• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Toluene and toluene derivatives are oxidatively dehydrocoupled to produce stilbene and stilbene derivatives by heating toluene or a toluene derivative in the vapor phase with a metal- and oxygen-containing composition which functions as an oxidant or oxygen carrier and has the empirical formula SbaPbbBicOd WHEREIN A IS 1, B IS 0.2 - 10, C IS 0 - 5 AND D IS A NUMBER TAKEN TO SATISFY THE AVERAGE VALENCES OF THE Sb, Pb and Bi in the oxidation states in which they exist in said composition. Alternatively, the same metal- and oxygen-containing composition can be employed as a catalyst for the dehydrocoupling reaction when oxygen or an oxygen-containing gas is heated with the hydrocarbon reactant.
    公开号:SU869552A3
    申请号:SU772535555
    申请日:1977-10-26
    公开日:1981-09-30
    发明作者:Пинг Ли Тао
    申请人:Монсанто Компани (Фирма)；
    IPC主号:
    专利说明:

    (5) METHOD FOR OBTAINING STYLBENE OR ITS ALKYL DERIVATIVES
    one
    The invention relates to a process for the preparation of 1,2-diphenylethylene (stilbene) and its alkyl derivatives.
    Due to its unsaturated character, stilbene is very reactive; g is able to find MoweT use in a whole range of organic reactions. It is useful in the preparation of products that can be used in the manufacture of dyes, paints and resins, and it is also valuable as a component in optical brighteners, pharmaceutical preparations and as an organic intermediate.
    A known method of producing styrene or its alkyl derivatives by vapor-phase oxidative dehydromerization of toluene or its alkyl derivatives at elevated temperature in the presence of a diluent - water vapor and a catalyst based on lead oxide. According to a known method, the process is carried out at 500-650 ° C in the presence of lead oxides, cadmium, bismuth, possibly on a carrier 25
    The yield of the target product is 18-27%.
    The purpose of the invention is to increase the yield of target products.
    This aim is achieved with a method for producing a stilbene or its alkyl derivatives vapor phase oxidation oxidative coupling toluene or its alkyl derivatives in the presence of a catalyst - oxides of lead and antimony, or a mixture of lead, antimony and bismuth, with an atomic ratio of Pb: Sb or Pb: Sb: Bi, equal respectively 0 or 0 , 2-5: 1: 0.25-5 at 500-60 0 С.
    The method can be carried out in a single reactor or in a whole series of reactors using either a stationary or a fluidized bed or a moving catalyst bed in order to achieve the contact of a reagent or reagents with an oxidizing agent or catalyst. The reactant — toluene or its derivative — is usually heated and 5 reactors are introduced in the form of steam. However, the reagent can be introduced into the reactor in liquid form with subsequent evaporation. The temperature range in which the reaction is carried out is in the range of 500-650 C, preferably 5 0-600 C. The pressure is not critical, so it is possible to work under reduced, atmospheric or elevated pressure. The contact time of the hydrocarbon with the oxidizing agent or catalyst in the reactor varies depending on the reaction temperature and the amount of toluene conversion. At higher temperatures and a small volume of toluene conversion, a shorter contact time is required. Typically, the contact time ranges from 0, s. For optimum conversion and selectivity in the preferred temperature range, a contact time of about 2 ° C is preferred. In addition to toluene and / or its derivatives, inert substances may be present in the reactor, such as nitrogen, helium, etc. Inert substances of this kind can be introduced separately or they can be mixed with other substances when fed into the reactor. Water or steam may be introduced into the reaction zone, preferably, during reactor loading in order to improve selectivity with respect to the desired products and, in particular, to suppress complete oxidation in CO. A vapor to hydrocarbon ratio of 0 or more is suitable; however, the upper limit is determined by practical financial reports. Ratios ranging from ISJB are preferred. The reaction can be carried out in the presence of or without added free oxygen. If oxygen is not supplied with the hydrocarbon, the oxygen required for the reaction is formed by reducing the catalyst during the reaction. This circumstance makes it necessary to regenerate or re-oxidize, which is easily accomplished by heating in air or oxygen at temperatures of the order of 3OO-BBO C for 3060 minutes. In the semi-continuous mode of operation, regeneration can be carried out by periodically interrupting the course of the reaction to over-oxidize the catalyst, i.e., reaction periods are carried out in a cycle with regeneration periods. However, it is possible to work completely without interruptions; however, part of the catalyst can be continuously or intermittently removed and reoxidized, and the reoxidized product can then be continuously or intermittently fed back into the reaction system. The last of the above methods can be applied when the catalyst is supplied in the form of a fluidized or moving bed. When used as an oxygen reagent, it is used in an amount sufficient to achieve a molar ratio of hydrocarbon and oxygen in the order of 1-8, preferably 2-6. Oxygen can be supplied only as a free element, or as an oxygen-containing gas, such as air. Suitable catalysts can be obtained in various ways. The simplest method involves adding metal oxides to water with stirring, heating the mixture to evaporate the water, drying and calcining. According to another method of preparation, powdered metal oxides can be initially mixed thoroughly, followed by obtaining a mass by adding water and again mixing this mass. The mass can be sprayed and air dried, followed by calcining in air. The calcined product is then crushed and sieved to achieve the desired grain size. Alternatively, the metal oxides are mixed with a tablet aid material that has been calcined before use. The catalyst can be used in pure form or on a carrier (for example, alumina, silica, aluminosilicate, metal aluminates, such as magnesium aluminate, and so-called PS carriers). The temperatures used for calcination vary within the range of 400-1200 ° C. Temperatures, starting from 900-1100 ° C, cause an increased selectivity with a simultaneous slight decrease in activity. Therefore, the preferred calcination temperatures are 700 ° C. Duration of the process
    KanbUMHMpoBtTfiMH fluctuates within 1-6 hours, preferably 2-Ch, at elevated temperatures. The surface of the catalyst is not critical and may range from 0.1-5.0.
    Example 1. A catalyst is prepared by adding to 250 ml of water 58.3 g of antimony trioxide and 134 g of PHO with stirring. This mixture is heated to evaporate the water, the resulting solid product is dried in an oven at overnight. A portion of the solid product is calcined at 0 ° C for 1 hour, then at 600 ° C k hours and, finally, 3 m at 950 ° C. The resulting product has an atomic ratio Sb / Pb of 1: 1.5
    3 As a reactor for the conversion of toluene, a stainless steel tube is used. It is equipped at the upper end with an intake device.
    for introducing the reagent and, at the lower end, for the outlet effluent collection device or for supplying it to a gas chromatographic device for analysis. The reactor contains 25 g of catalyst. A reactor in which a pressure of mm Hg is maintained and the temperature is 5 ° C, steam and toluene in a molar ratio of 1: 1 are supplied at a rate such that the residence time of toluene in the reactor is s and the reaction time is about 1 minute. Between the individual passages, the catalyst regenerates by passing air through it at 5 ° C for about 30-60 minutes. The results of individual passages for the conversion of toluene and the amount of toluene converted into stilbene (selectivity for stilbene) are summarized in table. one.
    Table 1
    Example 2. A series of catalysts having an Sb: Pb atomic ratio of 1: 5 is prepared according to the method for preparing catalysts in the process of dehydrocyclization of toluene in the preparation of stilbene.
    The powdered lead oxide and antimony oxide are thoroughly mixed, distilled water is added and the paste is prepared by mixing. The paste is forced through a sieve with holes mm and dried in air at. The catalyst is then calcined at 600 ° C. The resulting product is crushed and sieved through a sieve with openings of k30 min. A series of experiments was carried out in which the dehydrocyclization was carried out at a molar ratio of pairs: toluene equal to 2 and contact time +, 23 s using various catalysts obtained by the proposed method. The reactor used is essentially the same as that of Example 1, except that it contains a concentric thermocouple. The reactor contains about 18 ml (about 25 g) of catalyst. Toluene and steam are metered through the inlet system using an equilibrium type evaporator and syringe pumps, passing through the catalyst in the reactor about
    7 8695528
    3 min. The reaction effluent is summarized in table. 2. All of them are in a gas chromatographic apparatus with average double facies for the purpose of analysis. Re-passes. Example 3. A catalyst with an Sb / Pb atomic ratio of 1: 2 and a surface of 0.37 m / g is prepared as in Example 2 and then 3 m is re-calcined at 900 ° C. This catalyst is loaded into a reactor similar to that in Example 2, then the temperature is conducted, from 570 590 560 Time of contact 1, 28 1.28), 98 times, from 15.7 15, 26.9 Conversion,% Selectivity,% cis stilbene trans-stilbene 57.1 52, b5.2 bibenzyl 27, 8.3 8.6 benzene 6, 8.3 8.6 2.1 3.6 3, The average value of three experiments Example. Analogously to example 2, a catalyst is obtained which is recalcined for 2 hours at and at 3 hours. The atomic Sb / Pb ratio of this composition is 1: 2. It is used in analogous examples 2 and 3 of the reactor, the dehydro-coupling reaction
    Table 2: a series of experiments where steam and toluene (2: 1) are contacted in the reactor with a catalyst for 3 minutes, after which the effluent from the reaction is analyzed by gas chromatography. Conditions and results of the reaction are summarized in table. 3. Table 3 570 580 580 580 590 2.68 1.98 3.0 0.7 26.5 26.6, 8 b5.5 59.7 59.7 9, 9.9 15.2 9, 9, 9 1.2 3.7 3.6 6.9 toluene is carried out in the manner described in the previous examples using different steam-to-topop ratios. Reaction temperature, time to tact approx. 4.23 s. The conditions and peayjibiahi analysis are summarized in Table. k. 186 Example 5. Another series of experiments with toluene dehydro-combination was carried out in the same device and according to the same method as in examples 2-4. By the method described in example 2, a catalyst is obtained with an Sb / Pb atom ratio of 1: 2, after which the samples of this mixture are re-calcined at different temperatures over different time periods. Then the samples are evaluated for suitability as a calcination temperature, with 600 Calcination time, h 2.0 Surface, 37 Transformation,% 80.2 Selectivity,% cis-stilbene trans-stilbene 0.2 bibenzyl 1.9 benzene 3.9 11,
    The average value of the experiments.
    Example 6 A catalyst is obtained by adding to 250 ml of water a further 58.3 g of antimony oxide, g of lead oxide and 23.3 g of bismuth trioxide with stirring. The resulting liquid mass is heated, stirring, in order to evaporate water; The solid obtained is dried in an oven at 110 ° C. overnight and then calcined at 2 hours. The target oxidant has
    the ratio of Sb / Pb / Bi atoms is 1: 1.5:: 0.25
    The catalyst obtained above was used in a series of experiments in contacting toluene and steam at a molar ratio of 1: 2 under various conditions with the catalyst contained in the reactor described in Example 2. The reaction conditions and the results are shown in Table. 6
    Table 6 700 800 800 900 900 900 1000 1000 1100 3.0 2.0 C, O 1.0 3.0 5.0 2.0 C, O 3.0 0.320.250.260.280.220.22 0.210.150.26 79, t62.963, 25751, 7 2k, 16,315,7 37,952,653,558,665,968,5, 235,831.8 1,83,53,34,7,16,7 29,536, 5 38,12i, 92k, B19,715,612.8 8,512,78,8 11 , 2 7 212 catalysts with toluene dehydrosoxidia in the same device and according to the same method as in examples 2-k, Reaction temperature, contact time, 2 s, ratio of steam to toluene when fed to the reactor 2.0, and reaction time 3 min. The results obtained at different calcination temperatures for different periods of time are summarized in Table. 5. Table5 6.5 5.2 3.9, 6 6.7 7.7
    13
      3, 7
    pb2, sbBi4.
    Pb, 5 Sb Pb4SbBii
    PbSbSi PbBi2.
    1i |
    869552 Continued table. 6
    Table 8
    560
    权利要求:
    Claims (1)
    [1]
    1 2 1 2 2 2 590 560 59 560 590 Claims The method of producing stilbene or e alkyl derivatives by vapor phase oxidative dehydrodimerization of toluene or its alkyl derivatives at 500-600 ° C in the presence of a water vapor diluent and a catalyst based on lead oxide, different from so that, in order to increase the yield of the target product, a catalyst is used, which additionally contains antimony oxide or a mixture of antimony and bismuth oxides with an atomic ratio of Pb: Sb or Pb: Sb: Bi equal to 0.2-5.1 or 0, respectively, 2-5: 1: 0, 25-5. Sources of information taken into account during the examination 1. US patent ff 3965206, cl. 260-669, published 22.06,76 (prototype) „
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    同族专利:
    公开号 | 公开日
    CA1099697A|1981-04-21|
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    FR2369233A1|1978-05-26|
    ES463483A1|1978-07-16|
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    JPS5356646A|1978-05-23|
    DD133318A5|1978-12-27|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    FR1497090A|1965-10-20|1967-10-06|Eastman Kodak Co|Improved process for preparing 1, 2-bis ethylenes|
    US3476747A|1965-10-20|1969-11-04|Eastman Kodak Co|Manufacture of 1,2-bisethylenes|
    US3557235A|1968-12-27|1971-01-19|Union Carbide Corp|Production of ethylbenzene and benzene from toluene|
    JPS5335902B2|1973-07-07|1978-09-29|
    US3868427A|1973-10-19|1975-02-25|Monsanto Co|Dehydrocoupling process|US4255603A|1979-12-10|1981-03-10|Monsanto Company|Dehydrocoupling of toluene|
    US4247727A|1979-12-10|1981-01-27|Monsanto Company|Dehydrocoupling of toluene|
    US4278826A|1979-12-10|1981-07-14|Monsanto Company|Dehydrocoupling of toluene|
    US4255602A|1979-12-10|1981-03-10|Monsanto Company|Stilbene formation by means of toluene dehydrocoupling using a cobalt-lanthanide catalyst|
    US4243825A|1979-12-10|1981-01-06|Monsanto Company|Dehydrocoupling of toluene|
    US4255604A|1979-12-10|1981-03-10|Monsanto Company|Dehydrocoupling of toluene|
    US4268703A|1979-12-10|1981-05-19|Monsanto Company|Dehydrocoupling of toluene|
    US4278825A|1979-12-10|1981-07-14|Monsanto Company|Dehydrocoupling of toluene|
    US4254293A|1979-12-10|1981-03-03|Monsanto Company|Dehydrocoupling of toluene|
    US4278824A|1979-12-10|1981-07-14|Monsanto Company|Dehydrocoupling of toluene|
    DE3062083D1|1979-12-10|1983-03-24|Monsanto Co|Dehydrocoupling of toluene|
    US4268704A|1979-12-10|1981-05-19|Monsanto Company|Dehydrocoupling of toluene|
    US4454363A|1982-06-11|1984-06-12|Exxon Research & Engineering Co.|Process for preparing inorganic metal oxygen composition capable of dehydrocoupling toluene|
    US4727208A|1986-09-12|1988-02-23|The Dow Chemical Company|Oxidative coupling with methyl-substituted benzenes|
    US20070251462A1|2006-04-12|2007-11-01|Kurt Harris|Livestock transportation system and cover|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/735,865|US4091044A|1976-10-27|1976-10-27|Dehydrocoupling process|
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