催化热解废轮胎对于资源利用及环境保护具有重要意义,近年来引起人们关注.在废轮胎胶粉热解反应中加入催化剂,不仅会加速胶粉裂解速率,缩短反应时间,而且可以通过催化剂择形催化改变产物分布,从而提高目的产物衍生油的收率和性能.国内外对废轮胎催化热解已做了大量研究,以期提高衍生油中高附加值单环芳烃的含量,同时降低S,N和Cl含量,虽然已取得较大进展,但衍生油收率较低,大大降低了该技术的可行性.本文采用带搅拌器的1000 mL不锈钢反应器,在常压条件下研究了反应温度和催化剂类型对废轮胎胶粉热解反应及产物衍生油性能的影响,通过元素分析、馏程模拟和色谱-质谱等表征手段检测了衍生油的理化性能.结果表明,在废轮胎胶粉热解反应过程中,随反应温度上升,出油速率先增加后降低.至500℃时,热解衍生油收率最高达55.65 wt%,所得衍生油呈黑棕色,具有轻质油含量低、S和N含量高、粘度低和流动性好的特点,其轻质芳烃含量低,却含有大量可以转变为芳烃的脂肪烃类.因此,为了提高衍生油中轻质油和轻质芳烃收率,降低S和N含量,尽量维持较高的衍生油收率,在热解反应过程中引入少量ZSM-5,USY,β,SAPO-11和ZSM-22等常见催化剂,利用催化剂独特的孔道结构和酸分布,达到定向催化和转化的目的,提高轻质芳烃含量.同时,为了克服催化剂与胶粉难以接触进行反应的问题,在反应温度升至200℃时,维持一定时间保证胶粉发生溶胀和液化反应形成液体烃类,使得催化剂不仅能够均匀分散于液体烃中与其接触进行反应,而且有效提高了反应物料与催化剂之间传质传热效率,使得裂解反应在均相中进行,降低因传热不均匀而造成的结焦和过度裂化反应.在催化热解过程中,1.0 wt%催化剂的加入可明显缩短反应时间,在保证衍生油收率基本不变的情况下,获得的衍生油呈黄棕色,轻质油收率较高为70–75 wt%,S和N含量分别降至0.3–0.58wt%和0.78–1.0 wt%.以具有较高酸性和孔径分布的ZSM-5,USY,β和SAPO-11为催化剂时,衍生油中总芳烃含量可达到50 wt%,其中单环芳烃含量高达45 wt%. Catalytic pyrolysis of waste tires for the use of resources and environmental protection is of great significance in recent years has drawn people’s attention in waste tire rubber powder pyrolysis reaction added catalyst will not only accelerate the rate of cracking rubber powder, shorten the reaction time, and can be selected by the catalyst Shaped catalyst to change the distribution of the product so as to improve the yield and performance of the derivative oil of the target product.There have been a lot of studies on the catalytic pyrolysis of waste tires both at home and abroad in order to improve the content of the highly added monocyclic aromatic hydrocarbons in the derivative oil and to reduce the S, N And Cl content, although the progress has been made, but the yield of derivative oil is lower, which greatly reduces the feasibility of the technology.In this paper, a 1000 mL stainless steel reactor with a stirrer was used to study the reaction temperature and Catalyst type on the pyrolytic reaction of the waste tire rubber and the properties of the product derivative oil, the physical and chemical properties of the derivatized oil were tested by means of elemental analysis, distillation range simulation and chromatography-mass spectrometry, etc. The results showed that in the pyrolysis of waste tire rubber powder, During the reaction, as the reaction temperature increases, the oil yield first increases and then decreases, and at 500 ° C, the yield of pyrolysis derivatized oil is up to 55.65 wt%, and the derived oil is dark brown , With the characteristics of low light oil content, high S and N content, low viscosity and good fluidity, but with low light aromatic content but a large amount of aliphatic hydrocarbons that can be converted into aromatics, therefore, The yields of light oil and light aromatics are reduced, the S and N contents are reduced, the higher yield of derived oil is maintained, and a small amount of ZSM-5, USY, β, SAPO-11 and ZSM-22 are introduced during the pyrolysis reaction Catalyst to utilize the unique pore structure and acid distribution of the catalyst to achieve the purpose of directional catalysis and conversion and increase the content of light aromatic hydrocarbon.At the same time, in order to overcome the problem that the catalyst is difficult to be contacted with the rubber powder to react, when the reaction temperature is raised to 200 DEG C, Maintain a certain period of time to ensure the occurrence of swelling and liquefaction reaction of the powdered rubber to form liquid hydrocarbons so that the catalyst can not only be uniformly dispersed in liquid hydrocarbons and come into contact with the liquid hydrocarbons for reaction but also effectively increase the mass transfer efficiency between the reaction materials and the catalyst, In a homogeneous phase to reduce coking and overcracking caused by uneven heat transfer In the catalytic pyrolysis process, the addition of 1.0 wt% catalyst can significantly shorten the reaction time, to ensure the yield of derivative oil Under the same conditions, the derived oil is yellowish brown, with a higher light oil yield of 70-75 wt% and a reduced S and N content of 0.3-0.58 wt% and 0.78-1.0 wt%, respectively, When ZSM-5, USY, β and SAPO-11 with higher acidity and pore size distribution were used as catalyst, the total aromatic content in the derived oil could reach 50 wt% and the content of monocyclic aromatic hydrocarbons in it could reach 45 wt%.