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    • 2. 发明授权
    • Method for the production of hydrocarbon resins
    • 生产烃树脂的方法
    • US4357450A
    • 1982-11-02
    • US254383
    • 1981-04-15
    • Kurt HandrickGeorg Kolling
    • Kurt HandrickGeorg Kolling
    • C08F4/00C08F2/00C08F4/06C08F240/00C08F110/00
    • C08F240/00
    • In a method for the production of hydrocarbon resins based upon pyrolysates through cationic polymerization of the pyrolyzate in the presence of Friedel-Crafts catalysts and solvents at temperatures between -40.degree. and +60.degree. C., tetralin and/or tetralin derivatives are pyrolysed at 660.degree.-710.degree. C., preferably at 675.degree.-690.degree. C., in the presence of 1-10 mol, preferably 3-7 mol, vaporous water per mole tetralin or tetralin derivative with a dwell time of 1-2 seconds; the pyrolyzate is distilled to free it of high boiling (tarry) portions; and the unsaturated compounds contained in the distillate are polymerized in known manner. Styrene formed during the pyrolysis is preferably removed through distillation before the polymerization. The hydrocarbon mixture regenerated with the separation of the resins formed through polymerization are hydrogenated to tetralin and/or tetralin derivatives and again pyrolyzed.
    • 在-40〜+ 60℃的温度下,在Friedel-Crafts催化剂和溶剂存在下通过热解物的阳离子聚合制备基于热解物的烃类树脂的方法,四氢化萘和/或四氢化萘衍生物在 660℃-710℃,优选675℃-690℃,在1-10摩尔,优选3-7摩尔蒸气水/摩尔四氢化萘或四氢化萘衍生物存在下,停留时间为1-2秒 ; 将热解物蒸馏以使其沸腾(焦油)部分释放; 馏出物中所含的不饱和化合物以已知的方式聚合。 在热解过程中形成的苯乙烯优选在聚合之前通过蒸馏除去。 通过聚合形成的树脂分离再生的烃混合物被氢化成四氢化萘和/或四氢化萘衍生物,并再次热解。
    • 5. 发明授权
    • Preparation of .beta.-isopropylnaphthalene
    • 制备β-异丙基萘
    • US4440957A
    • 1984-04-03
    • US289525
    • 1981-08-03
    • Kurt HandrickGeorg KollingPaul Kiedel
    • Kurt HandrickGeorg KollingPaul Kiedel
    • C07C2/66C07C1/00C07C2/70C07C5/22C07C5/27C07C15/24C07C67/00C07C2/68
    • C07C15/24C07C2/70C07C5/2745C07C2521/08C07C2527/173
    • Process of preparing .beta.-isopropylnaphthalene substantially free of corresponding .alpha.-isomer, in yields amounting to 90% and more by a continuous two-stage process comprising (1) alkylating naphthalene with propylene at a temperature of about 150.degree.-280.degree. C. under a pressure of 5 to 30 atm in the presence of a phosphoric acid catalyst supported on a SiO.sub.2 carrier and using a mol ratio of 1/5 to 1/20 mol propylene to 1 mol naphthalene to isopropylate 45 to 65% of the naphthalene and form a mixture of .alpha.- and .beta.-isopropylnaphthalene and then without separating off the unreacted naphthalene, (2) heating the isomeric mixture from stage (1) in the presence of a phosphoric acid catalyst supported on SiO.sub.2, to a temperature of 180.degree.-280.degree. C. under an inert gas pressure of 5 to 30 atm until no further .beta.-isopropylnaphthalene is formed and recovering said .beta.-isopropylnaphthalene from the isomerization mixture.
    • 通过连续两步法制备基本上不含相应α-异构体的β-异丙基萘的方法,其收率为90%以上,其包括(1)在约150℃-280℃的温度下将萘与丙烯烷基化, 在负载在SiO 2载体上的磷酸催化剂存在下,使用5〜30atm的压力,使用1/5〜1/20摩尔丙烯与1摩尔萘的摩尔比,将45〜65%的萘异丙酯化,形成 α和β-异丙基萘的混合物,然后不分离出未反应的萘,(2)在负载在SiO 2上的磷酸催化剂存在下,将阶段(1)的异构体混合物加热至180-280℃ 在5至30atm的惰性气体压力下进行,直至不再形成β-异丙基萘,并从异构化混合物回收所述β-异丙基萘。
    • 7. 发明授权
    • Processes for the continuous production of aromatic carboxylic acids by
oxidation with nitric acid of aromatic compounds containing oxidizable
acyclic substituents
    • 通过用含有可氧化的无环取代基的芳族化合物的硝酸氧化连续生产芳族羧酸的方法
    • US3979448A
    • 1976-09-07
    • US478395
    • 1974-06-11
    • Kurt HandrickAnton BenningDietrich GeorgeJurgen Schlegel
    • Kurt HandrickAnton BenningDietrich GeorgeJurgen Schlegel
    • C07C63/00C07C51/00C07C51/275C07C67/00C07C205/24C07C205/57C07C51/33
    • C07C51/275C07C205/24C07C205/57
    • Processes for the continuous production of aromatic carboxylic acids by reaction of nitric acid with an aromatic compound having an oxidizable alkyl or alkoxyalkyl substitutent which comprise mixing the aromatic compound in the form of small droplets with a large volume of dilute nitric acid having a concentration between 2 and 14% by weight of nitric acid that is maintained at a superatmospheric pressure between 15 and 80 atmospheres and at a temperature between 160.degree. and 230.degree.C, which processes comprise continuously passing a reaction mixture consisting of the aromatic compound and the dilute nitric acid through a series of at least three consecutively arranged vertical reactor column in each of which the ratio of the weight of the reaction mixture containing the dilute nitric acid to the weight of the aromatic compound is continuously maintained at at least 50:1, the nitric acid concentration in each of the reactor column being continuously maintained at an originally preselected concentration by the addition of amounts of more-concentrated nitric acid while aliquot portions of the aromatic compound based upon the number of vertical reactor columns in the series are continuously introduced into each of the reactor columns, the reaction zones each being maintained at an optimal oxidation temperature between 160 and 230.degree.C for the aromatic compound that is being oxidized, and continuously passing the reaction mixture into a final reactor column that is maintained at a higher temperature than the preceding series of reactor columns, and continuously discharging the reaction mixture containing between 10 and 20% by weight of the aromatic carboxylic acid thus produced from the final reactor column.
    • 通过硝酸与具有可氧化烷基或烷氧基烷基取代基的芳族化合物的反应连续生产芳族羧酸的方法,其包括将小液滴形式的芳族化合物与大体积的浓度为2 和14重量%的硝酸,其保持在15至80个大气压之间的超大气压力和160-230℃的温度,该方法包括连续通过由芳族化合物和稀硝酸组成的反应混合物 通过一系列至少三个连续排列的立式反应器塔,其中含有稀硝酸的反应混合物的重量与芳族化合物的重量的比例连续保持在至少50:1,硝酸 每个反应器塔中的浓度连续保持在原来的预选中 通过加入较多浓度的硝酸的浓度,同时将基于该系列中的垂直反应器塔的数量的芳族化合物的等分试样部分连续引入每个反应器塔中,每个反应区保持在最佳状态 氧化温度在160〜230℃之间,待氧化的芳族化合物,并将反应混合物连续通入保持在比上一系列反应器塔高的温度的最终反应器塔中,并连续排出含有 10至20重量%的由最终反应器塔产生的芳族羧酸。