• 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:
    A process for preparation of glycols in which the vapor remaining after the partial condensation of a conventional ethylene oxide stripper overhead vapor stream is contacted with an aqueous solution of ethylene carbonate to recover ethylene oxide. No water need be removed from the enriched ethylene carbonate stream. Carbon dioxide is added and ethylene carbonate is formed by reaction at about 50 to 200°C and 5 to 150 kg/cm2 gauge in the presence of a suitable catalyst, preferably about 0.5-20 wt % of an organic phosphonium halide. After stripping off unreacted components, the ethylene carbonate is hydrolyzed to glycols in the presence of the same carbonation catalyst and at temperatures in the range of about 100 to 200°C and pressures of about 5 to 150 kg/cm2 gauge. Optionally, ethylene oxide and ethylene carbonate may be co-produced.
    公开号:SU1731041A3
    申请号:SU843778492
    申请日:1984-08-01
    公开日:1992-04-30
    发明作者:Бхайс Виджей；Гильман Гарольд
    申请人:Проусес Рисеч Энд Дивелопмент Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to dihydric alcohols, specifically to an improved method for the production of ethylene glycol, which is widely used in the industry of organic synthesis in the manufacture of varnishes, polyesters, lubricants and other purposes.
    A known method of producing ethylene glycol by hydrolysis of ethylene carbonate is that ethylene carbonate is mixed with water, carbon monoxide and potassium carbonate as a catalyst to form a homogeneous liquid mixture, which is fed to the reaction zone, where hydrolysis is performed at a temperature above 100 ° C and under pressure, then carbon dioxide is removed from the reaction mass, the catalyst is separated in a mixture with these
    W
    ethylene glycol lexarbonate, unreacted ethylene carbonate in a mixture with a catalyst is returned to the mixing stage.
    The purpose of the invention is to increase the yield of the target product due to the maximum absorption of almost the entire amount of ethylene oxide and water achieved through an intermediate product of the reaction - ethylene carbonate.
    The goal is achieved in that according to the method, a stream containing 77.8% ethylene oxide, 13.7% water, 5.7% carbon dioxide, obtained by reacting ethylene with molecular oxygen in the vapor phase over a supported silver catalyst, followed by washing the reaction product containing ethylene oxide, ethylene, carbon dioxide and water, with a recirculating water stream to absorb ethylene oxide, stripping the latter in the first vapor-liquid contact column from the resulting enriched water stream the phases, followed by partial condensation of an ethylene oxide-containing vapor stream, separating the condensed liquid from this stream and returning said liquid as reflux to the first contact column, is mixed with a vapor stream containing 15% ethylene oxide, 58% carbon dioxide and 27% water, with their molar ratio is 5: 4 and is subjected to absorption in the second contact column with an aqueous solution containing 9.5% water, 80.3% ethylene carbonate, ethylene glycol and a catalyst, with a molar ratio of vapor stream: water stream equal to 1: 5.1 , at a pressure of 1.2 kg / cm, carbon dioxide in a molar ratio of 1: 6.6 is added to the bottom stream from the column and the mixture is reacted at a temperature of 170 ° C and a pressure of 35 kg / cm in the presence of 0.8% triphenylphosphonium iodide, removing desorption at a temperature of 165-170 ° C and a pressure of 1.5 kg / cm from the resulting reaction mixture unreacted ethylene oxide and carbon dioxide, to the solution obtained after desorption of ethylene carbonate was added 1.6 mol per 1 mol of ethylenecarbonate and hydrolysis is carried out at a temperature of 180 ° C and pressure of 10 kg / cm.
    FIG. 1 shows a flow chart implementing the proposed method (in the form of a flowchart); in fig. 2 is a flow chart illustrating one embodiment of the invention.
    The block diagram (Fig. 1) shows the means for extracting ethylene carbonate, which
    is a possible complement to the basic process of making glycols. Ethylene and a source of oxygen are fed to reactor 10, the production of ethylene oxide, in which these
    the components react with the formation of ethylene oxide as a result, and a catalyst is used — silver supported on a support carrier. The reaction conditions here are typical for
    0 processes of this technology: temperature (approximately 200-400 ° C, pressure in the range of 10-40 kg / cm2 (according to the manometer). In one pass, the conversion of ethylene is equal to 1-20% (into ethylene oxide), and the remaining
    Part 5 is separated from ethylene oxide and recycled to the reactor. The ethylene concentration in the stream entering the reactor is approximately, the oxygen concentration is 5-15%, and the remaining part of the stream fed to the reactor consists of various inert gases and its composition depends in particular on the type of oxygen source used in the reactor. this particular system. The gases leaving the reactor contain
    5 minor amounts of ethylene oxide, which absorb (12) using a recirculating aqueous solution in a conventional absorption tower. Unabsorbed gases are recycled to the reactor.
    0 after the removal of carbon dioxide and any other blowing gases or inert gases (as necessary). The rich absorbent is fed to a stripping column 14, in which at higher temperatures and
    5, under reduced pressures, ethylene oxide is released. In accordance with the proposed process, this ethylene oxide is processed into ethylene glycols through an intermediate product, ethylene carbonate. The stripping column aqueous solution is recycled to the ethylene oxide absorber. The water resulting from this reaction, which is a by-product, is discharged from
    5 of this recycle stream, Despite the fact that in FIG. Figure 1 does not show that the vapors from the upper part of the stripping columns partially condense and the liquid fraction is returned to the stripping0 column in the form of reflux, this process takes place when implementing the proposed method.
    Alternatively, a portion of the fluid may be directed to improve the process.
    5 extraction of ethylene oxide and its purification. The vapor separated after the partial condensation process contains ethylene oxide, which is further processed in accordance with the invention. These gases are then subjected to absorption (16) by
    a recirculating aqueous stream containing ethylene carbonate, ethylene glycol and a catalyst, and the absorption process is carried out in a conventional vapor-liquid contact tower. Further, these gases are fed directly to the carbonization reactor 18, in which, in the presence of a suitable catalyst, preferably in the presence of an organic phos- phony halogen, ethylene oxide is converted into ethylene carbonate. The carbon dioxide required to carry out this reaction can be obtained from various sources,
    In cases where ethylene carbonate is used to produce ethylene glycols, carbon dioxide is decomposed during the hydrolysis reaction and it can be recycled to the carbonation reactor from the hydrolysis reactor 20. The product obtained in the carbonization reactor 18 is then fed to the hydrolysis reactor 20 and water is added. The catalyst used for the carbonation reaction is also used for the hydrolysis reaction. In cases where the ethylene carbonate is the desired product, it can be recovered by distillation from stream 19, which could otherwise be sent to the hydrolysis step. After the hydrolysis reaction is carried out, the glycols are fed to an extraction unit 22, in which the glycols are separated and purified by means of a distillation process.
    Details of the technological scheme of the proposed process and the composition of each of the blocks of the scheme shown in FIG. 1 is shown in FIG. 2
    The effluent from the ethylene oxide reactor is scrubbed in the tower (120) with a recirculating water stream (121) and then processed by a stripping process in the tower (140). As shown in FIG. 2, water can be discharged (141) from the recirculating water stream (121) after separation of the oxide / ethylene by a stripping process. Partial condensation of the stream (142). Ethylene oxide (140), coming out of the top of the stripping column, removes a significant amount of water by condensation. This water is returned to the stripping column (140) via conduit (143) and removed by discharge (141).
    If necessary, part or all of the fluid flow can be diverted to an ethylene oxide extraction unit. The amounts of water that passes with the ethylene oxide vapor (144) from the separator are in proportions that are highly suitable for both carbonization reactions and hydrolysis reactions. By adjusting the temperature of the refrigerator, it is possible to achieve a regime in which the vapor stream (144) contains about 50-95 mol% ethylene oxide and 5-50 mol% water. This stream is fed to an ethylene oxide scrubber (160), which may be a conventional tower for vapor-liquid contact, in
    0 where this stream moves in a countercurrent mode with respect to the aqueous stream (161) containing ethylene carbonate, ethylene glycol and a catalyst from the scrubber (170) of ethylene carbonate for the purpose of absorbing oxide
    5 ethylene. The operating conditions in the scrubber (160) are as follows: the temperature in the upper part is 35-45 ° C and in the lower part about 45-75 ° C with the average pressure in the scrubber 1-2 kg / cm (gauge). In those
    In cases where the scrubber operates in the adiabatic mode, the temperature in the lower part is higher than the temperature in the upper part, but alternatively, cooling can be arranged to control the temperature in the lower part of the scrubber.
    A liquid stream containing ethylene oxide is then fed to an ethylene carbonate reactor (180), in which, at a temperature in the range of 50–200 ° C and a pressure in the range of not approximately 5–75 kg / cm, ethylene oxide is reacted with carbon dioxide to form ethylene carbonate, in the presence of a suitable catalyst for this purpose. Since water is present in minor amounts, ethylene glycol is also formed. The catalyst is introduced into the ethylene carbonate reactor (180) as part of the stream (181), which is extracted during the purification process of ethylene carbonate. Carbon dioxide enters in large quantities from the hydrolysis reactor (200), in which ethylene carbonate reacts with water to form ethylene glycol. The product obtained from the ethylene glycol production reactor (201) is then fed to an instant evaporator (202), in which the bulk of the carbon dioxide is separated, which is then switched and recycled through the pipeline (203), as shown in FIG. 2. Fresh carbon dioxide is fed through a pipeline (171) from a source that is not covered by the proposed process and this carbon dioxide
    5 is fed to the lower part of the stripping column (170) of ethylene carbonate and recycled to the ethylene carbonate scrubber (160) via pipeline (172) or compressed and fed to the reactor (18U) and ethylene carbonate via pipeline (173).
    As shown in Fig. 2, low boiling point compounds are cooled and returned to the reactor (180), but some of these compounds can be dropped into the scrubber (160).
    The ethylene carbonate formed in the reactor (180) is recovered by passing the product stream (182) to a stripping column of ethylene carbonate (170), as shown in FIG. 2. At this time, any gas present is returned to the ethylene carbonate scrubber (160). If it is necessary to obtain ethylene carbonate, then this product can be recovered by distillation (not shown).
    The entire stream of ethylene carbonate obtained (or its part) produced in the reactor (180) is fed to the reactor (200) for hydrolysis through the pipeline (174). The hydrolysis process is carried out at a temperature in the range of about 100-200 ° C and a pressure in the range of about 5-75 kg / cm (according to a manometer). This process is carried out in the presence of a catalyst used for the production of ethylene carbonate. About 1-5 mol of water per 1 mol of ethylene carbonate should be used in this process. The ethylene glycols are separated by flash evaporation in an apparatus (202), while separating the heavy materials and the catalyst for subsequent recycling through the conduit (181). The resulting product, glycols, is fed through a pipeline (204) to a conventional distillation unit (not shown in Fig. 2), which separates monoethylene glycol from higher glycols, and also purifies these products.
    The following example relates to a typical implementation of the proposed process, shown in FIG. 2, but it does not consider the step of recovering ethylene carbonate as such.
    Example. A steam flow, in an amount of 1000 mol / h, supplied through a pipeline (144) from a stripping column of ethylene oxide, containing 77.8% ethylene oxide, 13.7% water and 5.7% carbon dioxide (the rest is inert substances and a small amount by-products), is mixed with the stream supplied through a pipeline (172) from a stripping column (170) of ethylene carbonate (the amount of this stream is 800 mol / h). This stream consists of 15% ethylene oxide, 58% carbon dioxide and 27% water. The mixed steam stream is scrubbed with the help of a 9660 mol / h water stream coming through a pipeline (161) and containing 9.5% water, 80.3% ethylene carbonate. 9.2% monoethylene glycol, 1.0% heavy glycols and catalyst. Steam discharged through the pipeline (162) from the top of the scrubber (160) contains 510 mol / h of carbon dioxide, as well as inert substances entering through the pipeline (144). The tower (160) works
    with a pressure of about 1.2 kg / cm (according to the manometer). The temperature of the liquid discharged from the bottom of the tower (160) is about 48 ° C and this temperature is controlled. Steam entering the pipeline (163)
    0 is fed to the ethylene carbonate reactor (180) in an amount of 10.924 mol / h. The composition of this pair is as follows: 8.2% ethylene oxide, 11.6% water, 71.0% ethylene carbonate, 8.1% monoethylene glycol, and the remaining with
    Part 5 consists of heavy glycols and a catalyst.
    In the reactor (180) at a pressure of 35 kg / cm2 (according to a manometer) and a temperature of 170 ° C, fresh ethylene oxide reacts with 726.5
    0 mol / h of carbon dioxide when using 0.8% methyltriphenylphosphonium iodide as a catalyst. 52 mol / h of ethylene glycol are obtained. The flow of the resulting product is withdrawn through a pipe (182) and fed to a stripping column (170) of ethylene carbonate, in which, at a pressure of 1.5 kg / cm (gauge) and a temperature of 165-170 ° C, ethylene carbonate is subjected to stripping by 450 mol / h of dioxide
    0 carbon (171). The stripped liquid is recycled to the ethylene carbonate scrubber (160), with the exception of the finished product, which in the amount of 904 mol / h is sent to the reactor
    5 hydrolysis (200), in which at a pressure of 10 kg / cm2 (according to a manometer) and a temperature of 180 ° C, ethylene carbonate is subjected to hydrolysis to ethylene glycol using 1453 mol / h of water. The carbon dioxide released in this way is separated and cooled to produce condensate water vapor and ethylene glycol, which are recycled to the hydrolysis reactor, while carbon dioxide is recycled to the carbonization reactor through pipe (203). The finished liquid product from the reactor is obtained in the amount of 1313 mol / h. It consists of 38.6% water, 60.0% monoethylene glycol, 1.5% heavy glycols and a catalyst. This product is subjected to
    0 instant evaporation in the tank (202), from the upper part of which steam in the amount of 1273 mol / h, containing all the water, as well as the target product — monoethylene glycol and higher glycols, which are further fed to the purification unit (FIG. 2 is not shown), while heavy glycols and the catalyst are recycled to the ethylene carbonate production reactor (180).
    The proposed method allows to increase the yield of ethylene glycol due to the achievement of maximum absorption of almost the entire amount of ethylene oxide and water,
    权利要求:
    Claims (1)
    [1]
    DETAILED DESCRIPTION A method for producing ethylene glycol comprising hydrolyzing ethylene carbonate at elevated pressure and temperature in the presence of a catalyst, characterized in that, in order to increase the yield of the target product, the stream obtained by reacting ethylene with molecular oxygen in the vapor phase over a silver catalyst carrier followed by washing the reaction product containing ethylene oxide, ethylene, carbon dioxide and water, recycling the aqueous stream to absorb ethylene oxide, desorbing the oxide ethylene in the first vapor-liquid contact column from the obtained enriched aqueous stream as a vapor phase, followed by partial condensation of an ethylene oxide-containing vapor stream, separating the condensed liquid from this stream and returning the specified liquid as reflux to the first contact column, and containing 77.8% oxide ethylene, 13.7% water. 5.7% carbon dioxide, mixed with a vapor stream containing 15% ethylene oxide, 58% dioxide
    carbon and 27% water, at their molar ratio of 5: 4 and is subjected to absorption in the second contact column with an aqueous solution containing 9.5% water, 80.3% ethylene carbonate, ethylene glycol and a catalyst,
    at a molar ratio of steam flow: an aqueous stream of 1: 5.1, at a pressure of 1.2 kg / cm2, carbon dioxide in a molar ratio of 1: 6.6 is added to the bottom stream from the column and the mixture is reacted at a temperature of 170 ° C and a pressure of 35 kg / cm in the presence of 0.8% triphenylphosphonium iodide, removed by desorption at a temperature of 165–170 ° C and a pressure of 1.5 kg / cm from the resulting reaction mixture unreacted ethylene oxide and dioxide carbon, to the ethylene carbonate solution obtained after desorption is added 1.6 mol of water per 1 m ethylene carbonate and carried out
    hydrolysis at a temperature of 180 ° C and a pressure of 10 kg / cm.
    ten
    /
    / 6
    WITH
    with,
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    同族专利:
    公开号 | 公开日
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    申请号 | 申请日 | 专利标题
    US06/519,653|US4508927A|1983-08-02|1983-08-02|Preparation of glycols from ethylene oxide|
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