WO2011015000A1 - 多级氧化甲苯制备苯甲醛、苯甲醇的工艺及设备 - Google Patents

多级氧化甲苯制备苯甲醛、苯甲醇的工艺及设备 Download PDF

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WO2011015000A1
WO2011015000A1 PCT/CN2009/074678 CN2009074678W WO2011015000A1 WO 2011015000 A1 WO2011015000 A1 WO 2011015000A1 CN 2009074678 W CN2009074678 W CN 2009074678W WO 2011015000 A1 WO2011015000 A1 WO 2011015000A1
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Prior art keywords
toluene
oxidation
benzyl alcohol
benzaldehyde
reactor
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PCT/CN2009/074678
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English (en)
French (fr)
Inventor
郭灿城
罗伟平
刘连冲
刘强
邓伟
Original Assignee
Guo Cancheng
Luo Weiping
Liu Lianchong
Liu Qiang
Deng Wei
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Application filed by Guo Cancheng, Luo Weiping, Liu Lianchong, Liu Qiang, Deng Wei filed Critical Guo Cancheng
Publication of WO2011015000A1 publication Critical patent/WO2011015000A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
    • B01J31/18—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms
    • B01J31/1805—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms the ligands containing nitrogen
    • B01J31/181—Cyclic ligands, including e.g. non-condensed polycyclic ligands, comprising at least one complexing nitrogen atom as ring member, e.g. pyridine
    • B01J31/1815—Cyclic ligands, including e.g. non-condensed polycyclic ligands, comprising at least one complexing nitrogen atom as ring member, e.g. pyridine with more than one complexing nitrogen atom, e.g. bipyridyl, 2-aminopyridine
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
    • C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
    • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
    • C07C45/36—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in compounds containing six-membered aromatic rings
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
    • B01J2231/70—Oxidation reactions, e.g. epoxidation, (di)hydroxylation, dehydrogenation and analogues
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
    • B01J2531/02—Compositional aspects of complexes used, e.g. polynuclearity
    • B01J2531/0213—Complexes without C-metal linkages
    • B01J2531/0216—Bi- or polynuclear complexes, i.e. comprising two or more metal coordination centres, without metal-metal bonds, e.g. Cp(Lx)Zr-imidazole-Zr(Lx)Cp
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
    • B01J2531/02—Compositional aspects of complexes used, e.g. polynuclearity
    • B01J2531/0238—Complexes comprising multidentate ligands, i.e. more than 2 ionic or coordinative bonds from the central metal to the ligand, the latter having at least two donor atoms, e.g. N, O, S, P
    • B01J2531/0241—Rigid ligands, e.g. extended sp2-carbon frameworks or geminal di- or trisubstitution
    • B01J2531/025—Ligands with a porphyrin ring system or analogues thereof, e.g. phthalocyanines, corroles

Definitions

  • the invention relates to a process and a device for preparing benzaldehyde and benzyl alcohol by multi-stage oxidation of toluene.
  • 03118066. 3 discloses the method of selective catalytic air oxidation of toluene and substituted toluene to aldehyde and alcohol.
  • the reaction temperature is controlled at 140-160 °C and the reaction pressure is 0 under the condition of 2-10 atm air.
  • 1-lMPa one or more of ⁇ -oxybimetallic porphyrin and monometallic porphyrin similar in structure to biological enzyme or the above metal porphyrin and inorganic and organic polymers are physically or chemically formed.
  • the supported metalloporphyrin is used as a catalyst alone, and the catalyst concentration is 1-40 ppm.
  • the catalytic air oxidizes toluene to benzaldehyde and benzyl alcohol; the conversion of substituted toluene varies between 10-50%, and the substitution of benzaldehyde and substituted benzyl alcohol The rate varies between 60 and 90%.
  • this reaction is carried out in an oxidation reactor because the liquid phase reaction mixture contains toluene, water, benzaldehyde, benzyl alcohol, benzoic acid and other by-products, and the primary oxidation products benzaldehyde or benzyl alcohol may also occur.
  • An object of the present invention is to provide a process and apparatus for preparing benzaldehyde and benzyl alcohol from a multistage oxidation of toluene.
  • benzyl alcohol In order to effectively inhibit the oxidation of the primary oxidation products benzaldehyde, benzyl alcohol, further increase the conversion of toluene and substituted toluene; increase the selectivity of benzaldehyde and benzyl alcohol; and can achieve oxidation reaction, gas-liquid separation and in the same equipment Continuous production of purification, simplifying the operation steps.
  • the process for preparing benzaldehyde and benzyl alcohol by multi-stage oxidation of toluene comprises the following steps: (1) oxidation reaction: in a multi-stage oxidation reactor with a gas-liquid separator and a reaction separation system with a side-line fractionation column or a fractionation column system, Using 0.
  • the monometallic porphyrin or u-oxybimetallic porphyrin has the following structural features:
  • the metal atom M of the formula (I) is a transition metal atom Co or Cu, Ni, Zn, Ru ; the metal atom M in the formula (II) is Fe or Mn, Cr ; the metal of the formula (III)
  • the atom M 2 is Fe or Mn, Cr ; the ligand X in the formula (II) is acetic acid or acetylacetone, halogen, acid anion;
  • the substituent in the formula (I) (II) (III) is hydrogen Or a hydrocarbyl group, a decyloxy group, a hydroxyl group, a halogen, an amine group, an amino group, a nitro group.
  • the metal salt or oxide in the metal porphyrin mixed with the metal salt is a transition metal Cu or Zn, Fe,
  • the apparatus of the present invention comprises a multi-stage oxidation reactor and a gas-liquid separator and a reaction separation system comprising a fractionation column or a split column with side line feed.
  • the multi-stage oxidation reactor is constituted by 1-6 stirred reactors or bubbling reactors in series with an air distributor or any combination therebetween, and a temperature regulating device is provided on the multi-stage oxidation reactor.
  • the fractionation column or the fractionation column of the side line feed is a normal pressure or a negative pressure with a nitrogen protection device.
  • the fractionation column is formed by a plurality of simple fractionation columns by series, parallel or series and parallel combination.
  • the invention relates to a multi-stage oxidation process according to a metal porphyrin-catalyzed free radical cyclic coupling mechanism and characteristics of hydrocarbon air oxidation, and the metal porphyrin catalyzes the air oxidation toluene system to efficiently prepare the primary oxidation products benzaldehyde and benzyl alcohol.
  • the multi-stage oxidation process can effectively inhibit the oxidation of the primary oxidation products benzaldehyde and benzyl alcohol.
  • the timely extraction of the benzaldehyde and benzyl alcohol by the separation column system can avoid the transition oxidation in the reactor.
  • the present invention can significantly increase the conversion of toluene, and the toluene conversion rate can reach 95°/.
  • the selectivity of benzaldehyde and benzyl alcohol can also be improved, benzaldehyde and benzyl alcohol.
  • the selectivity is over 50%.
  • the reaction apparatus consisted of six reactors with a stirring and air distributor and two fractionation columns connected in series.
  • the bottom of the reaction kettle is stirred, and the reaction liquid overflowed from the upper part of the first stirred reactor is mixed with air and then passed to the bottom of the second stirred reactor, and the reaction liquid overflowed from the upper part of the second stirred reactor. After mixing with air, pass through a third stirred reactor, and so on.
  • the toluene flow rate was controlled so that the average residence time was 73 minutes, and the controlled air flow rate was such that the tail oxygen content did not exceed 5%.
  • the reaction mixture overflowing from the sixth stirred reactor enters the fractionation column. After separation, toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a third stirred reactor for secondary oxidation. The above process is continuously cycled.
  • the conversion of toluene was 95/.
  • the selectivity of benzaldehyde benzyl alcohol is 50/. .
  • the reaction apparatus consisted of three reactors with a stirring and air distributor and three fractionation columns connected in series.
  • the reaction apparatus consisted of a reaction vessel with a stirring and air distributor and two fractionation columns.
  • toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a stirred reaction vessel for secondary oxidation. The above process is continuously cycled.
  • the conversion of toluene was 97%, and the selectivity of benzaldehyde benzyl alcohol was 60%.
  • the reaction apparatus comprises five reactors with a stirring and air distributor and a fractionation column in series.
  • the toluene flow rate was such that the average residence time was 100 minutes and the controlled air flow rate was such that the tail oxygen content did not exceed 5%.
  • the reaction mixture overflowing from the fifth stirred reactor enters the fractionation column. After separation, toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a second stirred reactor for secondary oxidation. The above process continues Ring.
  • the conversion of toluene was 96%, and the selectivity of benzaldehyde benzyl alcohol was 55%.
  • the reaction apparatus comprises a bubble column reactor connected in series and a stirred reactor and three fractionation columns.
  • toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a first stirred reactor for secondary oxidation. The above process is continuously cycled.
  • the conversion of toluene was 95/.
  • the selectivity of benzaldehyde benzyl alcohol is 55/. .
  • the reaction apparatus comprises three reactors with a stirring and air distributor and three fractionation columns connected in series.
  • the air is passed through the gas distributor to the bottom of the first stirred reactor, and the reaction liquid overflowed from the upper part of the first stirred reactor is mixed with air and then passed to the bottom of the second stirred reactor, from the second stirring.
  • the reaction liquid overflowed from the upper portion of the reactor was mixed with air and passed through a third stirred reactor.
  • the temperature of the three reactors was controlled to be 200 ° C, 160 ° C, 130 ° C, and the toluene flow rate was controlled so that the average residence time was 120 minutes, and the air flow rate was controlled so that the tail oxygen content did not exceed 5%.
  • the reaction mixture overflowing from the third stirred reactor enters the fractionation column. After separation, toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a first stirred reactor for secondary oxidation. The above process is continuously cycled.
  • the conversion of toluene was 95 ° /.
  • Benzoaldehyde benzene The methanol selectivity was 51%.
  • the reaction apparatus comprises three reactors with a stirring and air distributor and three fractionation columns connected in series.
  • the % gas is passed through the gas distributor to the bottom of the first stirred reactor, and the reaction liquid overflowed from the upper part of the first stirred reactor is mixed with air and passed to the bottom of the second stirred reactor, from the second
  • the reaction liquid overflowed from the upper portion of the stirred reactor was mixed with air and passed through a third stirred reaction vessel.
  • the temperature of the three reactors was controlled to be 190 ° C, 175 ° C, 160 ° C, and the toluene flow rate was controlled so that the average residence time was 110 minutes, and the air flow rate was controlled so that the tail oxygen content did not exceed 5%.
  • the reaction mixture overflowing from the third stirred reactor enters the fractionation column. After separation, toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained.
  • the recovered toluene is mixed with toluene containing a metal porphyrin catalyst and passed through a first stirred reactor for secondary oxidation. The above process is continuously cycled.
  • the conversion of toluene was 95%, and the selectivity of benzaldehyde benzyl alcohol was 52%.
  • the reaction apparatus consisted of three reactors with a stirring and air distributor in series and two multi-side fractionation columns.
  • the % gas is passed through the gas distributor to the bottom of the first stirred reactor, and the reaction liquid overflowed from the upper part of the first stirred reactor is mixed with air and passed to the bottom of the second stirred reactor, from the second
  • the reaction liquid overflowed from the upper portion of the stirred reactor was mixed with air and passed through a third stirred reaction vessel.
  • the toluene flow rate was controlled so that the average residence time was 65 minutes, and the air flow rate was controlled so that the tail oxygen content did not exceed 5%.
  • the reaction mixture overflowing from the third stirred reactor enters the fractionation column. After separation, toluene, benzaldehyde, benzyl alcohol and pure benzoic acid were obtained. Recovered toluene and metal The toluene of the porphyrin catalyst was mixed into the first stirred reactor for secondary oxidation. The above process is continuously cycled. The conversion of toluene was 95 ° /. The benzaldehyde benzyl alcohol selectivity is 55 ° /. .

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Description

多级氧化甲苯制备苯甲醛、 苯甲醇的工艺及设备
技术领域
本发明涉及一种多级氧化甲苯制备苯甲醛、 苯甲醇的工艺及设备。
背景技术
03118066. 3 公开了本人申请的选择性催化空气氧化甲苯和取代甲苯成醛 和醇的方法.是在通入 2-10 atm空气条件下， 控制反应温度为 140- 160 °C， 反应 压强为 0. 1-lMPa条件下，选用与生物酶结构类似的 μ -氧双金属卟啉和单金属卟 啉的一种或者多种或上述金属卟啉与无机和有机高分子通过物理或化学方法构 成的固载金属卟啉单独作为催化剂， 催化剂浓度为 1-40 ppm， 催化空气氧化甲 苯成苯甲醛和苯甲醇； 取代甲苯转化率在 10-50%之间变化， 取代苯甲醛和取代 苯甲醇的收率在 60 ~ 90%之间变化。 但是这种反应是在一个氧化反应器中进行 的， 由于液相反应混合物中含有甲苯、 水、 苯甲醛、 苯甲醇、 苯甲酸和其它副产 物， 且初级氧化产物苯甲醛、苯甲醇还可能发生进一步的氧化； 造成产品的纯度 不太好， 甲苯和取代甲苯转化率仍不理想； 另外为了获得高纯度的苯甲醛、苯甲 醇， 必须另外采用其它设备对其进行精制处理和提纯， 操作较复杂。
发明内容
本发明的目的在于提供一种多级氧化甲苯制备苯甲醛、 苯甲醇的工艺及设 备。 以实现有效抑制初级氧化产物苯甲醛、苯甲醇的氧化， 进一步提高甲苯和取 代甲苯的转化率；提高苯甲醛和苯甲醇的选择性； 并可在同一套设备中实现氧化 反应、 气液分离和纯化的连续生产， 简化操作步骤。
多级氧化甲苯制备苯甲醛、 苯甲醇的工艺包括以下步骤- ( 1 ) 氧化反应： 在多级氧化反应器并带气液分离器及带侧线分馏塔或分馏 塔系构成的反应分离系统中， 使用 0. Γδθρριη单金属卟啉或 u-氧双金属卟啉单 独作为催化剂、 或者金属卟啉与邻苯二甲酰亚胺 （或盐）按重量比为 1 : 2CT100 的混合催化剂， 在反应温度为 8(T200°C， 将甲苯在多级氧化器中停留 6(Γ180分 钟催化氧化成苯甲醛和苯甲醇；
( 2 ) 气液分离和纯化： 氧化反应混合物进入气液分离器， 液相产物经带侧 线分馏塔或分馏塔系在负压或常压或在氮气保护下分离出苯甲醛、苯甲醇、苯甲 酸和部分甲苯及水的轻组分， 轻组分在分离出水后甲苯循环至氧化器继续反应； 气相部分经冷凝分离后将甲苯循环至氧化反应器继续氧化，不凝气体经处理后排 空。
所述的单金属卟啉或 u-氧双金属卟啉具有以下结构特点：
Figure imgf000003_0001
Figure imgf000003_0002
( II )
Figure imgf000004_0001
(ΠΙ) 通式（ I )的金属原子 M为过渡金属原子 Co或 Cu、 Ni、 Zn、 Ru; 通式（II )中的 金属原子 M为 Fe或 Mn、 Cr; 通式（III) 的金属原子 M2为 Fe或 Mn、 Cr; 通式（II ) 中的配位基 X为乙酸或乙酰丙酮、 卤素、 酸根负离子； 通式（I ) ( II ) (III)中取 代基 ， ， 为氢或烃基、 垸氧基、 羟基、 卤素、 胺基、 氨基、 硝基。
金属卟啉与金属盐混合催化剂中的金属盐或氧化物为过渡金属 Cu或 Zn、 Fe、
Co、 Mn、 Cr、 Ni的盐或氧化物。 本发明的设备由多级氧化反应器和气液分离器及带侧线进料的分馏塔或分 熘塔系构成的反应分离系统。
所述多级氧化反应器是由带空气分布器的 1-6个串联的搅拌反应釜或鼓泡反 应器或者它们之间的任意组合， 在多级氧化反应器上设有温度调节装置。
所述侧线进料的分馏塔或分馏塔系为常压或负压并带氮气保护装置。
所述分馏塔系是由多个简单分馏塔通过串联、 并联或串联与并联组合而成。 本发明是根据金属卟啉催化碳氢化合物空气氧化的自由基循环耦合机理和 特点提出的多级氧化工艺，金属卟啉催化空气氧化甲苯体系中能高效制备初级氧 化产物苯甲醛、苯甲醇， 采用多级氧化工艺能有效抑制初级氧化产物苯甲醛、苯 甲醇的氧化，利用分离塔系统及时提取生成的苯甲醛和苯甲醇能避免其在反应器 中发生过渡氧化。本发明与已有技术相比， 可显著提高甲苯的转化率， 经实验甲 苯转化率可达到 95°/。以上， 也可提高苯甲醛和苯甲醇的选择性， 苯甲醛和苯甲醇 选择性达 50%以上。
具体实施方案
以下结合实施例对本发明作进一步说明，但不能理解为对本发明保护范围的 限制。
实施例 1 :
反应设备包括依次串联的 6个带搅拌和空气分布器的反应釜和 2个分馏塔构 成。
生产工艺流程为： 在 19CTC下通入溶有 5ppm结构式 (III)的金属卟啉， R^Cl , R2= =H， M=Fe的甲苯， 将 10 atm空气经气体分布器通入第一个搅拌反应釜的底 部，由第一个搅拌反应釜上部溢流出来的反应液与空气混合后通入第二个搅拌反 应釜的底部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合后通过第三 个搅拌反应釜， 如此类推。控制甲苯流速使平均停留时间为 73分钟， 控制空气流 速使尾氧含量不超过 5%。从第六个搅拌反应釜溢流出来的反应混合物进入分馏塔 系。 经分离后得到甲苯、 苯甲醛、 苯甲醇和苯甲酸纯品。 回收的甲苯与含有金属 卟啉催化剂的甲苯混合通入第三个搅拌反应釜进行二次氧化。 上述过程连续循 环。 甲苯转化率 95/。,苯甲醛苯甲醇选择性为 50/。。
实施例 2 :
反应设备包括依次串联的 3个带搅拌和空气分布器的反应釜和 3个分馏塔构 成。
生产工艺流程为： 通入溶有 20ppii结构式（Π )的金属卟啉， R2= R3=H, M=Cr的甲苯， 将 11 atm空气经气体分布器通入第一个搅拌反应釜的底部， 由第一 个搅拌反应釜上部溢流出来的反应液与空气混合后通入第二个搅拌反应釜的底 部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合后通过第三个搅拌反 应釜。 控制三个反应釜温度分别为 190°C， 185°C , 180 °C , 控制甲苯流速使平均 停留时间为 73分钟，控制空气流速使尾氧含量不超过 5%。从第三个搅拌反应釜溢 流出来的反应混合物进入分馏塔系。经分离后得到甲苯、苯甲醛、苯甲醇和苯甲 酸纯品。回收的甲苯与含有金属卟啉催化剂的甲苯混合通入第一个搅拌反应釜进 行二次氧化。 上述过程连续循环。 甲苯转化率 95%,苯甲醛苯甲醇选择性为 56%。
实施例 3 :
反应设备由 1个带搅拌和空气分布器的反应釜和 2个分馏塔构成。
生产工艺流程为：通入溶有 10 ppii结构式 (III)的金属卟啉， R!=0CH3, R2= R3=H， M=Ni 及 120ppm的 N-羟基邻苯二甲酰亚胺的甲苯， 将 5 atm含氧 23%气体经气体分 布器通入搅拌反应釜的底部，控制反应釜温度为 90°C， 甲苯流速使平均停留时间 为 180分钟， 控制空气流速使尾氧含量不超过 5°/。。 从搅拌反应釜溢流出来的反应 混合物进入分馏塔系。 经分离后得到甲苯、 苯甲醛、 苯甲醇和苯甲酸纯品。 回收 的甲苯与含有金属卟啉催化剂的甲苯混合通入搅拌反应釜进行二次氧化。上述过 程连续循环。 甲苯转化率 97%，苯甲醛苯甲醇选择性为 60%。
实施例 4 :
反应设备包括依次串联的 5个带搅拌和空气分布器的反应釜和 1个分馏塔构 成。
生产工艺流程为： 在 190°C通入溶有 40 ppm结构式（II )的金属卟啉， RfCl , RL= R2= R3=H, M=Fe的甲苯， 将 9 atm空气经气体分布器通入第一个搅拌反应釜的 底部，由第一个搅拌反应釜上部溢流出来的反应液与空气混合后通入第二个搅拌 反应釜的底部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合后通过第 三个搅拌反应釜， 如此类推。 甲苯流速使平均停留时间为 100分钟， 控制空气流 速使尾氧含量不超过 5%。从第五个搅拌反应釜溢流出来的反应混合物进入分馏塔 系。 经分离后得到甲苯、 苯甲醛、 苯甲醇和苯甲酸纯品。 回收的甲苯与含有金属 卟啉催化剂的甲苯混合通入第二个搅拌反应釜进行二次氧化。 上述过程连续循 环。 甲苯转化率 96%,苯甲醛苯甲醇选择性为 55%。
实施例 5 :
反应设备包括依次串联的 1个鼓泡塔反应器和 1个搅拌反应釜和 3个分馏塔构 成。
生产工艺流程为： 在 100 °C通入溶有 15 ppm结构式（ I )的金属卟啉， R1= R2= R3=H, M=Co及 200 ppn的 N-羟基邻苯二甲酰亚胺的甲苯， 将 10 atm空气经气体分 布器通入鼓泡塔反应釜的底部，由鼓泡塔反应釜上部溢流出来的反应液与空气混 合后通入搅拌反应釜的底部。 控制甲苯流速使平均停留时间为 150分钟， 控制空 气流速使尾氧含量不超过 5%。 从搅拌反应釜溢流出来的反应混合物进入分馏塔 系。 经分离后得到甲苯、 苯甲醛、 苯甲醇和苯甲酸纯品。 回收的甲苯与含有金属 卟啉催化剂的甲苯混合通入第一个搅拌反应釜进行二次氧化。 上述过程连续循 环。 甲苯转化率 95/。，苯甲醛苯甲醇选择性为 55/。。
实施例 6 :
反应设备包括依次串联的 3个带搅拌和空气分布器的反应釜和 2个分馏塔构 成。
生产工艺流程为：通入溶有 25ppm结构式（ II )的金属卟啉， R Cl , R1= R2= R3=H， M=Mn及 lOOppm的 Co (0AC) 2的甲苯， 将 12 atm空气经气体分布器通入第一个搅拌反 应釜的底部，由第一个搅拌反应釜上部溢流出来的反应液与空气混合后通入第二 个搅拌反应釜的底部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合后 通过第三个搅拌反应釜。 控制三个反应釜温度分别为 200°C , 160°C , 130°C , 控 制甲苯流速使平均停留时间为 120分钟， 控制空气流速使尾氧含量不超过 5%。 从 第三个搅拌反应釜溢流出来的反应混合物进入分馏塔系。经分离后得到甲苯、苯 甲醛、苯甲醇和苯甲酸纯品。回收的甲苯与含有金属卟啉催化剂的甲苯混合通入 第一个搅拌反应釜进行二次氧化。上述过程连续循环。 甲苯转化率 95°/。，苯甲醛苯 甲醇选择性为 51%。
实施例 7 :
反应设备包括依次串联的 3个带搅拌和空气分布器的反应釜和 2个分馏塔构 成。
生产工艺流程为： 在 190°C下通入溶有 2 ppm结构式（I )的金属卟啉， R2=0H， R: = R3=H, M=Cu的甲苯， 将 15 atm含氧 17%气体经气体分布器通入第一个搅拌反 应釜的底部，由第一个搅拌反应釜上部溢流出来的反应液与空气混合后通入第二 个搅拌反应釜的底部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合后 通过第三个搅拌反应釜。 控制三个反应釜温度分别为 190°C， 175°C， 160 °C , 控 制甲苯流速使平均停留时间为 110分钟， 控制空气流速使尾氧含量不超过 5%。 从 第三个搅拌反应釜溢流出来的反应混合物进入分馏塔系。经分离后得到甲苯、苯 甲醛、苯甲醇和苯甲酸纯品。回收的甲苯与含有金属卟啉催化剂的甲苯混合通入 第一个搅拌反应釜进行二次氧化。上述过程连续循环。 甲苯转化率 95%，苯甲醛苯 甲醇选择性为 52%。
实施例 8 :
反应设备包括依次串联的 3个带搅拌和空气分布器的反应釜和 2个带多侧线 分馏塔构成。
生产工艺流程为：在 190°C下通入溶有 8 Ppm结构式（ΠΙ)的金属卟啉， R1=N02, R2= H， R3=Br, M=Mn的甲苯， 将 8 atm含氧 25%气体经气体分布器通入第一个搅拌 反应釜的底部，由第一个搅拌反应釜上部溢流出来的反应液与空气混合后通入第 二个搅拌反应釜的底部，从第二个搅拌反应釜上部溢流出来的反应液与空气混合 后通过第三个搅拌反应釜。控制甲苯流速使平均停留时间为 65分钟，控制空气流 速使尾氧含量不超过 5%。从第三个搅拌反应釜溢流出来的反应混合物进入分馏塔 系。 经分离后得到甲苯、 苯甲醛、 苯甲醇和苯甲酸纯品。 回收的甲苯与含有金属 卟啉催化剂的甲苯混合通入第一个搅拌反应釜进行二次氧化。 上述过程连续循 环。 甲苯转化率 95°/。,苯甲醛苯甲醇选择性为 55°/。。

Claims

权 利 要 求 书
1. 多级氧化甲苯制备苯甲醛、苯甲醇的工艺，其特征在于，包括以下步骤：
( 1 )氧化反应： 是在多级氧化反应器并带气液分离器及带侧线分馏塔或分 馏塔系构成的反应分离系统中， 使用 0. δθρριη单金属卟啉或 U-氧双金属卟啉 单独作为催化剂、或者金属卟啉与邻苯二甲酰亚胺（或盐）按重量比为 1 : 20^100 的混合催化剂， 在反应温度为 80~200°(， 将甲苯在多级氧化器中停留 6(Γ180分 钟催化氧化成苯甲醛和苯甲醇；
(2)气液分离和纯化： 氧化反应混合物进入气液分离器， 液相产物经带侧 线分馏塔或分馆塔系在负压或常压或在氮气保护下分离出苯甲醛、苯甲醇、苯甲 酸和部分甲苯及水的轻组分， 轻组分在分离出水后甲苯循环至氧化器继续反应； 气相部分经冷凝分离后将甲苯循环至氧化反应器继续氧化，不凝气体经处理后排 空。
2. 一种权利要求 1所述工艺的专用设备， 其特征在于， 由多级氧化反应器和 气液分离器及带侧线进料的分馏塔或分馏塔系构成的反应分离系统。
3. 根据权利要求 2所述的专用设备， 其特征在于， 所述多级氧化反应器是由 带空气分布器的 1-6个串联的搅拌反应釜或鼓泡反应器或者它们之间的任意组 合， 在多级氧化反应器上设有温度调节装置。
4. 根据权利要求 2所述的专用设备， 其特征在于， 所述侧线进枓的分馏塔 或分馏塔系为常压或负压并带氮气保护装置。
5. 根据权利要求 2所述的专用设备， 其特征在于， 所述分馏塔系是由多个 简单分馏塔通过串联、 并联或串联与并联组合而成。
9
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CN103130639B (zh) * 2011-11-23 2014-12-10 中国石油化工股份有限公司 单塔侧线精馏分离苯甲酸、苯甲醛、甲苯的方法
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