• 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:
    Terephthalic acid (e.g. that produced by oxidizing p-xylene) is obtained in the form of dried powder from a slurry containing terephthalic acid and acetic acid and/or water by introducing the slurry into a tubular type heater having at least one heating tube which discharges at one end into a separation chamber whereby the slurry is converted into a solid-gas mixture in the heating tube, and discharging the mixture into the separation chamber to separate the solid component from the gas component. Critical slurry concentrations for continuous operation are given. <IMAGE>
    公开号:SU1087072A3
    申请号:SU792776761
    申请日:1979-06-07
    公开日:1984-04-15
    发明作者:Цутия Фудзио；Ямамото Кензо；Ямагути Кацунобу；Окагами Акио
    申请人:Джей Джи Си Корпорейшн (Фирма)；Ориент Кагаку Когио К.К. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to organic chemistry, specifically to the new method of separating terephthalic acid from a suspension in water and / or acetic acid, obtained by oxidizing p-xylene with air in the presence of heavy metal salts catalysts in an acetic acid medium. toluene diisocyanate from the resin installation consisting of a tubular heater connected to a separator chamber. The solution containing toluene diisocyanate, resin and pitch is introduced into the tubular heater and in the separator chamber is divided into toluene diisocyanate in the form of steam and into the resin and pitch in the form of porous mass Cl3. terephthalic acid, which consists in using for separating terephthalic acid from a suspension in acetic acid and / or water, centrifugal separators, followed by drying the desired product in a drum incubator at 100-250 ° C in a stream of nitrogen. As a result, tereftshevuyu acid with a moisture content of 0.11 wt.% C23. The disadvantages of the method are the duration of the process, and therefore the prolonged effect of the elevated temperature on the target product, the need to use sophisticated technological equipment (centrifugal separator, auger, drum dryer, nitrogen recycling system), and the need to carefully control the product humidity after leaving centrifugal separator, as with a decrease in the water content, the screw and the dryer stop. The aim of the invention is to simplify the process of separating terephthalic acid from a suspension in water and / or acetic acid. The goal is achieved by the fact that, according to the method of separating terephthalic acid from its suspension in acetic acid and / or water during heating, the suspension at the concentration of terephthalic acid in it calculated by the formula: C (2,) - nd. + (3,) - d-ot). where C is in wt.%; 8 - temperature of the heating pipe, C; d- the molar concentration of water in the suspension is passed through a heating tube in which the temperature is maintained at 80-240 ° C, after which the mixture of solid and gaseous substances formed is transferred to a separation chamber with which the pipe is connected at one end and in which pressure 0 is maintained, 1-12 atm, to obtain terephthalic acid in powder form. Preferably used for collecting terephthalic acid is a pick-up into which it enters through a flap at the bottom of the separation chamber, in which the pressure is kept lower than in the chamber, which is 0, t1, 5 atm, and if necessary, an inert gas is passed through the collector use of pressure in the separation chamber within 1-6 atm at a temperature near the open end of the heating tube, at the suspension medium that exceeds the dew point at a pressure in the separation chamber. The temperatures, pressures, charges and composition of the suspension are shown in Table 2 for examples. 1 and. 2. Example 1. A suspension of terephthalic acid is dried using a device consisting of a pipe and a separation chamber having a glass window through which the ejection of terephthalic acid can be observed from the open end of the heating pipe. In case of blockage, you can quickly find out about it by stopping the ejection of the powder. The suspension, which contains 80% by weight of a solid and whose medium consists only of acetic acid, is led to a heating tube. The suspension is supplied smoothly by suction into the separation chamber, the pressure of which is maintained at an equal 120 mmHg. The temperature of the heating tube. support equal to 80 ° C by means of a hot branch. Work is carried out without plugging the pipe. After working for 30 minutes, erephthalic acid collected in the bottom of the separation chamber is removed. The amount of residual moisture in the product is determined by heating in an electric oven in a nitrogen atmosphere for 2 hours, which is 0.065%. Examples 2-11. The process of drying terephthalic acid is repeated with different s; suspensions, medium compositions, and heating tube temperatures that satisfy the conditions of the formula derived from experimental results (Tables 1 and 2).
    In all cases, the work is carried out for a long time to obtain a highly dried terephthalic acid powder.
    Example 12 .. In the same device that was used in example 1 and which is equipped with a solid product collector, a suspension containing 60 wt.% Solids and whose medium consists of 90 wt.% Acetic acid and 10 wt. % water, 270 The heating pipe is steam heated to. The pressure in the separation chamber is 1 kg / cm2 abs., I.e. atmospheric.
    These conditions lead to continuous operation without clogging the heating tube. After working for 10 minutes, the valve at the bottom of the separation chamber is closed, and the terephthalic acid is removed from the collector.
    The amount of residual moisture (0.074%) is determined by the above method.
    examples 13-29. The process carried out in example 12 is repeated with different suspension
    media, suspension concentrations, heating tube temperatures, and pressures in the separation chamber (Tables 1 and 2).
    Example 30. A ribbon mixer was used as a terephthalic acid collector, and the separation of the solid, substance and gas was carried out under the same conditions as in Example 12.
    After working for 10 minutes, the valve is closed and the pressure in the collector is reduced to 0.1 kg / cm-abs. Then, with stirring, nitrogen gas is introduced into the collector. Terephthalic acid is recovered after increasing the pressure in the collector to atmospheric. A certain amount of residual moisture is low - 0.035%.
    Examples 31 and 32. Example 30 is repeated at other temperatures of the heating tube and pressures in the separation chamber (Tables 1 and 2).
    Example 33. Terephthalic acid is separated from volatile materials under the same conditions as in example 30. After working for 10 minutes, the valve at the bottom of the separation chamber is closed and heated nitrogen gas is introduced into the collector for 5 minutes at a flow rate of 100 liters / h
    Example 34. Example 31 is repeated with the exception that the pressure in the collector is 1.5 kg / cm abs. These conditions correspond to the modification of Example 15, where the collector, although not under vacuum, was kept under pressure lower than in the separation chamber.
    Table 1
    Continuation of the table. t
    300
    120
    300 200
    300 200
    600 200
    300 158
    (1) 130
    (1) 240
    (1) 245
    (5) 185
    (7.5) 205
    (10) 215
    (12) 245
    (one)
    Atmos150 ferrous
    (1.5)
    Also
    122 (1.5)
    245 (7) 175
    (ten)
    190 (1) 130
    (1.5)
    130
    (1.5) 245
    (7) 185
    (10) 200
    (2) 170
    470
    White
    1.12 460 The same 1.15 720 1.02 650 1.13 560 31.1 740 57.9 510 57.2
    Yellow 510 0.86 White 930 0.85
    The same 960 0.84
    11 1230 0.85
    Yellowish 1250 0.86 710 White 1.03
    710
    Also
    57,8
    Yellowish 480 57.3 White 860 57.3 57.6 Same
    1100,770 0.96
    620
    57.3
    Yellow 450 57.2 White 810 57.9 Same 780 0.86 580 0.96
    Proceedings 2
    权利要求:
    Claims (3)
    [1]
    1. METHOD FOR ISOLATING TERPHTHALIC ACID from its suspension in acetic acid and / or water when heated, characterized in that, in order to simplify the process, the suspension is at a concentration of terephthalic acid in it, calculated by the formula:
    C = (2.56 ° 4 +66) οί + (3.2 0 ° E 3-74) · (1-c0, where C is expressed in wt.%;
    Θ is the temperature of the heating pipe, in ° C;
    cl is the molar concentration of water in the suspension. It is passed through a heating pipe in which a temperature of 80-240 ° C is maintained, after which the resulting mixture of solid and gaseous substances is transferred to a separation chamber: a chamber to which the pipe is connected at one end and in which pressure is maintained 0 , 1-12 atm, to obtain terephthalic acid in powder form.
    [2]
    2. The method of pop. 1, characterized in that in the separation chamber maintain pressure
    1-6 atm at a temperature near the open end of the heating pipe by 20 ° C higher than the dew point of the suspension medium at a pressure in the separation chamber.
    [3]
    3. The method of pop. 1, characterized in that terephthalic acid is collected through a valve in the bottom of the separation chamber in a collector in which the pressure is lower than in the chamber, comprising 0.1-
    1.5 atm., And if necessary inert gas is passed through the collector.
    > SU „.1087072>
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    同族专利:
    公开号 | 公开日
    GB2024810B|1982-09-22|
    CS207795B2|1981-08-31|
    DD144258A5|1980-10-08|
    JPS5811418B2|1983-03-02|
    DE2923382A1|1979-12-20|
    DE2923382C2|1983-09-08|
    GB2024810A|1980-01-16|
    JPS54160331A|1979-12-19|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    IT1289177B1|1997-01-17|1998-09-29|Lonza Spa|POLYCARBOXYLIC ACID RECOVERY PROCEDURE|
    CA2282255C|1997-04-10|2007-12-04|E.I. Du Pont De Nemours And Company|Improved method for producing crystalline carboxylic acids and apparatus therefor|
    US6972342B1|1997-04-10|2005-12-06|Invista North America S.A R.L.|Method for producing crystalline carboxylic acids|
    AT504996B1|2007-03-02|2009-03-15|Andritz Tech & Asset Man Gmbh|METHOD AND DEVICE FOR DRYING CRYSTALLINE CARBOXYLIC ACIDS|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP53068260A|JPS5811418B2|1978-06-08|1978-06-08|
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