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Process for the production of hydroaromatic hydrocarbons from coal tar and coal tar fractions and products therefrom

机译:由煤焦油和煤焦油馏分及其产物生产氢芳烃的方法

摘要

Coal tar, coal tar fractions and aromatic hydrocarbons derived from coal tar are hydrogenated in two stages, the first using a sulphur-resistant catalyst at 350-450 DEG C. and a hydrogen partial pressure of 0.5-70 atmospheres to destructively hydrogenate sulphur compounds and hydrogenate part of the aromatic hydrocarbons, the second being a non-destructive, complete hydrogenation of the product entirely in the vapour phase at 200-500 DEG C. and 20-100 atmospheres hydrogen partial pressure using a catalyst consisting of one or more Group 8 metals. The coal tar fractions used may comprise mixtures of aromatic hydrocarbons with partially hydrogenated derivatives, paraffins, olefins, and naphthenes. The first stage may be effected in liquid, vapour or mixed phase, continuously or batchwise. Catalysts include molybdates and thiomolybdates, supported or not, especially cobalt molybdate on alumina. The hydrogen partial pressure used increases with the complexity of the sulphur compounds present. The exit gas may be re-used after removal of H2S. The products are treated, if necessary, to remove H2S and completely hydrogenated in the second stage as in Specification 761,755. Excess hydrogen from each stage may be recycled. In examples: (1) sublimed naphthalene is desulphurized by hydrogenation at 375 DEG C. and 32 atmospheres using cobalt molybdate, and the product vaporized in hydrogen at 300 DEG C. and 32 atmospheres in the presence of nickel on kieselguhr to yield decahydronaphthalene; (2) a 200-280 DEG C. coal tar fraction freed of tar acids and bases is similarly desulphurized but at 410 DEG C., and then hydrogenated, after a caustic soda wash, to yield naphthenes; (3) a 300-380 DEG C. fraction is similarly treated, first at 410 DEG C. and 42 atmospheres, and then at 300-330 DEG C. and 32 atmospheres, the product then being recycled to the second stage at 360-370 DEG C. and 55 atmospheres; (4) a 120-200 DEG C. fraction is treated first at 410 DEG C. and 20 atmospheres, then at 270-280 DEG C. and 30 atmospheres.
机译:煤焦油,煤焦油馏分和衍生自煤焦油的芳烃分两个阶段进行氢化,第一阶段使用抗硫催化剂在350-450℃和氢气分压为0.5-70个大气压下破坏性地氢化硫化合物和使用一种或多种第8组的催化剂,在200-500℃和20-100个大气压的氢分压下,部分氢化芳烃的一部分,第二部分是完全在气相中将产物完全进行无损氢化。金属。所用的煤焦油馏分可包含芳族烃与部分氢化的衍生物,链烷烃,烯烃和环烷烃的混合物。第一步可以在液相,气相或混合相中连续或分批进行。催化剂包括或不负载的钼酸盐和硫代钼酸盐,特别是氧化铝上的钼酸钴。所使用的氢分压随所含硫化合物的复杂性而增加。去除H2S后可以重新使用出口气体。如果需要,可以对产品进行处理,以去除H2S,并在第二阶段按照761,755规范进行完全氢化。每个阶段多余的氢气可以循环使用。在实施例中:(1)将升华的萘用钼酸钴在375℃和32个大气压下通过氢化脱硫,并将产物在硅藻土上在镍存在下在300℃和32个大气压下在氢中汽化,得到十氢化萘; (2)将不含焦油酸和碱的200-280℃的煤焦油馏分同样地脱硫,但在410℃下进行脱硫,然后在苛性苏打洗涤后氢化,得到环烷烃; (3)对300-380℃的馏分进行类似的处理,首先在410℃和42个大气压下,然后在300-330℃和32个大气压下,然后将产物在360-200℃下再循环到第二阶段。 370℃和55个大气压; (4)首先在410℃和20个大气压下处理120-200℃的馏分,然后在270-280℃和30个大气压下处理。

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