• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1492276 Ethers by dehydration of aliphatic alcohols SNAMPROGETTI SpA 13 Nov 1975 [21 Nov 1974] 46951/75 Heading C2C [Also in Division C1] An ether is produced by contacting an aliphatic alcohol at an elevated temperature with a catalyst comprising an active alumina modified by reaction with a silicon compound in such a manner that the surface region of the alumina has a layer of an oxygen compound of silicon deposited thereon. The silicon compound has for example the formula SiWXYZ where each of W, X, Y and Z, which can be the same or different is -R, -OR, -Cl, -Br, -SiH 3 , -COOR or -SiH n Cl m where R is a hydrogen atom or a hydrocarbon radical having up to 30 carbon atoms, m and n are integers of 1, 2 or 3 and m + n = 3. The silica may comprise 0À5- 20% by weight of the total catalyst. The contacting is preferably at 200-400‹ C. In examples, the catalyst was prepared by treating activated gamma alumina with tetraethyl orthosilicate, and was used for the dehydration of methanol to dimethyl ether at 300‹ C.
    公开号:SU841578A3
    申请号:SU752190954
    申请日:1975-11-20
    公开日:1981-06-23
    发明作者:Фатторе Витторио；Манара Джованни；Нотари Бруно
    申请人:Снампрогетти С.П.А. (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a process for the preparation of ethers, in particular dimethyl and diethyl ethers, which are widely used in chemical production as solvents and intermediates in chemical synthesis. A known method of obtaining ethers by the dehydration of alcohols at, nepafy pe 15 O-350 ° C, a pressure of 1-30 kg / cm (activated alumina is used as a catalyst) and a space velocity of 1-10. The process can also be carried out in the presence of aluminum on an inert carrier-kieselguhr 1. However, alumina during the hydrothermal dehydration process (due to sintering) undergoes rather rapid aging, which leads to a noticeable decrease in the conversion of alcohol to ether just after 200 hours of operation of the catalyst (Fig. 1). A known method of producing ethers in which the catalyst on support 2 is used. This disadvantage is inherent in the catalyst on the support as well, since the silicon derivative plays a role. an inert substrate serving only as a carrier of the active component of the catalyst. On the surface of such a catalyst, there is also the presence of OH-rpsTtn, which promotes sintering. The purpose of the invention is to improve the process technology. The goal is achieved by the method of obtaining ethers by dehydration; alcohols P temperature 280-350 ° C and a space velocity of 1 10 cm in the presence of a catalyst, which is alumina, the surface of which is modified with a layer of silicon dioxide in an amount of 8-18% by weight of the catalyst. The dehydration process is carried out in the presence of inert gases (NgjCO) in a solid or liquefied catalyst bed at atmospheric pressure. The catalyst used in this process (alumina) with silicon dioxide particles deposited on its surface is more durable, h & l conventional activated alumina, and ensures that the process has passed through for at least 500 hours without noticeably liquefying the conversion. Modifying the alumina surface with silica is achieved by treating the surface of the oxide with such compounds as (CaH50) 4Si; (CH-0), 51014: (C Hj-VSiCl; (CH3) (CrHH), (CH, 0) SiH, SiH5; H S i / COOCHj / As a result of this treatment, a surface layer of silicon dioxide is formed due to the reaction OFs of alumina and silicon containing / compounds. IR spectroscopic data shows that the spectral bands at 3795 and 3737 cm-corresponding to different RF groups on the surface of alumina disappear, while the band at 3745 cm is observed. characteristic of OH groups bound to oxide, for Si -OH. Example: The preparation of the catalyst is carried out as follows.
    Properties of aluminum oxide type A
    T a b l i
    C a
    Indicator 100 g of alumina, cn.) Whose properties are listed in tab. I, placed in an autoclave e autoheating) m together with 40 g () Si. Lavtoklav is pumped out and purged with nitrogen several times to remove all traces of oxygen, after which it is filled with nitrogen under a pressure of 5 kg / cm I g and the flare is heated to and kept at this temperature for 4 hours. At the end, the autoclave is cooled, the pressure is reduced and the extracted the alumina is subjected to further heat treatment in nitrogen for 2 hours at 200 ° C, and then calcined in air at 500 ° C for 4 hours. In the catalyst thus obtained, the silica content is. The specified catalyst is used in the dehydration reaction.
    Bulk specific weight-, g / cm
    Surface area, m / g

    Total pore volume, cm / g Example 2., C1.) Avnon catalytic properties of the proposed and known catalysts. One part of technical1-type aluminum oxide-type alumina in the form of wigs with a diameter of 3-4 mm, whose properties are indicated in Table. 1, is activated in a stream of nitrogen at 450 C and then used. in the dehydration process for comparison with the proposed catalyst. The second part is treated (as in example 1, so that the silica content of the alumina is 10.2%.
    Volumetric rate, g / g-h
    Conversion of methanol, mol.%
    0.51
    301
    0.88
    one
    The stationary tube reactor with a stationary layer is alternately filled with 1 g of alumina treated (C-H OhSi or 1 g of untreated alumina. The reactor is heated to nitrogen at a flow rate of 400 ml / hr at atmospheric pressure, and then treated with methanol, feeding at a rate of 1 g / g-h. Products leaving the reactor (nitrogen, dimethyl ether (DME), water) are analyzed with a PMC GLC, while there are no by-products. The results of the analysis are shown in Table 2. . Table 2
    It can be seen from the table data that the image (changes the catalytic properties of aluminum oxide type A in the absence of water vapor pressure
    Example 3. Comparison of resistance to aging of known and proposed catalysts.
    It is known that during dehydration of alcohols to ethers, an increase in the partial pressure of water vapor occurs, which gradually decreases with time the activity of alumina.
     Type A aluminum and Aluminum type A oxide + 10.2% silica
    Conversion, mol.%
    The decrease in catalyst activity is accompanied by sintering of alumina, whose surface area drops to 10 hours in 10 hours,
    On the contrary, alumina of type A, containing 10.2% silica, after treatment at 300 ° C and a water pressure of 15 atm, only slightly reduces the catalytic activity (after 46 hours, the conversion of methanol is stabilized by 75%).
    In addition, the surface area of the catalyst is reduced to a much lesser extent (after 46 hours it is 232).
    Thus, modifying the surface of alumina with dioxide allows preserving the dehydration properties of alumina, which remain unchanged even after a long stay in an atmosphere of water vapor I-.
    subjected to the process of rapid aging by treating them with steam at a temperature and pressure of water vapor of 15 atm.
    From time to time, water is removed and the catalyst is dried at and at atmospheric pressure in a stream of nitrogen at a rate of 400 ml / h, and then methanol is supplied.
    The catalytic activity of catalysts (known and proposed) in the aging process (Fig 2) at a temperature and pressure of water vapor of 15 atm is presented in Table. 3
    Table3
    77; 77 75
    23.5
    under alumina, under the same conditions, alumina, untreated with crettle compounds, quickly loses its activity.
    Example 4 Type A aluminum oxide and type A aluminum squeeze, containing 10.2% silica, are aged in a presence of water vapor under milder conditions, namely at a pressure of 5.5 atm and nitrogen at 2 atm. for 512 hours
    Samples of catalyst are periodically taken in order to trace changes in their catalytic activity.
    The catalytic activity of catalysts (known and proposed) at a water vapor pressure of 5.5 agm 1I and a nitrogen pressure of 2 atm is presented in the table below. four..
    Table 4
    Volumetric speed
    G / Hp h
    processing time, h
    Conversion of tins, mol.%
    The table shows that the decrease in the activity of the catalyst is slower than in example 2, when the vapor pressure is 15 atm, after 210 h the decline in activity is much more significant for aluminum oxide type A.
    However, with an increase in processing time of up to 5l2 h, alkali oxide type A still continues to decompose, while alumina containing
    Temperature, with Pressure, atm Vol. Speed, Processing time, h Conversion, mol.%
    Continued table. four
    36; 115; 210; 512
    36; 115; 210; 512
    79; 78; 78; 78
    .79; 79; 72 b1
    10.2% dioxide, does not change
     its activity.
    Example 5, One part of a technical y-oxide and aluminum type B, the properties of which are given in table. 5, used for dehydration, another
    20 parts are treated with () 431 of example 1, so that the content of krellny dioxide in the catalyst is 8.1%.
    280
    one
    0.8
    0; 5; 10; 3b; 52; 1b8
    75; 74; 73; 73; 72; 71. T a b litsa 5 ... in "" - T about. . Type B aluminum oxide properties. Indicator Bulk specific gravity, g / cm 0.95 Surface area, m / g 210 Total pore volume, cm / g 40 Processed and untreated nitrogen, then add {C EgQ Si. aluminum oxide is subjected to AQ tanol. aging in the presence of water pap, “at a pressure of 15 at.”. °. In table. 6 shows the catalyst. The water is periodically removed and the aging time at the pressure of the water lyser is dried at 280 ° C in a current of 45 vapors of 15 atm during the production of DU. Table Catalyst Aluminum oxide Type B aluminum alumina + 8.1% dioxide activity of two type B aluminum oxide samples depending on 1 belt The surface area of type B aluminum oxide after 168 hours at 280 ° C while dosing. water 30 atm is reduced to 90, while the amount of alumina containing 8.1% silica is, under the same conditions, the initial surface area, 210, is reduced only to 195. The process of siliconization allows to achieve almost unchanged properties of aluminum type B compression during dehydration even. After its long treatment at 280 ° C in an atmosphere of steam, i.e. under conditions in which the same alumina itself, not previously processed by silicon derivatives, decomposes rapidly. Example 6, Obtaining diethyl ether. o In a tubular reactor with a fixed catalyst bed in example 2, 1 g of activated alumina containing 10.2% sulfur dioxide is added, which is heated to 270 ° C in a stream of nitrogen supplied at a rate of 400 MJj / at atmospheric pressure for 2 hours, and then ethanol is loaded at a volume rate of 1 g / g h. The effluent from the reactor is analyzed by GLC. There are no by-products.
    9.45
    9.75
    10.05
    9.75
    9.45
    9.60
    9.60
    83,8
    4 83.6
    40 84.1
    3 84.0
    42 84.3
    4 84.4
    39 83.9
    2 83.7
    48 84.0
    .
    4 84.0
    45 83.0
    3 83.6
    50 82.9
    2 82.9
    46 1% organic ethanol is 90%. After 210 hours of operation, the catalyst converts and does not change. Examples 7-13. The preparation of the catalyst is carried out according to the following procedure. 150 grams of a ball alumina (type A) is placed in the press, which is purged with nitrogen to remove oxygen. Then, the corresponding one of the following compounds is introduced, g: (CH, 0) d.81S1d, 87.0; 94.5; (C2, H) SICU 90; (CH-) 4SI (C, H.) E51H 49.6; (CHjOTsiH SlHg 25.5; (COOCHj) The temperature is gradually raised to 20 ° C, which is maintained for 10 hours. The excess pressure is released and the nitrogen is passed through at the same temperature for 4 hours to displace the reaction products. The product is then cooled and calcined at a temperature. The catalyst thus obtained is used to prepare dimethyl ether with an atmobile catalyst bed at atmospheric pressure. The process conditions and results are shown in Table 7. T a b l and c a
    Example 14. Two layers of a fluidized catalyst are prepared, which consist respectively of alkaline oxide type A and the same oxide, but. processed () Si, resulting in a SiO content of 8.18 Weight. %
    . With the above catalysts, the process is conducted in tubular reactors with external electrically heated, having a diameter of 5 cm and a height of 80 cm.
    A baked metal porous diaphragm located at the bottom of the reactor allows the feed stream to be dispersed in such a way that the catalyst is maintained in a fluidized state. This layer contains 200 cm of catalyst.
    The porous diaphragm is also located at the top of the reactor in order to hold the smallest particles. The catalyst is methanol, which is pre-evaporated at atmospheric 150 120 90 75 60 45 30 30
     The data in the table- show that Silicon-coated Kata, the A + 10% SiO discharger after operation. In fact, does not show a change in the size analysis of the analysis, while the catalyst from the raw alumina of type A degrades and shows a more VEG percent of small particles,
    10% (catalyst type L t 10i SiO).
    The granulometric analysis for catalysts of type A and A + 10% 510 is presented in table. eight.
    As can be seen from the table, the change in activity does not occur.
    Spreadsheets
    eight
    . spherical pressure, served with a linear j, a speed of 8 CMVc, and the catalyst bed has a temperature. Methanol conversion is first 85% for both catalysts. However, after 200 hours of operation, the conversion of untreated alumina drops to 77%, while on catalyst A + 10% SiO. the conversion remains at the same level.
    After the specified period of work, the particle size analysis of the catalysts is again determined (CHjOH loading linear methanol feed rate cm / s; temperature 300 ° C, pressure 1 kg / cm), the data of which are given in Table. 9.
    E table
    1.30
    8.12
    13.05
    33.26
    10.40
    12.50
    18.20
    3.1.7
    权利要求:
    Claims (2)
    [1]
    Example 15. According to Example 1, 10 g of alumina is carried out with 7 g (02.45-0) 481 at the autoglow. The alumina-treated alumina is analyzed and its content of silica dusts, which is equal to about 17.2 wt.%, 1, g of this oxide a, pmini (containing 17.2% of dioxide k-p & l 13, 52 133, 35 10.30 13.83 17.81 1.60 ni) are heated to a stream of nitrogen (flow rate of 400 ml / h) at atmospheric pressure, after which the water is solid: methanol at a rate of 10 g / g-h. The stream of the reaction products, including nitrogen, dimethyl ether, unreacted methanol and water, is analyzed with the help of GLC, not detecting any by-products at ECM. The degree of conversion of methanol is 80%. Example 16. In Example 1, 10 g of alcine oxide is reacted with 2 g of () Si. The alumina treated in this way contains 5.1% silica, 1 g of this alumina is heated to A stream of nitrogen at a flow rate of 400 ml / h and then methanol is introduced at a rate of 10 g / g. The reaction product stream consisting of nitrogen, dimethyl ether, unreacted methanol and water is analyzed by means of GLC. At the same time, no byproducts of willows are available at tso tftMH fabomu mtalinamtsv (the fitt-l 55 is not detected. The conversion of methanol is 76 mol .%. Formula of the invention. The method of producing simple esters by dehydrating aliphatic alcohols at a temperature of 280-350 ° C and a space velocity of 1-10 cm in the presence of a catchiesclimate containing oxides of aluminum and silicon, so that process technology improvements in alumina is used as a catalyst, the surface of which is modified by a layer of silicon dioxide in the amount of 8–18% by weight of the catalyst Sources of information taken into account in examination 1, German Patent 844740, class 120, 5/09, published 29.05.52 (prototype)
    [2]
    2. Published for the Federal Republic of Germany No. 2451850 Cl. From 04 to 41/00, published 1972. ..7Г /, iJTplntfftfHUHf (or i / .iSecmweMy ciiocoSy 500 550

    vx
    "M

    :
    i “i
    I "
    one
    I n
    one
    about o cs
    Vq o
    I
    Se "m
    one
    but.
    03
    "
    iNa
    类似技术:
    公开号 | 公开日 | 专利标题
    SU841578A3|1981-06-23|Method of preparing ethers
    US4374265A|1983-02-15|Preparation of ethylidene diacetate
    Macquarrie et al.1997|Catalysis of the Knoevenagel reaction by γ-aminopropylsilica
    US4780552A|1988-10-25|Preparation of furan by decarbonylation of furfural
    US3453331A|1969-07-01|Catalytic synthesis of ketones from aldehydes
    US4289710A|1981-09-15|Process for producing methanol from synthesis gas with palladium-calcium catalysts
    US7205416B2|2007-04-17|Liquid phase synthesis of methylene lactones using novel grafted catalyst
    SU603330A3|1978-04-15|Method of preparing carbonic acid esters
    CA2119388C|1998-10-13|Hydrogenation catalyst, a process for its preparation and the use thereof
    US4244889A|1981-01-13|Production of acetamides with rhodium-manganese catalysts
    WO2006015023A2|2006-02-09|Liquid phase synthesis of methylene lactones using novel catalyst
    KR20010051302A|2001-06-25|Process for the preparation of ammonia and ammonia synthesis gas
    US20060025611A1|2006-02-02|Gas phase synthesis of methylene lactones using novel grafted catalyst
    WO2006015019A1|2006-02-09|Gas phase synthesis of methylene lactones using novel catalyst
    EP0091662B1|1988-07-06|Catalyst and process for dehydrating 2-alcohols
    US6124480A|2000-09-26|Process for preparing trioxane
    JP4911974B2|2012-04-04|Fischer-Tropsch synthesis catalyst and hydrocarbon production process
    US4471075A|1984-09-11|Process for producing two-carbon atom oxygenated compounds from synthesis gas with minimal production of methane
    US4446251A|1984-05-01|Process for producing two-carbon atom oxygenated compounds from synthesis gas with minimal production of methane
    JP2519976B2|1996-07-31|Method for producing oxygen-containing compound
    US4185022A|1980-01-22|Furfuryl alcohol production process
    CN107915709B|2020-01-03|Method for preparing ethylene carbonate from ethylene oxide and carbon dioxide
    Vishwanathan et al.1990|A direct correlation between dispersion, metal area, and vapour phase hydrogenation of aniline; a first report
    US5175308A|1992-12-29|Preparation process of indoles
    CA1139789A|1983-01-18|Process for the manufacture of ethanolfrom synthesis gas
    同族专利:
    公开号 | 公开日
    ZA756932B|1976-10-27|
    DE2552318C3|1978-05-24|
    US4337366A|1982-06-29|
    LU73829A1|1976-06-11|
    JPS5176207A|1976-07-01|
    PH16408A|1983-09-29|
    SE7513085L|1976-05-24|
    NO753905L|1976-05-24|
    AT341487B|1978-02-10|
    PL101463B1|1978-12-30|
    DD122068A5|1976-09-12|
    SE425564B|1982-10-11|
    DE2552318B2|1977-09-29|
    IE43445B1|1981-02-25|
    BE835757A|1976-05-20|
    TR18684A|1977-06-23|
    AU8639375A|1977-05-12|
    IT1025882B|1978-08-30|
    NO144829B|1981-08-10|
    BG33274A3|1983-01-14|
    AR210338A1|1977-07-29|
    DE2552318A1|1976-05-26|
    ES443121A1|1977-04-16|
    RO68986A|1982-05-10|
    IN142332B|1977-06-25|
    HU173921B|1979-09-28|
    YU293275A|1982-05-31|
    DK523475A|1976-05-22|
    EG12066A|1978-06-30|
    CA1069541A|1980-01-08|
    IE43445L|1976-05-21|
    MW6075A1|1977-03-09|
    NL7513658A|1976-05-25|
    FR2291961A1|1976-06-18|
    NO144829C|1981-11-18|
    ZM15775A1|1977-04-21|
    GB1492276A|1977-11-16|
    CS198178B2|1980-05-30|
    ATA884875A|1977-06-15|
    FR2291961B1|1977-12-16|
    BR7507742A|1976-08-10|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2459799C2|2007-03-30|2012-08-27|Чайна Петролеум Энд Кемикал Корпорейшн|Catalytic method of producing dimethyl ehter from methanol|
    RU2466980C2|2008-03-26|2012-11-20|Чайна Петролеум & Кемикал Корпорейшн|Method of producing dimethyl ether from methanol|US2282469A|1942-05-12|Production of ethers from alcohols |
    US2045560A|1936-06-23|Process for conversion of alcohols |
    US2922822A|1957-01-08|1960-01-26|Exxon Research Engineering Co|Production of methyl butenyl ethers|
    BE601277A|1961-02-15|1900-01-01|
    US3267156A|1961-08-07|1966-08-16|Socony Mobil Oil Co Inc|Production of dialkyl ethers|
    US3140252A|1961-12-21|1964-07-07|Socony Mobil Oil Co Inc|Hydrocarbon conversion with crystalline acid-metal aluminosilicates|
    US3175967A|1962-01-11|1965-03-30|Socony Mobil Oil Co Inc|Catalytic conversion with activated catalyst|
    IT1001614B|1973-10-31|1976-04-30|Snam Progetti|PROCEDURE FOR PREPARING MATERIALS WITH IMPROVED MECHANICAL AND THERMAL PROPERTIES AND MATERIALS OBTAINED|
    AR204423A1|1974-09-19|1976-02-06|Snam Progetti|PROCEDURE FOR PREPARING ALUMINA WITH IMPROVED MECHANICAL PROPERTIES AND ALUMIN OBTAINED THUS|JPS6210488B2|1980-06-16|1987-03-06|Nippon Gosei Arukooru Kk|
    NL8201289A|1982-03-29|1983-10-17|Shell Int Research|METHOD FOR PREPARING A CATALYTICALLY ACTIVE NETWORKED METAL SILICATE|
    US4605788A|1982-07-01|1986-08-12|E. I. Du Pont De Nemours And Company|Catalytic preparation of dimethyl ether|
    CA1215963A|1982-11-12|1986-12-30|Tenneco Oil Company|A1.sub.20.sub.3alkene isomerization process|
    US4507401A|1983-04-01|1985-03-26|At&T Bell Laboratories|Intermetallic catalyst preparation|
    JPH042577B2|1983-04-27|1992-01-20|
    US4806513A|1984-05-29|1989-02-21|Phillips Petroleum Company|Silicon and fluorine-treated alumina containing a chromium catalyst and method of producing same|
    JPS6117528A|1985-01-07|1986-01-25|Mitsubishi Gas Chem Co Inc|Preparation of dimethyl ether|
    CA1276002C|1985-12-31|1990-11-06|Lawrence L. Murrell|Catalysts comprising silica supported on alumina their preparation and use|
    US4708945A|1985-12-31|1987-11-24|Exxon Research And Engineering Company|Catalysts comprising silica supported on a boehmite-like surface, their preparation and use|
    DE3642845C2|1986-12-16|1992-04-09|Rwe-Dea Ag Fuer Mineraloel Und Chemie, 2000 Hamburg, De|
    US4885405A|1987-12-10|1989-12-05|Horst Dornhagen|Process for the production of pure dimethylether and a catalyst used in the process|
    ES2038353T3|1988-03-14|1993-07-16|Texaco Development Corporation|METHOD FOR SYNTHESIS IN A STAGE OF METHYL T-BUTIL ETER.|
    US5214217A|1990-03-16|1993-05-25|Texaco Chemical Company|Method for one-step synthesis of methyl t-butyl ether|
    US5650544A|1994-09-19|1997-07-22|Nippon Shokubai Co., Ltd.|Process for production of unsaturated ether and catalyst used for production of unsaturated ether|
    US5831116A|1996-12-18|1998-11-03|Northeastern University|Catalytic process for making ethers, aldehydes esters and acids from alcohols using a supercritical fluid mobile|
    JP4938941B2|2001-08-30|2012-05-23|関西電力株式会社|Synthesis method of dimethyl ether|
    JP4048043B2|2001-11-02|2008-02-13|日揮株式会社|Catalysts and methods for decomposition of carbonyl sulfide and hydrogen cyanide|
    JP5075104B2|2008-12-22|2012-11-14|住友化学株式会社|Catalyst for dimethyl ether production|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT29683/74A|IT1025882B|1974-11-21|1974-11-21|PROCESS FOR THE PREPARATION OF DIETERS|
    [返回顶部]