• 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:

    公开号:SU1250167A3
    申请号:SU813352656
    申请日:1981-06-26
    公开日:1986-08-07
    发明作者:Найер Вильгельм；Веберс Вернер；Юрген Оствальд Вольф
    申请人:Дейче Тексако Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to an improved method for producing lower alcohols, in particular to a method for producing isopropyl and sec-butyl alcohols, which can be used as solvents.
    The purpose of the invention is to simplify the process due to the fact that gaseous propene or butene before feeding it
    into the reactor or propene or butene on
    evaporation stages are impregnated with water in an amount of 0.3-1.8% by weight of propene or butene.
    The drawing shows an apparatus for carrying out the method.
    In the examples, technical propylene or butene is a mixture of this olefin with an appropriate aliphatic hydrocarbon.
    Having tried on a reactor with a clear width of 500 mm and a length of 10 m, filled with 1900 l of stainless steel packing and 1700 l of strongly acidic cation exchanger as a catalyst, 300 are fed through line 2, which is 85% by weight N-butene mixture of butane and butene (4534 mol of butene 253.9 kg / h), and through the pipeline 3 150.0 kg / h of water (8333 mol). Water is heated in the preheater 4 to 155-160 ° C. In addition, 54 kg / h (3000 mol) of water are supplied via pipeline 5, and 6 2699.6 kg / h of recycled technical olefin, i consisting of 1851.9 kg / h of butene and 847.7 kg / h butane. The feed consisting of recycled olefin and water (1.8% by weight from technical butene) stream is evaporated in the evaporator 7 and brought to temperature.
    The reaction is carried out at a pressure of 70 atm and a molar ratio of water and butene equal to 2.5: 1. The resulting sec-butyl alcohol, 201.3 kg / h, together with excess gas C (1953.4 kg / h of butgna and 894.1 kg / h of butane) and 31 kg / h of water are drained from the top of the reactor via pipeline B and after the pressure has been released and the water is separated, the separator is fed to column 9, from which 1318.0 kg / h of m-butane and 2631.0 kg / h of n-butene are withdrawn via line 10. This overhead stream is divided into a stream consisting of 101.5 kg / h of rt-butene and 46.4 kg / h of n-butane and, discharged through line 11, into a stream consisting of 976, 0 kg / h of m-butene and

    five
    0

    20 30 35 40
    55
    423.9 kg / h of N-butane and recirculated through conduit 12 to the upper part of column 9, and to the stream of said composition recycled through conduit 6. Pipeline 13 from column 9 discharged 201.3 kg / h (2720 mol) of sec-butyl alcohol and 2.1 kg / h (16.2 mol) of simple di-sec-butyl alcohol and 2.1 kg / h (16.2 mol) of di-sec-butyl ether as 99% crude alcohol.
    1.6 mol of sec-butyl alcohol and 0.0095 mol of ether are formed per hour of catalyst per hour. Throughout the reactor, the reaction temperature is 155-162 seconds, and no additional heating or cooling is required.
    Heat consumption data: 1,700 l of catalyst, capacity 1.6 mol of sec-butyl alcohol, 2999.9 kg / h of feed gas (2699.6 kg / h of recycled technical olefin and 300.3 kg / h of fresh technical olefin); the heat of evaporation of sec-butyl alcohol is 477.2 kJ / kg, and that of water at 155 ° C and 2102 kJ / kg; pre-saturation with water of 54 kg / h (1.8 wt.% of ole-final); maximum degree of saturation under reaction conditions of 54.9 kg / h; heat of reaction 102272 kJ / h; heat consumption for evaporation of water in the reactor is 1892 kJ / h, for evaporation of sec-butyl alcohol is 96060 kJ / h, in total .97952 kJ / h; heat balance (tegshot reaction minus heat consumption) 4320 kJ / h (excess heat).
    Example 2, with the difference that the process is carried out at a molar ratio of water to olefin of 1: 1. At the same time, 54 kg of water (1.8 wt.% From 3000.2 kg / h of circulating and fresh gas) are supplied to the butene evaporation stage and
    in the lower part of the reactor. I
    Due to the saturation of the source gas with water along the entire length of the reactor, the temperature is maintained at 150-155 ° C. The pressure in the reactor is 60 bar. The average amount of alcohol that is drained hourly through conduit 13 from column 9 is 199 kg (2689 mol). The content of di-sec-butypic ether is 2.03 kg / h (15.6 mol). Thus, the production rate is 1.58 mol / l of catalyst per hour.
    Heat consumption data: 1700 l of catalyst; capacity 1.58 moles of sec-butyl alcohol, 3000.2 kg / h of feed gas (2699.9 kg / h of fresh technical olefin); heat of hydration 37.6 kJ / mol sec-butyl alcohol; the heat of evaporation of sec-butyl alcohol is 477.2 kJ / kg, and that of water at 2102 kJ / kg; water preloading 5A kg / h (1.8 may.% of olefin); the maximum degree of saturation under the reaction conditions is 54.9 kg / h; heat of reaction 100993.6 kJ / h; heat consumption for evaporation of water in the reactor is 1892 kJ / h, for evaporation of sec-butyl alcohol 96060 kJ / h, in total 97952 kJ / h; heat balance (heat of reaction minus heat consumption) 3041.6 kJ / h (excess heat).
    Example 3. Example 1 is repeated with the difference that the process is carried out at 60 atm and a molar ratio of 10: 1. The amount of fresh gas used is 30.3 kg / h (4.56 kmol) and the total amount of gas (through pipelines 2 and 6) is 3000.1 kg / h. The total amount of water supplied to the reactor every hour is 821 kg. (45.6 kmol). Of this amount, 54 kg / h (1.8% by weight of butene) are withdrawn via line 5 and fed to the evaporation stage. At the same time throughout the reactor maintain the temperature without additional heating. At the bottom of column 9, the pipeline 13 hourly: an average of 201.3 kg (2720 mol) of secondary butyl alcohol and 2.1 kg (16.2 mol) of di-sec-butyl ether are obtained in the form of 99% crude alcohol . Thus, 1.6 mol of sec-butyl alcohol and 9.510 mol of ether are obtained per hour of catalyst per hour.
    Heat consumption corresponds to the flow rate shown in example 1.
    EXAMPLE 4 Example 3 is repeated with the difference that 9 kg / h (0.3% by weight of butene) of water is fed to the evaporation stage. At the same time throughout the reactor maintain the temperature of 155 C without additional heating. 1.6 mol of sec-butyl alcohol and 1-10 moles of di-sec-butyl ether are obtained per hour of catalyst per hour.
    Heat consumption data: process characteristics: - 1700 l catalysis
    2501674
    Torah; Capacity: 1.6 mol of sec-butyl alcohol, 3000.1 kg / h of feed gas (2699.8 kg / h of recycled technical olefin 5 and 300.3 kg / h of fresh technical olefin); heat of hydration 37.6 kJ / mol sec-butyl alcohol; the heat of evaporation of sec-butypic alcohol is 477.2 kJ / kg, and that of water at 10,2102 kJ / kg; pre-saturation with water 9 kg / h (0.3 wt.% from olefin); the maximum degree of saturation under the reaction conditions is 54.9 kg / h; heat of reaction 102272 kJ / h; Teppe 15 consumption for evaporation of reactor water
    96481 kJ / h, for the evaporation of sec-butyl alcohol 96060 kJ / h, in the amount of 192541 kJ / h.
    Heat balance (heat of reaction Jo minus heat consumption) -90,269 kJ / h (the lack of heat is compensated for in the preheater 4 and the evaporator 7).
    EXAMPLE 5 Example 4 is repeated, with the difference that the process is carried out 25 at 170 ° C and 40 atm. In this case, 1.8 mol of sec-butyl alcohol and 2-10 mol of di-sec-butyl ether are obtained per hour of catalyst per hour.
    3Q: Heat consumption data: process characteristic - 1700 l of catalyst; productivity 1.8 mol of sec-butyl alcohol, 3000 kg / h of source gas (2699.7 kg / h of recycled Technical olefin and 300.3 kg / h of fresh technical olefin), heat of hydration 37.6 kJ / mol sec-butyl alcohol; the heat of evaporation of sec-butyl alcohol is 477.2 kJ / kg, and that of water at 170 C is 2133 kJ / kg; water predation 9 kg / h (0.3 wt.% of olefin); maximum; the degree of saturation under reaction conditions is j54.9 kg / h; heat of reaction 115056 kJ / h, heat consumption for evaporation of water in the reactor 97904. kJ / h, for evaporation of sec-butyl alcohol 108181 kJ / h, total 206085 kJ / h; heat balance (heat of reaction minus heat consumption) -91029 kJ / h (the lack of heat is compensated in heater 4 and evaporator 7).
    EXAMPLE 6 Example 4 is repeated with the difference that the process is carried out
    35
    40
    45
    55
    at 135 C 100 atm. In this case, 1, b5 mol of sec-butyl alcohol and 510 mol of di-sec-butyl ether are obtained per hour of catalyst.
    Data on heat consumption: process characteristics - 1700 l of catalyst; capacity 1.65 mol of sec-butyl alcohol, 2999.9 kg / h of feed gas (2699.6 kg / h of recycled technical olefin and 300.3 kg / h of fresh technical olefin); heat of hydration 37.6 kJ / mol sec-butyl alcohol; the heat of evaporation of sec-butyl alcohol is 477.2 kJ / kg, and that of water at 2143 kJ / kg; preliminary. water saturation 9 kg / h (0.3 wt.% of the olefin); maximum temperature saturation in terms of kg / h;
    20
    54.9 kg / h; heat of reaction 105468 kJ / h, heat consumption for evaporation of water in the reactor is 98364 kJ / h, for evaporation of sec-butyl alcohol 99162 kJ / h, in total 197526 kJ / h; heat balance (heat of reaction minus heat consumption) -92058 kJ / h (the lack of heat is compensated in heater 4 and evaporator 7).
    Example 7. B-reactor 1 with a width of 25 mm in the light of 200 mm and a length of 3 m, filled with 147 liters of nozzles from. stainless steel and 126 l of strongly acidic cation exchanger, through pipeline 2 serves
    isopropyl alcohol, 555.8 kg / h of source gas (49V, 1 kg / h of recycled technical olefin and 57.7 kg / h of fresh technical
    5 olefins); warmth of hydration
    50.2 kJ / mol isopropyl alcohol; heat of evaporation of isopropyl alcohol 586 kJ / kg, -a water at 2143 kJ / kg; preliminary
     With a water of 3.5 kg / h (0.63 May,%) the heat of reaction is 24036 kJ / h; 6858 kJ / h of evaporation of water in the reactor, 16865 kJ / h of evaporation of isopropyl alcohol, total
     5 23723 kJ / h; heat balance (heat of reaction and minus heat consumption) 313 kJ / H (excess heat)
    Example 8. An example is repeated with the difference that the reaction is conducted at 160 ° C and 40 atm. In addition, the foam is saturated with 7 kg / h (1.32% by weight of propene) water. At the same time, the productivity of the process is 4.2 mol of isopropyl alcohol per liter of catalyst per hour.
    Data on heat consumption: process characteristics - 126 l of catalyst; performance 4.2 mol of
    57.7 kg / h of 96% propene (1.32 kmol). 30 propyl alcohol, 528.7 kg / h, is used through a pipeline of 6,498.2 kg / h of recycled technical propene. In addition, pipeline 3 supplies 233 kg / h (45.6 kmol) of water, a part of which (3.5 kg / h or 0.63 wt.% 35 from technical propene) through pipeline 5 is added to the raw materials fed to evaporation stage. The reaction is carried out at 135 ° C, 100 atm and a molar ratio of water and propene equal to 40 1.05: 1. At the same time, the reaction temperature is kept constant throughout the reactor without the need for external heating or cooling.
    Hourly receive 28.78 kg of isopropyl alcohol 45 (3.8 mol of alcohol per 1 liter of catalyst per hour) and 0.22 kg of diisopropyl ether).
    Data on heat consumption: characteristic of the process - 126 l of catalyst; performance 3.8 mol
    feed gas (471 kg / h of recycled technical olefin and 57.7 kg of fresh technical olefin); temperature of hydration is 50.2 kJ / mol isopropanol; evaporation heat of isopropyl alcohol is 586 kJ / kg, and water at 2112 kJ / kg, preliminary saturation with water is 7 kg / h (1.32 wt.% of technical olefin, the maximum degree of saturation under the reaction conditions is 7.1 kg / h; reaction heat 26566 kJ / h; heat consumption for evaporation of water in the reactor 211 k, CJ / h, evaporation of isopropyl alcohol 18,635 kJ / h, a total of 18,846 kJ / h; heat balance (reaction heat minus heat consumption) 7720 kJ / h ( excess heat).
    The data on the total material balance in examples 2-8 are shown in the table.
    isopropyl alcohol, 555.8 kg / h of source gas (49V, 1 kg / h of recycled technical olefin and 57.7 kg / h of fresh technical
    olefin); warmth of hydration
    50.2 kJ / mol isopropyl alcohol; evaporation heat of isopropyl alcohol 586 kJ / kg, -a water at 2143 kJ / kg; preliminary pressing with water of 3.5 kg / h (0.63 May,%) is the heat of reaction of 24036 kJ / h; heat consumption for evaporation of water in the reactor is 6858 kJ / h, for evaporation of isopropyl alcohol 16865 kJ / h, in total
    23723 kJ / h; heat balance (heat of reaction minus heat consumption) 313 kJ / H (excess heat)
    Example 8. Example 7 is repeated with the difference that the reaction is carried out at 160 ° C and 40 atm. In addition, propene is saturated with 7 kg / h (1.32% by weight of propene) water. The productivity of the process is 4.2 mol of isopropyl alcohol per liter of catalyst per hour.
    Data on heat consumption: process characteristics - 126 liters of catalyst; capacity: 4.2 mol of isopropyl alcohol, 528.7 kg / h of source gas (471 kg / h of recycled technical olefin and 57.7 kg / h of fresh technical olefin); hydration point of 50.2 kJ / mol isopropyl alcohol; evaporation heat of isopropyl alcohol is 586 kJ / kg, and water at 2112 kJ / kg, pre-saturation with water 7 kg / h (1.32 wt.% from technical olefin); the maximum degree of saturation under the reaction conditions is 7.1 kg / h; reaction heat 26566 kJ / h; heat consumption for the evaporation of water in the reactor 211 k, GW / h, for the evaporation of isopropyl alcohol 18,635 kJ / h, a total of 18,846 kJ / h; heat balance (heat of reaction minus heat consumption) 7720 kJ / h (excess heat).
    The data on the total material balance in examples 2-8 are shown in the table.
    Editor A.Shishkin
    Compiled by A. Evstigneev
    Tehred N. Bonkalo Proofreader M. Demchik
    Order 4341/60 Circulation 379Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, Projecto st., 4
    Table continuation
    权利要求:
    Claims (1)
    [1]
    METHOD FOR PRODUCING ISOPROPYL OR SECOND-BUTYL ALCOHOL by vaporizing technical propene or butene, feeding it in a gaseous state to the lower part of the reactor, which is also separately fed ! water the interaction of propene or butene with : water at a temperature of 13517O 0 C, pressure 40-100 atm, the molar ratio of water, propene or butene 1-10: 1 in the presence of strongly acidic cation exchange resin, followed by isolation of the target product, characterized in that, in order to simplify the process , gaseous foam or butene before feeding it into the reactor or propene or butene at the stage of evaporation is saturated with water in an amount of 0.3-1., 8 wt.% of propene or § butene.
    SU <„. 1250167 AZ
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    引用文献:
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    GB809318A|1956-09-27|1959-02-18|Exxon Research Engineering Co|Hydration of propylene|
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    DE1249845B|1965-07-24|
    DE2147739C3|1971-09-24|1974-11-14|Deutsche Texaco Ag, 2000 Hamburg|
    JPS49117412A|1973-02-27|1974-11-09|
    DE2429770C3|1974-06-21|1981-04-16|Deutsche Texaco Ag, 2000 Hamburg|Process for the production of lower alcohols by direct catalytic hydration of lower olefins|DE3419392C1|1984-05-24|1985-12-05|Deutsche Texaco Ag, 2000 Hamburg|Process for the continuous production of isopropyl alcohol or sec. Butyl alcohol|
    US4670612A|1985-06-18|1987-06-02|Sumitomo Chemical Company, Limited|Method for producing alicyclic alcohols|
    IT1223016B|1987-10-29|1990-09-12|Enichem Anic Spa|PROCESS FOR THE DIRECT HYDRATION OF LINEAR OLEFINS|
    US4956506A|1989-12-21|1990-09-11|Conoco Inc.|Vapor-phase hydration of olefins to alcohols in series reactors with intermediate alcohol removal|
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    US5268515A|1992-05-01|1993-12-07|The Pritchard Corporation|Process of preparing an isopropanol and diisopropyl ether oxgenate motor fuel additive|
    US5191129A|1992-05-01|1993-03-02|The Pritchard Corporation|Method of preparing an isopropanol and diisopropyl ether oxygenate motor fuel additive|
    US5488185A|1993-09-30|1996-01-30|The Boc Group, Inc.|Process for the production of ethanol and isopropanol|
    US6563006B2|2001-04-30|2003-05-13|Melvin K. Carter|Catalytic oxidative conversion of hydrocarbons to aldehydes|
    US7399891B2|2005-06-08|2008-07-15|Exxonmobil Chemical Patents Inc.|Process for alcohol production by selective ether decomposition|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3024146A|DE3024146C2|1980-06-27|1980-06-27|Process for the continuous production of alcohols having 3 to 5 carbon atoms|
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