WO2003101938A1 - Procede d'oxamidination de composes carbonyle - Google Patents

Procede d'oxamidination de composes carbonyle Download PDF

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Publication number
WO2003101938A1
WO2003101938A1 PCT/CN2003/000423 CN0300423W WO03101938A1 WO 2003101938 A1 WO2003101938 A1 WO 2003101938A1 CN 0300423 W CN0300423 W CN 0300423W WO 03101938 A1 WO03101938 A1 WO 03101938A1
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silicon
catalyst
liquid
silicate
added
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PCT/CN2003/000423
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English (en)
French (fr)
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WO2003101938A8 (fr
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Wei Wu
Bin Sun
Yongxiang Li
Shibiao Cheng
Enquan Wang
Shuzhong Zhang
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China Petroleum & Chemical Corporation
Research Institute Of Petroleum Processing, Sinopec
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Priority to DE60328693T priority Critical patent/DE60328693D1/de
Priority to JP2004509632A priority patent/JP4574348B2/ja
Priority to AU2003246098A priority patent/AU2003246098A1/en
Priority to EP03737834A priority patent/EP1541548B1/en
Publication of WO2003101938A1 publication Critical patent/WO2003101938A1/zh
Publication of WO2003101938A8 publication Critical patent/WO2003101938A8/zh

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C251/00—Compounds containing nitrogen atoms doubly-bound to a carbon skeleton
    • C07C251/32—Oximes
    • C07C251/34—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals
    • C07C251/48—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals with the carbon atom of at least one of the oxyimino groups bound to a carbon atom of a six-membered aromatic ring
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C249/00—Preparation of compounds containing nitrogen atoms doubly-bound to a carbon skeleton
    • C07C249/04—Preparation of compounds containing nitrogen atoms doubly-bound to a carbon skeleton of oximes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C251/00—Compounds containing nitrogen atoms doubly-bound to a carbon skeleton
    • C07C251/32—Oximes
    • C07C251/34—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals
    • C07C251/36—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals with the carbon atoms of the oxyimino groups bound to hydrogen atoms or to acyclic carbon atoms
    • C07C251/38—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals with the carbon atoms of the oxyimino groups bound to hydrogen atoms or to acyclic carbon atoms to carbon atoms of a saturated carbon skeleton
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C251/00—Compounds containing nitrogen atoms doubly-bound to a carbon skeleton
    • C07C251/32—Oximes
    • C07C251/34—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals
    • C07C251/42—Oximes with oxygen atoms of oxyimino groups bound to hydrogen atoms or to carbon atoms of unsubstituted hydrocarbon radicals with the carbon atom of at least one of the oxyimino groups bound to a carbon atom of a ring other than a six-membered aromatic ring
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/06—Systems containing only non-condensed rings with a five-membered ring
    • C07C2601/08—Systems containing only non-condensed rings with a five-membered ring the ring being saturated
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
    • C07C2601/14—The ring being saturated

Definitions

  • the present invention relates to an ammoximation method of a carbonyl compound. Background technique
  • the reaction between carbonyl compounds and hydroxylamines is the main method for the synthesis of corresponding oxime compounds.
  • cyclohexanone oxime is a key intermediate for the production of ⁇ -caprolactam
  • ⁇ -caprolactam is an important organic chemical raw material, mainly used as a synthetic fiber and engineering plastics (such as nylon- 6) monomer.
  • About 91% of caprolactam is produced industrially via the cyclohexanone oxime route, the cyclohexanone-hydroxylamine process. This process is not only complex process, long production process, high equipment investment, but also due to the generation or use of N0 X, S0 X, etc. exist more serious corrosion and pollution problems.
  • Patents EP 0208311, EP 0267362, EP 0496385, EP 0564040, etc. have successively reported a new method for preparing cyclohexanone oxime from cyclohexanone with ammonia and hydrogen peroxide in a one-step ammoximation reaction under the catalysis of titanium silicon molecules.
  • the method has mild reaction conditions, high yields of target products, and has the characteristics of simple process, low equipment investment, three wastes, and environmental friendliness.
  • amoximation reaction of cyclohexanone reported in EP 0347926 is based on titanium oxide supported on silicon oxide, which also has good catalytic performance; J. Le Bars et al. In Appl. Catal. A 136 ( 1996) P69 and P. Wu et al. In J. Catal. 168 (1997) P. 400 also reported other types of molecular sieves containing Ti (mainly silica), such as Ti-ZSM-48, ⁇ - ⁇ , Ti-MOR has good catalytic performance for the ammoximation of various aldehyde and ketone compounds.
  • EP 0496385 states that during the reaction, it is necessary to periodically remove the deactivated catalyst and replenish it with fresh catalyst to maintain the desired catalyst activity.
  • USP5498793 discloses a method for preparing an oxime from a carbonyl compound, hydrogen peroxide, and ammonia.
  • a cocatalyst is added to the reaction system to improve the yield and conversion of the amidoximation reaction of the carbonyl compound.
  • the carbonyl compounds described in this patent are acetophenone, cyclododecanone, and the co-catalyst is amorphous silica.
  • the cocatalyst did not solve the problem of deactivation of the main catalyst.
  • the method for preparing an oxime by using a carbonyl compound, hydrogen peroxide and ammonia disclosed in CN1345718A is to add a co-catalyst containing an acidic solid to the reaction system to increase the ammoximation conversion rate of the carbonyl compound.
  • the acidic solid co-catalyst added to this method does not solve the problem of deactivation of the main catalyst.
  • An object of the present invention is to provide a method for the ammoximation of a carbonyl compound that delays the deactivation process of the catalyst, extends the stable operation time of the catalyst, and improves the recovery rate of the catalyst.
  • the method of the present invention comprises reacting a liquid-phase reaction system containing a carbonyl compound, ammonia and hydrogen peroxide in the presence of a silicon-containing catalyst, and is characterized in that a liquid silicon-containing auxiliary agent is added to the reaction system to make the system 1 ⁇ : L 0000 ppm, Preferably the silicon concentration reaches the dissolved equilibrium concentration of silicon in the solution.
  • the carbonyl compound is selected from the group consisting of cyclohexanone, acetone, acetophenone, cyclopentanone, acetophenone, p-hydroxyacetophenone, cyclododecanone, furfural, benzophenone, and p-methylbenzaldehydekind of.
  • the silicon-containing catalyst refers to a silicon-containing molecular sieve or a metal-supported silicon oxide catalyst, wherein the silicon-containing molecular sieve may be in the form of a molecular sieve powder or a shaped form.
  • the molecular sieves titanium-silicon molecular sieves are preferred, such as TS-1, TS-2, Ti-ZSM-5, Ti-ZSM-12, and Ti-ZSM-8 Ti- ⁇ , Ti-MCM-41, or Ti-M0R, etc.
  • TS-1 molecular sieve having MFI crystal structure is more preferable.
  • the silicon-containing catalyst is an amorphous silicon oxide or a silicon-containing molecular sieve of different structure
  • the silicon oxide structure is dissolved and can reach an equilibrium concentration in the ammonia-containing medium, but the equilibrium concentration value may vary with the composition of the medium It varies within a wide range (0.1 to several thousand ppm).
  • the inventors have unexpectedly found that if a liquid silicon-containing substance is added to the reaction system, the substance can be preferentially dissolved in the reaction system, while the silicon-containing catalyst is hardly dissolved.
  • the liquid silicon-containing auxiliary agent may be in a liquid form such as a sol, a solution, a suspension, or an emulsion.
  • This liquid-type silicon-containing auxiliary agent may be preferentially used in the reaction system. Is dissolved so that the silicon-containing catalyst is hardly dissolved.
  • the liquid silicon-containing auxiliary agent is not limited to the gas, liquid, and solid forms of the raw materials, as long as the silicon-containing raw materials are added to the system in a liquid form such as a sol, a solution, a suspension, or an emulsion. Just fine.
  • the liquid silicon-containing auxiliary agent is preferably a liquid form of a sol or a solution.
  • the silicon-containing auxiliary agent is selected from various types of inorganic silicon-containing substances or various types of organic silicon-containing substances, the inorganic silicon-containing substances include silicon oxide or silicate, and the silicates include sodium silicate, silicon Potassium acid, aluminum silicate, etc .;
  • the organic silicon-containing substance is selected from silicate or silane, and the silicate is preferably ethyl silicate.
  • the added amount of the liquid silicon-containing auxiliary agent should be such that the silicon content in the reaction solution is between 0.1 and 10,000 ppm, and it is preferable to add the silicon content in the reaction solution to its dissolution equilibrium concentration Of the added amount.
  • the composition of the reaction system such as solvent, ammonia concentration, etc.
  • the equilibrium concentration of silicon in the system will change.
  • the dissolved equilibrium concentration of silicon is 1000 to 3000 ppm.
  • the liquid silicon-containing auxiliary agent in the method provided by the present invention may be added in a continuous or intermittent manner, and among them, it is preferably added in a continuous manner.
  • the ammoximation method of a carbonyl compound provided by the present invention is based on the dissolution rule of silicon in an alkaline solution.
  • a step of adding a liquid silicon-containing auxiliary agent is used, which can suppress the catalyst.
  • the dissolution of silicon on the catalyst slows down the destructive effect of ammonia on the catalyst, maintains a stable catalyst concentration in the system, reduces catalyst deactivation caused by the dissolution of silicon in the catalyst, prolongs the catalyst life, and improves stable operation time.
  • the analysis and characterization results of TS-1 molecular sieve after operation show that compared with the fresh agent, its crystallinity and Ti content No change has occurred; for systems without the addition of silicon-containing additives or systems containing only silicon-containing substances in solid form, the deactivator after operation is due to the dissolution of silicon in the molecular sieve, and Ti remains on the molecular sieve As a result, the relative Ti content on the molecular sieve increases, and the crystallinity of the molecular sieve also decreases.
  • the titanium-silicon molecular sieve (TS-1) used was produced by Yueyang Jianchang Co., Ltd .; cyclohexanone (purity ⁇ 99.5%) was provided by Beijing Chemical Plant, hydrogen peroxide (containing H 2 0 2 27.5 wt%) supplied by Tianjin Dongfang Chemical Plant; ammonia (purity ⁇ 99.9%) supplied by Beijing Provided by the test chemical plant; tert-butanol (containing 86.5 wt% tert-butanol, the rest is water and a small amount of impurities) provided by Beijing Pingshun Chemical Co., Ltd .; silica sol is the product of Qingdao Ocean Chemical Plant; unless otherwise specified, all other chemical reagents are Products from Beijing Chemical Plant are chemically pure.
  • the composition of the reaction product was analyzed by a gas phase colorimetric method, and the conversion rate of hydrogen peroxide was obtained by measuring its content by the iodometric method.
  • the Ti content in the catalyst and the silicon content in the reaction system were determined by inductively coupled plasma emission spectroscopy (ICP).
  • the crystallinity of the molecular sieves was measured by X-ray diffraction (XRD).
  • This embodiment is a process for preparing cyclohexanone oxime by the cyclohexanone ammoximation, and the catalyst is titanium silicon (TS-1) molecular sieve powder.
  • the volume of the reaction kettle was 150ml, magnetically stirred, and heated in an oil bath.
  • the reaction raw materials and reaction products continuously enter and exit the reactor, and the molecular sieve is pulled and intercepted in the reaction kettle.
  • Example 1 was repeated, except that no silica sol was added. The reaction results are shown in Table 1. Comparative Example 2
  • Example 1 was repeated, except that the silicon-containing auxiliary agent was not continuously added during the reaction, but the acidic silica gel solid was added all at once, and the dosage ratio of the catalyst to the catalyst (TS-1) was 0.4: 1, and the reaction results are shown in Table 1.
  • Example 2
  • Example 1 was repeated, except that toluene was used as a solvent instead of tert-butanol, an aqueous solution of ethyl orthosilicate (Beijing Chemical Reagent Co., Ltd.) was added, and the silicon content in the reaction solution was 1035 ppm.
  • the reaction results are shown in Table 1.
  • Example 1 was repeated, except that the reaction temperature was 83 ⁇ 1. C, the reaction pressure is 0.3Mpa, the catalyst concentration is 2.0% by weight, the molar ratio of H 2 0 2 to cyclohexanone is 1.08: 1, and the silicon content in the reaction solution is 100 ppm.
  • the reaction results are shown in Table 2.
  • the stable running time of the catalyst is calculated based on the one-way running time of the cyclohexanone conversion rate of ⁇ 97%. Comparative Example 3
  • Example 3 was repeated, except that no silicon-containing auxiliary agent was added. The results are shown in Table 2.
  • Examples 4 to 7 were acetone, cyclopentanone, benzaldehyde, Methylbenzaldehyde is a raw material of carbonyl compounds, and is reacted with ammonia and hydrogen peroxide in an ammoximation reaction. Water is used as a solvent, and a silica sol is added.
  • the average residence time of the material is 120min.
  • the reaction temperature is 60 ⁇ 1 TC
  • the pressure is normal pressure.
  • the activity and selectivity of the catalyst are not affected, the conversion rate is above 90%, and the selectivity is between 95 and 99.5%.
  • the stable running time of the catalyst Compared with the operation time without adding silica sol, there is a significant extension, and the catalyst recovery rate is above 96% by weight.
  • a Ti-supported silicon oxide catalyst (the preparation method is the same as that of EP0347926 Example 6) was used to perform the reaction of cyclohexanone with ammonia and hydrogen peroxide, and the process conditions were the same as those of Example 1. After the silica sol was added, the activity and selectivity of the catalyst were not affected, but the stable running time of the catalyst was extended by 30% compared with the time when the silica sol was not added, and the catalyst recovery was 97% by weight.

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  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Description

羰基化合物的氨肟化方法 技术领域
本发明是关于羰基化合物的氨肟化方法。 背景技术
羰基化合物是指含有 >C=0官能团的化合物， 如醛类和酮类化合物， 羰基化合物和羟胺反应是合成相应的肟化合物的主要方法。
以环己酮肟的合成为例， 环己酮肟是生产 ε -己内跣胺的关键中间 体， 而 ε -己内酰胺是重要的有机化工原料， 主要用作合成纤维和工程 塑料（如尼龙- 6)的单体。 工业上约 91 %的己内酰胺是经过环己酮肟 路线生产的，即环己酮 -羟胺工艺。 此过程不仅工艺复杂、生产流程长、 设备投资高， 而且因产生或使用 N0X、 S0X等而存在较严重的腐蚀和污 染问题。
八十年代初， 意大利 Taramas so在 USP4410501中， 公开了一种新 型催化材料-钛硅分子筛， 它对烃、 醇、 酚等具有很好的选择性氧化 作用 （EP 0230949 , USP4480135 , USP4396783 ) ， 它应用于苯酚氧化 制苯二酴已实现了工业化。
专利 EP 0208311、 EP 0267362、 EP 0496385、 EP 0564040等相继 报道了在钛硅分子歸催化下， 由环己酮与氨、 过氧化氢进行氨肟化反 应一步制备环己酮肟的新方法。 该方法反应条件温和、 目标产物收率 高， 而且具有工艺过程简单、 装置投资少、 三废少、 对环境友好等特 点。
此外， EP 0347926 报道的环己酮的氨肟化反应， 是以负载于氧化 硅上的氧化钛为催化剂，同样具有较好的催化性能； J. Le Bars等在 Appl . Ca tal. A 136 (1996) P69和 P. Wu等在 J. Catal. 168 (1997) P. 400 中还 报道了含 Ti 的其它类型分子筛 （均以氧化硅为主） ， 如 Ti-ZSM-48、 Π-β、 Ti-MOR 等对多种醛、 酮化合物的氨肟化反应， 均具有较好的催 化性能。
随着对环己酮氨肟化制备环己酮肟反应研究的逐步深入， 各种含 钛催化剂， 主要是钛硅分子筛在该反应中的失活问题也越来越引起关 注。
EP 0496385 中 4艮道认为在反应过程中， 需采用定期取出失活催化 剂并补充新鲜剂的方法， 才能维持理想的催化剂活性。
USP5498793公开了一种由羰基化合物、 过氧化氢和氨制备肟的方 法， 是采用在反应体系中加入共催化剂的手段， 以提高羰基化合物的 氨肟化反应收率和转化率。 该专利中所述的羰基化合物为苯乙酮、 环 十二碳酮， 共催化剂为无定形氧化硅。 但共催化剂并未解决主催化剂 失活的问题。
CN1345718A公开的羰基化合物、 过氧化氢和氨制备肟的方法， 是 采用在反应体系中加入含有酸性固体的共催化剂的手段， 以提高羰基 化合物的氨肟化转化速率。 但是该方法所加入的酸性固体共催化剂， 并未解决主催化剂失活的问题。
G. Petr ini等在 Stud. Surf. Sci. Catal. 68 (1991) P. 761 中， 对环 己酮氨肟化反应中钛硅分子薛的失活原因进行了较为详细的分析， 认 为引起钛硅分子筛的失活原因有三个： （1 )分子筛中硅溶解、 （2 ) 骨架钛迁移和（3 )副产物堵孔。 前两个原因都是由氨引起的， 由于氨 的存在， 反应体系呈碱性， 分子筛上的硅便会溶解下来。 由于硅溶解 流失， 而 Ti 仍留存于催化剂上， 造成催化剂上相对 Ti含量增加， 分 子筛结晶度也呈下降趋势。 该文进一步指出， 虽然在反应物流中只溶 有很少量的硅（ppm级） ， 但在长周期运转的过程中， 硅溶解会导致 反应体系中分子筛数量在不断减少， 回收催化剂重量低于起始添加的 催化剂重量， 在极端条件下， 催化剂回收率仅 35%。
在 Select ive Oxidat ion by Heterogeneous Catalys i s ( 2001， P112 )一书中， 也提到氨引起的分子筛的硅溶解是造成环己酮氨肟化 反应中催化剂失活的首要因素。 由于氨是环己酮氨肟化反应中必不可 少的原料， 由其引起的问题不可避免。 这一问题虽已被证实， 但却未 见报道相应的解决办法。 在其它醛、 酮的氨肟化反应体系也存在类似 的问题。
上面所述的羰基化合物氨肟化反应中， 由于催化剂中硅溶解流失， 会造成催化剂稳定运转时间缩短和催化剂回收率下降的不利影响， 但 是， 虽然氨引起的分子筛的硅溶解是催化剂失活的首要因素， 但是向 体系中加入如 CN1345718A中所述的酸性固体， 如固体的硅胶却并不能 解决催化剂失活问题。 发明内容
本发明的目的是针对现有技术中的不足， 提供一种延緩催化剂失 活进程， 延长催化剂稳定运转时间， 提高催化剂回收率的羰基化合物 的氨肟化方法。
本发明的方法包括使包含羰基化合物、 氨和过氧化氢的液相反应 体系在含硅催化剂存在下反应，其特征在于， 在反应体系中加入了一种 液态的含硅助剂， 使体系中的硅浓度达到 0. 1〜： L 0000 ppm, 优选硅浓 度达到溶液中硅的溶解平衡浓度。
所说的羰基化合物选自环己酮、 丙酮、 曱乙酮、 环戊酮、 苯乙酮、 对-羟基苯乙酮、 环十二碳酮、 糠醛、 苯曱醛和对甲基苯甲醛中的一种。
所说的含硅催化剂是指含硅分子筛或负载金属的氧化硅催化剂， 其中所说的含硅分子筛可以是分子筛原粉的形式或经成型的形式。 所 说的分子筛中优选钛硅分子筛， 如 TS - 1、 TS - 2、 Ti - ZSM - 5、 Ti - ZSM - 12 > Ti-ZSM- 8 Ti-β, Ti - MCM - 41或 Ti- M0R等， 其中更优选 具有 MFI晶体结构的 TS - 1分子筛。
含硅催化剂无论是无定形的氧化硅还是不同结构的含硅分子筛， 在含氨介庸中均存在氧化硅结构被溶解且能达到一平衡浓度的现象， 但随介质组成不同该平衡浓度值可在很大范围（0. 1 ~数千 ppm)内变 化。 本发明人意外地发现， 若在反应体系中加入液态的含硅物质， 则 该物质可在反应体系中优先被溶解， 而含硅催化剂几乎不被溶解。
在本发明提供的方法中， 所说的液态的含硅助剂， 可以为溶胶、 溶液、 悬浮液或乳浊液等液态的形式， 这种液态形式的含硅助剂可在 反应体系中优先被溶解， 从而使含硅催化剂几乎不被溶解。 所说的液 态的含硅助剂并不限定其原料的气、 液、 固形态， 只要这种含硅的原 料在加入体系时是以溶胶、 溶液、 悬浮液或乳浊液等的液态形式加入 即可。 所说的液态的含硅助剂优选溶胶或溶液的液态形式。
所说的含硅助剂选自各类无机含硅物质或各类有机含硅物质， 所 说的无机含硅物质包括氧化硅或硅酸盐， 所说的硅酸盐包括硅酸钠、 硅酸钾、 硅酸铝等； 所说的有机含硅物质选自硅酸酯或硅烷， 所说的 硅酸酯优选硅酸乙酯。
在本发明提供的方法中， 所说的液态的含硅助剂的添加量应使反 应液中的硅含量在 0. 1 - 10000 ppm, 优选加入后使反应液中硅含量达 到其溶解平衡浓度的添加量。 由于随反应体系组成（如溶剂、 氨浓度 等） 的不同， 体系中硅的平衡浓度会变化， 例如在溶剂为叔丁醇-水 的反应体系中， 硅的溶解平衡浓度在 10 - l OOppm之间； 而在水的反应 体系中， 硅的溶解平衡浓度为 1000 ~ 3000ppm。 另外， 本发明提供的 方法中所说的液态的含硅助剂可以以连续或间歇的方式进行添加， 其 中优选以连续方式进行添加。
本发明提供的羰基化合物的氨肟化方法， 是根据硅在碱性溶液中 的溶解规律， 在羰基化合物的氨肟化反应中， 采用了添加液态的含硅 助剂的步骤， 这样可以抑制催化剂上的硅溶解， 减緩氨对催化剂的破 坏作用， 维持体系中稳定的催化剂浓度， 减少由催化剂中硅溶解造成 的催化剂失活， 延长催化剂寿命， 提高了稳定运转时间。 从以 TS - 1 分子筛催化的环己酮氨肟化反应为例， 采用本发明提供的方法， 运转 后的 TS - 1 分子筛的分析表征结果看， 与新鲜剂相比， 其结晶度、 Ti 含量均未发生变化；而对于未添加含硅助剂的体系或者只是添加了固体 形式的含硅物质的体系， 运转后的失活剂则由于分子筛中硅的溶解流 失、 Ti 仍留存于分子筛上， 造成分子筛上相对 Ti 含量的增加， 分子 筛结晶度也呈下降趋势。 具体实施方式
下面通过实施例对本发明做进一步说明。
在实施例和对比例中， 所用的钛硅分子筛 （TS - 1 ) 由岳阳建长股 份公司生产； 环己酮 （纯度≥99. 5% ) 由北京化工厂提供， 双氧水（含 H202 27. 5 重量％) 由天津东方化工厂提供； 氨（纯度≥99. 9% ) 由北京 试验化工厂提供；叔丁醇（含叔丁醇 86.5重量％，其余为水及少量杂质） 由北京平顺化工有限公司提供； 硅溶胶为青岛海洋化工厂产品； 如不 作特别说明， 其它化学试剂都采用北京化工厂产品， 化学纯。
实施例中， 反应产物用气相色镨法分析组成， 过氧化氢的转化率 通过碘量法测定其含量得到。 催化剂中 Ti的含量和反应体系中硅含量 通过电感耦合等离子体发射光谱（ICP)测定。 分子筛的结晶度通过 X -衍射光谱（XRD)测定。 实施例 1
本实施例为环己酮氨肟化制备环己酮肟的过程， 催化剂为钛硅（TS - 1 )分子筛原粉。
反应釜体积 150ml， 磁力搅拌， 油浴加热。 反应原料及反应产物 连续进出反应器， 分子筛被拉截在反应釜内。
工艺参数如下为 H202： 环己酮 = 1.10 ： 1(摩尔比）， 氨： 环己 酮 = 1.70 ： 1(摩尔比）， 叔丁醇： 环己酮 == 3.30 ： 1(摩尔比）， 反 应液中硅含量 = 35 ppm, 催化剂浓度为 1.8重量％ ， 物料平均停留时 间为 72min， 反应温度为 76±1V, 反应压力为常压， 添加硅溶胶， 连 续加入。反应结果见表 1，其中催化剂稳定运转时间以环己酮转化率≥97 %的单程运转时间计。 对比例 1
重复实施例 1， 不同之处在于不添加硅溶胶。 反应结果见表 1。 对比例 2
重复实施例 1, 不同之处在于反应时没有连续添加含硅助剂， 而是 一次性加入酸性硅胶固体， 其与催化剂 （TS- 1 )用量比为 0.4: 1， 反 应结果见表 1。 实施例 2
重复实施例 1， 不同之处在于： 以甲苯代替叔丁醇作溶剂， 添加正 硅酸乙酯 （北京化学试剂公司 ） 水溶液， 反应液中硅含量 1035ppm。 反应结果见表 1。 实施例 3
重复实施例 1,不同之处在于：反应温度 83±1。C，反应压力 0.3Mpa, 催化剂浓度为 2.0 重量％， H202与环己酮摩尔比 1.08: 1， 反应液中硅 含量 100 ppm。 反应结果见表 2， 其中催化剂稳定运转时间以环己酮转 化率≥97 %的单程运转时间计。 对比例 3
重复实施例 3， 不同之处在于：不添加含硅助剂。 反应结果见表 2。
表 1 编 号 对比例 1 对比例 2 实施例 实施例 2
1 含硅助剂种类 酸性硅胶 硅溶胶 正硅酸 固体 乙酯 反应结果
环己酮转化率 ％ 98. 5 98. 5 98. 6 98. 5
H202转化率 % 100 100 100 100 酮对环己酮肟选择性 °/。 99. 6 99. 6 99. 7 99. 5
H202对环己酮肟选择性 ％ 89. 2 89. 2 89. 4 89. 1 催化剂稳定运转时间 h 40 42 65 60 催化剂回收率 （焙烧） , 重量％ 87. 7 88. 5 98. 7 97. 8 催化剂表征结果
Ti含量（相对新鲜剂） ％ 106. 8 106. 0 99. 5 101. 1 结晶度（相对新鲜剂） ％ 99 99 100 100
表 2
Figure imgf000009_0001
从表 1和 2可以看出， 添加含硅的溶胶或溶液以后， 催化剂 的活性、 选择性均未受影响， 而稳定运转时间相比对比例有明 显延长， 催化剂回收率大于 97重量％; 失活催化剂与新鲜剂相 比， 其结晶度、 Ti含量均未发生变化， 而对比例中，没有添加含 硅的溶胶或溶液（对比例 1、 3)或者仅仅含硅物质只是以固体形 式加入到体系中 （对比例 2 ), 其运转后得到的失活剂则由于分 子筛中硅的溶解流失、 Ti 仍留存于分子筛上， 造成分子筛上相 对 Ti含量的增加， 分子筛结晶度也呈下降趋势。
实施例 4 ~ 7
以 Ti -M0R(Si/Al = 300, 以 J. Catal.168 (1997) p.400 中记 载的方法制备）为催化剂， 实施例 4~ 7 分别是以丙酮、 环戊酮、 苯甲醛、 对甲基苯曱醛为羰基化合物原料与氨、 过氧化氢进行氨 肟化反应过程， 以水为溶剂， 添加硅溶胶。 反应工艺条件如下为 H202： 酮 （醛） - 1.15 ： 1 (摩尔比）， 氨 ： 酮 （醛） = 2.0 ： 1 (摩尔比）， 水： 酮 （醛） - 8 ： 1 (体积比） ， 催化剂浓度为 3.0 重量。 /。， 物料平均停留时间为 120min.， 反应温度为 60±1 TC , 压力为常压。
反应结果见表 3， 其中催化剂稳定运转时间以所用的酮或醛的 转化率≥90 %的单程运转时间计。
表 3
Figure imgf000010_0001
采用本发明提供的方法， 添加硅溶胶后， 催化剂的活性、 选 择性均未受影响， 转化率在 90%以上， 选择性在 95 ~ 99.5%， 从 表 3 可以看出， 催化剂的稳定运转时间同未添加硅溶胶的运转时 间相比有明显的延长， 且催化剂回收率在 96重量％以上。
实施例 8
采用负载 Ti 的氧化硅催化剂 （制备方法同 EP0347926 实施例 6 ) ， 进行环己酮与氨、 过氧化氢的反应， 工艺条件同实施例 1。 添加硅溶胶后， 该催化剂的活性、 选择性均未受影响， 但催化剂 的稳定运转时间较未添加硅溶胶的运转时间延长 30% , 催化剂回 收率为 97重量％。

Claims

权 利 要 求
1、 一种羰基化合物的氨肟化方法， 其中包括使包含羰基化合 物、 氨和过氧化氢的液相反应体系在含硅催化剂存在下反应， 其 特征在于， 在反应体系中加入了一种液态的含硅助剂， 使体系中 的娃浓度达到 0.1 - 10000 ppm。
2、 按照权利要求 1 所说的方法， 其特征在于所说的羰基化合 物选自环己酮、 丙酮、 曱乙酮、 环戊酮、 苯乙酮、 对-羟基苯乙酮、 环十二碳酮、 糠醛、 苯甲醛和对曱基苯甲醛中的一种。
3、 按照权利要求 1 所说的方法， 其特征在于所说的含硅催化 剂选自含硅分子 或负载金属的氧化硅催化剂。
4、 按照权利要求 3 所说的方法， 其特征在于所说的含硅分子 筛为钛硅分子筛。
5、 按照权利要求 4 所说的方法， 其特征在于所说的钛硅分子 筛选自 TS_ 1、 TS- 2、 Ti -ZSM - 5、 Ti - ZSM - 12> Ti-ZSM-48. Ti-β, Ti -MCM-41或 Ti - M0R中的一种。
6、 按照权利要求 3 所说的方法， 其特征在于所说的含硅分子 筛为分子筛原粉的形式或经成型的形式。
7、 按照权利要求 1 所说的方法， 其特征在于所说的含硅助剂 选自各类无机含硅物质或各类有机含硅物质。
8、 按照权利要求 7 所说的方法， 其特征在于所说的无机含硅 物质选自氧化硅或硅酸盐。
9、 按照权利要求 8 所说的方法， 其特征在于所说的硅酸盐选 自硅酸钠、 硅酸钾或硅酸铝。
10、 按照权利要求 7 所说的方法， 其特征在于所说的有机含 硅物质选自硅酸酯或硅烷。
11、 按照权利要求 10 所说的方法， 其特征在于所说的硅酸酯 为硅酸乙酯。
12、 按照权利要求 1 所说的方法， 其特征在于所说的液态的 含硅助剂的添加量应使反应液中的硅含量达到溶液中硅的溶解平 衡浓度。
1 3、 按照权利要求 1 所说的方法， 其特征在于所说的液态的 含硅助剂以连续或间歇的方式进行添加。
14、 按照权利要求 13 所说的方法， 其特征在于所说的液态的 含硅助剂以连续的方式进行添加。
1 5、 按照权利要求 1 所说的方法， 其特征在于所说的液态的 含硅助剂为硅溶胶或含硅溶液。
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