CN101829571A - Method for preparing Cu/SiO2 catalyst - Google Patents
Method for preparing Cu/SiO2 catalyst Download PDFInfo
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- CN101829571A CN101829571A CN 201010198781 CN201010198781A CN101829571A CN 101829571 A CN101829571 A CN 101829571A CN 201010198781 CN201010198781 CN 201010198781 CN 201010198781 A CN201010198781 A CN 201010198781A CN 101829571 A CN101829571 A CN 101829571A
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Abstract
The invention relates to a catalyst, in particular to a method for preparing a Cu/SiO2 catalyst. The prepared Cu/SiO2 catalyst has the advantages of higher specific area, Cu loading capacity, dispersibility, stability and the like. The preparation method comprises the following steps of: preparing an ethyl silicate solution containing a surface active agent; preparing an inorganic acid solution; adding the prepared ethyl silicate solution containing a surface active agent to a reaction kettle, simultaneously adding the prepared inorganic acid solution to the reaction kettle, stirring, and aging at constant temperature to obtain a mixed solution; dissolving the obtained mixed solution in absolute ethyl alcohol, stirring, adding catalyst and ethanol, and stirring again to obtain a mixed liquid; adding a copper salt solution containing Cu of 2-5% in calculated amount to the obtained mixed liquid, adding ammonia water to adjust the pH value, stirring, aging at room temperature, carrying out water bath at constant temperature, drying, calcining, grinding, and sieving to obtain the Cu/SiO2 catalyst.
Description
Technical field
The present invention relates to a kind of catalyst, especially relate to a kind of carbon monoxide-olefin polymeric that is applicable to that olefinic polymerization is required, with SiO
2Be carrier, Cu is the preparation method of the loaded catalyst of active component.
Background technology
The chemical composition of silica gel is SiO
2, there is one deck physical absorption water on the silica gel surface under the room temperature, has silanol [SiOH] structure on the surface simultaneously, and when 423～473K, the water of most of absorption is mainly stayed [SiOH] by desorption on the surface.Under higher temperature, adjacent [OH] dehydration forms [Si-O-Si] structure.Silica gel has special pore structure, bigger serface and good heat endurance, is widely used as adsorbent, drier, thickener, chromatographic column carrier and catalyst carrier etc.
Silica gel has crucial status as the carrier of the required catalyst of olefinic polymerization in catalytic component, parameters such as its form, particle diameter and distribution thereof, specific surface, pore-size distribution can produce great influence to the form and the performance of polymer.Early 1980s, China has begun to be applicable to the production domesticization research of polyolefin catalyst silica-gel carrier, but the catalyst system therefor silica-gel carrier still relies on import mostly in the present polyolefin industry.Therefore, abroad the monopolization to market has important practical application meaning to the new polyolefin catalyst silica-gel carrier of exploitation in catalyst carrier silica gel field for a long time to breaking.
The preparation method that catalyst is commonly used mainly contains infusion process, the precipitation method, sol-gel process, ion-exchange etc.Sol-gel process is meant that metal organic or inorganic compound solidifies through solution, colloidal sol and gel, forms the method for oxide or other compound solids again through Overheating Treatment.Colloidal sol is the system of having disperseed 1～100nm particle (elementary cell) in the medium, gel is to contain sub-micron pore and the interconnective solid network of polymeric chain, and gel structure can be divided into the network of ordered lamellar structure, unordered copolymerization network, unordered control polymerization and particle disordered structure etc.Sol-gal process has lot of advantages: reaction temperature is low, and course of reaction is easy to control; The uniformity of goods and purity height (uniformity can reach molecule or atomic level); Stoichiometry is accurate, is easy to modification, the wide ranges of doping (amount and the kind that comprise doping); From with a kind of raw material, change technical process and can obtain different products; Technology is simple, does not need expensive equipment.
Olefinic polymerization occupies bigger proportion in petrochemical industry, and polyolefin catalyst carrier produces tremendous influence as an important component part of olefinic polymerization industry to polyolefinic development.After the eighties in 20th century, applied for many patents about the research of polyolefin catalyst silica-gel carrier both at home and abroad, and the report of many correlation theory researchs aspect has been arranged.Yao Peihong etc. disclose a kind of preparation method of silica-gel carrier in Chinese patent CN1403486, when preparation silicon gel, dilute silicate and inorganic acid added simultaneously promptly that to be equipped with part dilute silicate solution be in the reactor of mother liquor, when treating that colloidal sol and partial gel occur, mother liquor pH value to 5～8.5 in the conditioned reaction still, after treating that the hydrosol all is converted into the silicon gel, obtaining specific area through aging, washing, processing and drying is 200～400m
2/ g, pore-size distribution are 8～15nm, and bulk density is 0.2～0.4g/ml, and pore volume is the silica-gel carrier of 1.0～1.2ml/g.The polyolefin catalyst that uses on the polyolefin industry requires the pore volume 1.00～2.00ml/g of silica-gel carrier, and specific area is 280～555m
2/ g, pore-size distribution are 9～18nm.
Cu is widely used in catalytic combustion, the NO of oxidation, hydrogenation and hydrocarbon owing to having good catalytic oxidation and catalytic reduction performance
xFields such as Chemical Engineerings such as catalytic reduction, environmental protection and fuel cell.Cu-series catalyst is widely used it with advantages such as activity are high, cheap and easy to get in catalytic field.Cu/SiO
2Catalyst is paid close attention to deeply owing to have hydrogenation selectivity and non-environmental-pollution problem preferably.Abroad to Cu/SiO
2The research starting of catalyst early studies in great detail to 80～nineties of 20th century.Domestic to Cu/SiO
2The research of catalyst was risen the nineties in 20th century, Li Zhuxia etc. (Li Zhuxia, Qian Zhigang, Zhao Xiuge, etc. carrier is to the influence [J] of dimethyl oxalate hydrogenation copper-based catalysts. East China University of Science's journal, 2005,31 (1): 27-31; Li Zhuxia. the research [D] of dimethyl oxalate catalytic hydrogenation synthesizing glycol process. Shanghai: East China University of Science, 2004.) study various oxide carriers (γ one Al
2O
3, SiO
2, TiO
2And ZrO
2) time finds Cu/SiO
2Activity is best, and has studied the influence (Ni, Zn and Ca) of auxiliary agent.Huang Weijie etc. (Huang Weijie, Wen Feng, Kang Wenguo, etc. preparing ethylene glycol by using dimethyl oxalate plus hydrogen Cu/SiO
2Preparation of catalysts and modification [J]. Industrial Catalysis, 2008,16 (6): 13-17.) and Wen Feng etc. (Wen Feng, Huang Weijie, Xiao Wende. dimethyl oxalate hydrogenation catalyst Cu/SiO
2Preparation research [J]. the Guangdong chemical industry, 2008,35 (4): 5-11) studied respectively ammonia still process method and urea the precipitation sedimentation prepare Cu/SiO
2The influence of each preparation factor of catalyst.
Present studies show that Cu/SiO
2Catalyst has purposes widely as selective hydrocatalyst, and the preparation method also has multiple, but certain limitation is all arranged, and such as the carrier impregnation method the inhomogeneous reunion of active component at the fine grained edge of carrier takes place easily; Though ion-exchange is the dispersed activity component preferably, activity component load quantity is very low; The Cu/SiO of precipitation sedimentation preparation
2Catalysts Cu content is lower, and the content that improves copper can cause surperficial copper grain growth, easy-sintering.
Summary of the invention
The purpose of this invention is to provide a kind of preparation Cu/SiO
2The method of catalyst, prepared Cu/SiO
2Catalyst has advantages such as higher specific surface area, Cu load capacity, dispersiveness and stability.
Technical scheme of the present invention is to adopt nucleus growth technology and effectively control the particle diameter control method, by sol-gel process with catalyst effectively spread loads in Ludox, thereby obtain a kind of Cu/SiO with advantages such as higher specific surface area, Cu load capacity, dispersiveness and stability
2Catalyst.
The present invention includes following steps:
1) preparation contains the ethyl silicate solution of surfactant;
2) preparation inorganic acid solution;
3) ethyl silicate solution that contains surfactant that step 1) is prepared is added in the reactor, adds simultaneously step 2 in reactor) inorganic acid solution for preparing, stir, constant temperature is aging, mixed solution;
4) mixed solution with the step 3) gained dissolves in absolute ethyl alcohol, stirs, and adds catalyst, ethanol again, stirs again, gets mixed liquor;
5) copper salt solution that will contain 2%～5%Cu amount of calculation adds in the mixed liquor of step 4) gained, regulates pH value with ammoniacal liquor again, stir, and aged at room temperature, water bath with thermostatic control dry roasting again, grinding is sieved, must Cu/SiO
2Catalyst.
In step 1), described surfactant can be selected from neopelex etc., and the concentration of described neopelex can be 0.01～0.02mol/L; The concentration of described ethyl silicate solution can be 0.5～1.0mol/L.
In step 2) in, the concentration of described inorganic acid solution can be 0.5～1.0mol/L; Described inorganic acid can be selected from a kind of in hydrochloric acid, sulfuric acid and the nitric acid etc.
In step 3), the flow velocity that the described ethyl silicate solution that contains surfactant that step 1) is prepared is added in the reactor can be 2～5ml/min; The described step 2 that in reactor, adds) inorganic acid solution for preparing, the pH value that preferably makes solution in the reactor is 8.5～10; The speed of described stirring can be 2000～3000r/min; The temperature that described constant temperature is aging can be 65～85 ℃, and the time that constant temperature is aging can be 1～2h.
In step 4), described mixed solution with the step 3) gained dissolves in absolute ethyl alcohol, and by volume, mixed solution: absolute ethyl alcohol can be 11: (18～20); Described catalyst, ethanol, by volume, catalyst: ethanol can be 1: (2.5～10), the volume ratio of alcohol to water of described ethanol can be 7: 11; Described catalyst can be selected from HNO
3Or NH
4OH etc.
In step 5), the concentration of described ammoniacal liquor can be 2mol/L, and the temperature of described roasting can be 400 ℃, and the time of roasting can be 4h; Described mantoquita can be selected from Cu (NO
3)
2, CuCl
2, Cu (CH
3COO)
2Deng in a kind of, be preferably Cu (NO
3)
2Described again with ammoniacal liquor adjusting pH value, preferably the pH value is 6～8; The temperature of described water bath with thermostatic control can be 60～70 ℃, and the temperature of described roasting can be 400 ℃.
Because the present invention adopts nucleus growth technology and effectively controls the particle diameter control method, by sol-gel process with catalyst evenly effectively spread loads in Ludox, therefore the present invention has following outstanding advantage: technical process is simple, process conditions are easy to control, the specific area height of gained catalyst, copper load capacity height, dispersiveness and excellent in stability are a kind of very promising polyolefin catalyst.Through test, its catalytic efficiency of the catalyst that the present invention makes is convenient to Industry Promotion than the obvious height of typical catalyst.
The specific embodiment
Embodiment 1
1) add the 200ml deionized water in the reactor that thermometer, pH meter and agitator are installed, start agitator speed 3000r/min, making temperature of reaction kettle is 80 ℃.
2) compound concentration is the 1.0mol/L ethyl silicate solution, adds neopelex again in this solution, and making neopelex concentration is 0.01mol/L.Compound concentration is the salpeter solution of 0.5mol/L.
3) flow velocity with 3ml/min adds ethyl silicate solution in the reactor, drips salpeter solution simultaneously, and making the pH value of solution in the reactor is 8.5, keeps constant agitation speed and steady temperature in reaction, after dripping, and the aging 1～2h of constant temperature under agitation.
4) get 11ml step 3) gained solution and dissolve in the 18.5ml absolute ethyl alcohol, stir.HNO with 1ml
3, 8ml ethanol mixes and to pour in the mixture, stir.
5) will contain the Cu (NO of 2%Cu amount of calculation
3)
2Solution 50ml slowly splashes in the step 4) gained mixed liquor, again with concentration be the ammoniacal liquor of 2mol/L to regulate pH value be 7, the powerful 1h that stirs, aged at room temperature 12h is at 60 ℃ of waters bath with thermostatic control drying 20h, 110 ℃ of oven drying 15h, 400 ℃ of roasting 4h.Grind, sieve, standby.
6) with step 5) gained catalyst sample preliminary treatment 3h under 300 ℃ of vacuum conditions, make adsorbate, under liquid nitrogen temperature, use the BET method to measure with high purity nitrogen.Recording specific surface area of catalyst is 716.5m
2/ g, pore volume are 0.696cc/g.
7) step 5) gained catalyst sample 0.2mol is mixed with the quartz sand of equal particle diameter and volume be placed on pump type reactor middle part, the inlet amount of controlling diethy-aceto oxalate solution is 0.01ml/min, after the preheater preheating is gaseous state, mixes with hydrogen and to react.Reaction temperature 220-250 ℃, pressure 0.5～4MPa, hydrogen/ester mol ratio 170～290. liquid products are analyzed with the 3700 type gas chromatographs that U.S. Varian company produces, adopt the correction factor method to calculate the percentage composition of each material, the diethy-aceto oxalate conversion ratio be 94.5% and the ethylene glycol yield be 81%.
Embodiment 2
Preparation process is with embodiment 1.Temperature of reaction kettle is 80 ℃, and ethyl silicate solution concentration is 1.0mol/L, and neopelex concentration is 0.01mol/L, and flow velocity is 3ml/min in the ethyl silicate solution adding reactor, and the pH value of solution is 8.5 in the reactor, Cu (NO
3)
2The Cu amount of calculation is 2% in the solution, and it is 7.2 that ammoniacal liquor is regulated the pH value, and the water bath with thermostatic control temperature is 65 ℃, and specific surface area of catalyst is 715.5m
2/ g, pore volume are 0.689cc/g, and the gained catalyst is used for the reaction of diethy-aceto oxalate hydrogenation preparing ethylene glycol, the diethy-aceto oxalate conversion ratio be 93.8% and the ethylene glycol yield be 79.8%.
Embodiment 3
Preparation process is with embodiment 1.Temperature of reaction kettle is 85 ℃, and ethyl silicate solution concentration is 0.5mol/L, and neopelex concentration is 0.01mol/L, and flow velocity is 3ml/min in the ethyl silicate solution adding reactor, and the pH value of solution is 9.0 in the reactor, Cu (NO
3)
2The Cu amount of calculation is 2% in the solution, and it is 7.5 that ammoniacal liquor is regulated the pH value, and the water bath with thermostatic control temperature is 65 ℃, and specific surface area of catalyst is 714.9m
2/ g, pore volume are 0.690cc/g, and the gained catalyst is used for the reaction of diethy-aceto oxalate hydrogenation preparing ethylene glycol, the diethy-aceto oxalate conversion ratio be 93.5% and the ethylene glycol yield be 80%.
Embodiment 4
Preparation process is with embodiment 1.Temperature of reaction kettle is 80 ℃, and ethyl silicate solution concentration is 1.0mol/L, and neopelex concentration is 0.02mol/L, and flow velocity is 4ml/min in the ethyl silicate solution adding reactor, and the pH value of solution is 9.0 in the reactor, Cu (NO
3)
2The Cu amount of calculation is 3% in the solution, and it is 7.5 that ammoniacal liquor is regulated the pH value, and the water bath with thermostatic control temperature is 60 ℃, and specific surface area of catalyst is 717.1m
2/ g, pore volume are 0.693cc/g, and the gained catalyst is used for the reaction of diethy-aceto oxalate hydrogenation preparing ethylene glycol, the diethy-aceto oxalate conversion ratio be 95.3% and the ethylene glycol yield be 83%.
Embodiment 5
Preparation process is with embodiment 1.Temperature of reaction kettle is 85 ℃, and ethyl silicate solution concentration is 1.0mol/L, and neopelex concentration is 0.01mol/L, and flow velocity is 3ml/min in the ethyl silicate solution adding reactor, and the pH value of solution is 9.0 in the reactor, Cu (NO
3)
2The Cu amount of calculation is 3% in the solution, and it is 7 that ammoniacal liquor is regulated the pH value, and the water bath with thermostatic control temperature is 70 ℃, and specific surface area of catalyst is 716.8m
2/ g, pore volume are 0.701cc/g, and the gained catalyst is used for the reaction of diethy-aceto oxalate hydrogenation preparing ethylene glycol, the diethy-aceto oxalate conversion ratio be 94.7% and the ethylene glycol yield be 81.6%.
Embodiment 6
Preparation process is with embodiment 1.Temperature of reaction kettle is 80 ℃, and ethyl silicate solution concentration is 0.5mol/L, and neopelex concentration is 0.02mol/L, and flow velocity is 4ml/min in the ethyl silicate solution adding reactor, and the pH value of solution is 8.5 in the reactor, Cu (NO
3)
2The Cu amount of calculation is 2% in the solution, and it is 7.2 that ammoniacal liquor is regulated the pH value, and the water bath with thermostatic control temperature is 70 ℃, and specific surface area of catalyst is 715.9m
2/ g, pore volume are 0.688cc/g, and the gained catalyst is used for the reaction of diethy-aceto oxalate hydrogenation preparing ethylene glycol, the diethy-aceto oxalate conversion ratio be 94.1% and the ethylene glycol yield be 80.5%.
Claims (10)
1. one kind prepares Cu/SiO
2The method of catalyst is characterized in that may further comprise the steps:
1) preparation contains the ethyl silicate solution of surfactant;
2) preparation inorganic acid solution;
3) ethyl silicate solution that contains surfactant that step 1) is prepared is added in the reactor, adds simultaneously step 2 in reactor) inorganic acid solution for preparing, stir, constant temperature is aging, mixed solution;
4) mixed solution with the step 3) gained dissolves in absolute ethyl alcohol, stirs, and adds catalyst, ethanol again, stirs again, gets mixed liquor;
5) copper salt solution that will contain 2%～5%Cu amount of calculation adds in the mixed liquor of step 4) gained, regulates pH value with ammoniacal liquor again, stir, and aged at room temperature, water bath with thermostatic control dry roasting again, grinding is sieved, must Cu/SiO
2Catalyst.
2. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 1) described surfactant is selected from neopelex; The concentration of described neopelex is 0.01～0.02mol/L; The concentration of described ethyl silicate solution is 0.5～1.0mol/L.
3. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 2) in, the concentration of described inorganic acid solution is 0.5～1.0mol/L; Described inorganic acid is selected from a kind of in hydrochloric acid, sulfuric acid and the nitric acid.
4. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 3), and the flow velocity that the described ethyl silicate solution that contains surfactant that step 1) is prepared is added in the reactor is 2～5ml/min.
5. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 3), the described step 2 that adds in reactor) inorganic acid solution for preparing is that to make the pH value of solution in the reactor be 8.5～10.
6. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 3), and the speed of described stirring is 2000～3000r/min; The temperature that described constant temperature is aging is 65～85 ℃, and the time that constant temperature is aging is 1～2h.
7. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 4), and described mixed solution with the step 3) gained dissolves in absolute ethyl alcohol, and by volume, mixed solution: absolute ethyl alcohol is 11: 18～20.
8. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 4), described catalyst, ethanol, and by volume, catalyst: ethanol is 1: 2.5～10, the volume ratio of alcohol to water of described ethanol is 7: 11; Described catalyst is selected from HNO
3Or NH
4OH.
9. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 5), and the concentration of described ammoniacal liquor is 2mol/L, and the temperature of described roasting is 400 ℃, and the time of roasting is 4h.
10. a kind of preparation Cu/SiO as claimed in claim 1
2The method of catalyst is characterized in that in step 5) described mantoquita is selected from Cu (NO
3)
2, CuCl
2, Cu (CH
3COO)
2In a kind of, be preferably Cu (NO
3)
2Described again with ammoniacal liquor adjusting pH value, be that the pH value is 6～8; The temperature of described water bath with thermostatic control is 60～70 ℃.
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|---|---|---|---|
| CN 201010198781 CN101829571A (en) | 2010-06-08 | 2010-06-08 | Method for preparing Cu/SiO2 catalyst |
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|---|---|---|---|
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102716744A (en) * | 2012-06-18 | 2012-10-10 | 河南煤业化工集团研究院有限责任公司 | Preparation method for synthesizing copper-based catalyst by sol-gel ammonia still process |
| CN108393076A (en) * | 2018-03-20 | 2018-08-14 | 扬州大学 | Containing copper adsorbent, preparation method and its in adsorbing water tetracycline application |
| CN112830871A (en) * | 2019-11-22 | 2021-05-25 | 中国科学院大连化学物理研究所 | Method for preparing cyclopentanone by catalytic conversion of furan derivative |
| CN115212885A (en) * | 2022-05-24 | 2022-10-21 | 天津大学 | Cobalt silicate derived cobalt-based catalyst for directly preparing low-carbon alcohol from synthesis gas, preparation method and pretreatment method |
| CN117942998A (en) * | 2023-12-06 | 2024-04-30 | 江苏宏邦化工科技有限公司 | Cu/SiO2Preparation method of catalyst and application of catalyst in preparation of sandalwood 196 by catalytic hydrogenation |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1403486A (en) * | 2001-09-03 | 2003-03-19 | 中国石油天然气股份有限公司 | Preparation method of silica gel carrier |
| CN1803600A (en) * | 2005-12-16 | 2006-07-19 | 厦门大学 | Preparation method of silica gel carrier |
-
2010
- 2010-06-08 CN CN 201010198781 patent/CN101829571A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1403486A (en) * | 2001-09-03 | 2003-03-19 | 中国石油天然气股份有限公司 | Preparation method of silica gel carrier |
| CN1803600A (en) * | 2005-12-16 | 2006-07-19 | 厦门大学 | Preparation method of silica gel carrier |
Non-Patent Citations (1)
| Title |
|---|
| 《中国优秀硕士论文全文数据库（工程科技I辑）》 20090915 杨佳 溶胶凝胶法制备的Cu/SiO2催化剂在NO+CO反应中的活性研究 B014-238 1-10 , 第9期 2 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102716744A (en) * | 2012-06-18 | 2012-10-10 | 河南煤业化工集团研究院有限责任公司 | Preparation method for synthesizing copper-based catalyst by sol-gel ammonia still process |
| CN108393076A (en) * | 2018-03-20 | 2018-08-14 | 扬州大学 | Containing copper adsorbent, preparation method and its in adsorbing water tetracycline application |
| CN108393076B (en) * | 2018-03-20 | 2021-06-11 | 扬州大学 | Copper-containing adsorbent, preparation method and application thereof in adsorption of tetracycline in water |
| CN112830871A (en) * | 2019-11-22 | 2021-05-25 | 中国科学院大连化学物理研究所 | Method for preparing cyclopentanone by catalytic conversion of furan derivative |
| CN112830871B (en) * | 2019-11-22 | 2022-03-08 | 中国科学院大连化学物理研究所 | Method for preparing cyclopentanone by catalytic conversion of furan derivative |
| CN115212885A (en) * | 2022-05-24 | 2022-10-21 | 天津大学 | Cobalt silicate derived cobalt-based catalyst for directly preparing low-carbon alcohol from synthesis gas, preparation method and pretreatment method |
| CN115212885B (en) * | 2022-05-24 | 2023-08-01 | 天津大学 | Cobalt silicate derived cobalt-based catalyst for directly preparing low-carbon alcohol from synthesis gas, preparation method and pretreatment method |
| CN117942998A (en) * | 2023-12-06 | 2024-04-30 | 江苏宏邦化工科技有限公司 | Cu/SiO2Preparation method of catalyst and application of catalyst in preparation of sandalwood 196 by catalytic hydrogenation |
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Application publication date: 20100915 |