ce) is contained in the range of 1: 2 to 10.
- the content of, lanthanum and cerium is modified in excess in excess of the above range, there is a problem in that the activity of the catalyst is lowered.
- a method of modifying lanthanum and cerium on a zirconia-based / alumina carrier or a method of supporting nickel may be a method of drying, kneading, extruding, and baking after dry or wet mixing. It is preferable to use distilled water as a solvent.
- a zirconia / alumina carrier modified with lanthanum and cerium can be obtained by mixing lanthanum oxide (La 2 O 3 ), ceria, zirconia, nickel oxide, and alumina in a desired ratio.
- the powder form of nickel oxide is mixed with a zirconia / alumina carrier modified with lanthanum and cerium, followed by kneading and baking after extrusion. It is preferable to perform baking for 5 to 8 hours in air at the temperature of 700-1200 degreeC.
- the catalyst when measuring the reforming activity of the catalyst, a typical fixed bed catalyst reactor manufactured in a laboratory is used.
- the catalyst is molded and pulverized to have a particle size of 1 to 2 mm as a pretreatment process before the reaction, and then charged in a reactor by a required amount, and then reduced with 5% hydrogen at 700 ° C. for 1 hour before use.
- methane and water vapor are injected into the reactor as a reactant in a molar ratio of 1: 1 to 3 and carbon dioxide of 0.4 to 1, and nitrogen is added as a diluent gas if necessary.
- the temperature of the reactor is controlled in the range of 700 ⁇ 950 °C by the electric heater and the programmable thermostat, the reaction pressure is 10 ⁇ 20 atm, the mass velocity so that the conditions of 3000 ⁇ 4000 hr -1 Synthetic gas may be prepared by continuously injecting a gas while controlling a flow rate of the gas with a mass flow controller.
- the composition of the gas before and after the reaction is analyzed by gas chromatograph directly connected to the reactor, whereby a poropak column is used for separation of the gas.
- the activity was measured at 750 ° C. over time, and the initial activity and the activity after 200 minutes were determined by the yield of hydrogen in the product and the conversion rate of methane. Measured through.
- the method for producing syngas from natural gas using the reforming catalyst according to the present invention shows better activity than the activity of the conventional zirconia-supported nickel reforming catalyst, and also improves the activity of the catalyst to maintain high activity even at high gas space velocity. This suggests the possibility of using it as an industrial catalyst.
- Alumina, ceria, zirconia, nickel oxide, and lanthanum oxide are mixed in the form of powder in the ratio as shown in Table 1, distilled water is added, stirred by using a stirrer, mixed well, and dried. After sufficient mixing, the temperature was raised to 700 to 950 ° C at a rate of 3 ° C / min and calcined for 6 hours to obtain a catalyst.
- Ceria and zirconia are added to alumina in the form of a dry powder and mixed by ball milling.
- the two powders are mixed and calcined at 700 to 950 ° C. for 6 hours to obtain NiO-La / Ce-ZrO 2 / Al 2 O 3 .
- Example Methane Carbon Dioxide: Water Vapor CH 4 conversion (%) H 2 / CO
- Example 1 1: 1-3 95.93 2.32
- Example 2 1: 1: 1 to 2.5 94.69 2.11
- Example 3 1: 1: 1 to 2 93.41 1.92
- Example 4 1: 0.5 to 1: 1 to 2 93.31 2.08
- Example 5 1: 0.4-1: 1-2 93.70 2.05
- Example Methane Carbon Dioxide: Water Vapor CH 4 conversion (%) H 2 / CO
- Example 6 1: 1: 1-3 97.07 2.11
- Example 7 1: 1: 1 to 2.5 95.66 1.95
- Example 8 1: 1: 1 to 2 95.50 1.91
- Example 9 1: 0.5 to 1: 1 to 2 95.32 1.96
- Example 10 1: 0.4-1: 1-2 95.57 2.02
- the catalyst of the example is much larger than that of the comparative example. This means that the reactor size can be minimized so that the same CH 4 conversion can be achieved with the capacity of 1/3 to 1/5 in the design of the commercialization reactor, that is, the economic efficiency is high.
- the CO 2 content in the reaction gas can be increased by more than two times compared to the comparative example. Therefore, it is advantageous to use a gas having a high CO 2 content in the reaction gas, and in addition, it is possible to recover a large amount of CO 2 generated after the reaction, there is an advantage that the CO 2 treatment capacity is higher than other processes.
- the catalyst according to the present invention is effective in minimizing carbon deposition and producing synthetic petrochemical products (wax, naphtha, diesel, etc.) in preparing syngas by steam-carbon dioxide reforming reaction (SCR) of methane (2.0). Syngas having a ⁇ 0.2) can be produced, thereby reducing the production cost of the synthetic material.
- the catalyst and the process using the same according to the present invention can be applied to gas to liquid (GTL) floating production, storage and offloading (FPSO), and moreover, DME FPSO to facilitate various industrial applications in the future. You can expect that.
- GTL gas to liquid
- FPSO floating production, storage and offloading
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- Organic Chemistry (AREA)
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Abstract
Description
분석항목 | 재조예 1(wt%) | 제조예 2 (wt%) |
La2O3 | 1~8 | 1~13 |
CeO2 | 1~13 | 1~10 |
NiO | 3~12 | 5~14 |
ZrO2 | 2~10 | 2~11 |
Al2O3 | 70~90 | 70~90 |
제조방법 | 강도 | 벌크밀도 | |
L축(N) | R축(N) | ||
제조예 1 | 6125.0 | 114.7 | 1.531 |
제조예 2 | 6066.2 | 419.0 | 1.707 |
실시예 | 메탄 : 이산화탄소 : 수증기 | CH4 전환율 (%) | H2/CO |
실시예 1 | 1 : 1 : 1 ~ 3 | 95.93 | 2.32 |
실시예 2 | 1 : 1 : 1 ~ 2.5 | 94.69 | 2.11 |
실시예 3 | 1: 1: 1 ~ 2 | 93.41 | 1.92 |
실시예 4 | 1 : 0.5 ~ 1 : 1 ~ 2 | 93.31 | 2.08 |
실시예 5 | 1 : 0.4 ~ 1 : 1 ~ 2 | 93.70 | 2.05 |
실시예 | 메탄 : 이산화탄소 : 수증기 | CH4 전환율 (%) | H2/CO |
실시예 6 | 1 : 1 : 1 ~ 3 | 97.07 | 2.11 |
실시예 7 | 1 : 1 : 1 ~ 2.5 | 95.66 | 1.95 |
실시예 8 | 1: 1: 1 ~ 2 | 95.50 | 1.91 |
실시예 9 | 1 : 0.5 ~ 1 : 1 ~ 2 | 95.32 | 1.96 |
실시예 10 | 1 : 0.4 ~ 1 : 1 ~ 2 | 95.57 | 2.02 |
반응몰비 (CH4/STM/CO2) | 공간속도 (hr-1) | CH4 conv. |
1/1.5/0.4 | 1300 | 95 |
1/1.5/0.39 | 1700 | 93 |
1/1.5/0.34 | 1700 | 97 |
Claims (10)
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CN201380071806.3A CN104955564A (zh) | 2012-12-12 | 2013-12-12 | 用于通过水蒸气-二氧化碳重整制造合成气的含镧催化剂及使用其制造合成气的方法 |
AU2013360537A AU2013360537B2 (en) | 2012-12-12 | 2013-12-12 | Catalyst containing lanthanum for manufacturing synthetic gas through steam-carbon dioxide reforming, and method for manufacturing synthetic gas by using same |
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KR1020120144030A KR101401170B1 (ko) | 2012-12-12 | 2012-12-12 | 수증기-이산화탄소 개질에 의한 합성가스 제조용 란탄함유 촉매 및 이를 이용한 합성가스 제조방법 |
KR10-2012-0144030 | 2012-12-12 |
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KR101761829B1 (ko) * | 2015-05-07 | 2017-07-26 | 성균관대학교산학협력단 | 합성가스 및 일산화탄소의 제조 방법 |
KR101825495B1 (ko) * | 2015-11-24 | 2018-02-05 | 한국화학연구원 | 저온 개질반응용 코발트 담지촉매 및 이의 제조방법 |
CN105413734B (zh) * | 2015-12-07 | 2020-05-26 | 西南化工研究设计院有限公司 | 一种用于甲烷-二氧化碳重整制还原气的镍系催化剂及其制备方法 |
KR102488300B1 (ko) * | 2017-04-12 | 2023-01-13 | (주)바이오프랜즈 | 매립지 가스를 이용한 전력 및 화학원료 병산 시스템 |
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KR20080043161A (ko) * | 2006-11-13 | 2008-05-16 | 고려대학교 산학협력단 | 액화천연가스의 수증기 개질반응에 의한 수소가스 제조용담지 촉매, 그 제조방법 및 상기 담지 촉매를 이용한수소가스 제조방법 |
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JP3761947B2 (ja) * | 1995-11-08 | 2006-03-29 | 石油資源開発株式会社 | 合成ガス製造用触媒組成物およびこれを用いて合成ガスを製造する方法 |
CN101637726A (zh) * | 2008-07-31 | 2010-02-03 | 中国石油天然气股份有限公司 | 一种甲烷-二氧化碳重整制备合成气催化剂的制备方法 |
CN101352687B (zh) * | 2008-08-29 | 2011-09-14 | 同济大学 | 可用于甲烷二氧化碳干重整的催化剂、其制备方法与应用 |
KR101068995B1 (ko) * | 2008-12-08 | 2011-09-30 | 현대중공업 주식회사 | 메탄, 수증기 및 이산화탄소를 혼합 개질반응하여 생성된 합성가스를 이용한 메탄올의 합성방법 |
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2012
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KR20080043161A (ko) * | 2006-11-13 | 2008-05-16 | 고려대학교 산학협력단 | 액화천연가스의 수증기 개질반응에 의한 수소가스 제조용담지 촉매, 그 제조방법 및 상기 담지 촉매를 이용한수소가스 제조방법 |
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AU2013360537A1 (en) | 2015-07-16 |
MY169114A (en) | 2019-02-18 |
KR101401170B1 (ko) | 2014-05-29 |
AU2013360537B2 (en) | 2016-05-12 |
CN104955564A (zh) | 2015-09-30 |
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