Research On FCC Refining Hydrogenation To Jet Fuel Catalyst And Process

As the world's conventional crude oil reserves are decreasing,the heavy and poor quality of crude oil is becoming more and more serious.In recent years,the progress of unconventional oil resource extraction has accelerated,making the proportion of heavy crude oil in refineries significantly increased.Therefore,the high-value processing of crude oil is bound to be the focus and hotspot of research in the petroleum refining industry.Unlike foreign refineries that use hydrogenation technology as the main secondary processing method of petroleum,FCC technology is widely used in China's refineries,and in addition to producing liquefied gas,catalytic gasoline and diesel fuel,catalytic cracking technology can also produce large quantities of refining oil.Among them,refining oil usually refers to the raw material that passes through the FCC and passes into the rectification tower below the diesel fraction to above the slurry fraction.Normally,the refining oil needs to be returned to the catalytic cracking unit for secondary reaction,which will cause the load of the raw material preheating furnace,reactor and fractionation tower to increase,and ultimately reduce the economic and environmental protection of the catalytic cracking unit.In addition,due to the vigorous development of China's aviation industry,the demand for aviation kerosene in China is very high and will continue to increase.If aviation kerosene can be prepared by FCC refining and hydrogenation,it can solve the shortage of China's aviation kerosene to a certain extent and achieve FCC high-value conversion and utilization of refining oil.In this thesis,first,a single carrier is used to evaluate the hydrogenation saturation performance of FCC refining oil products,and a suitable hydrogenation saturation catalyst carrier is determined.Then,a single carrier is mixed with a HY type molecular sieve with a silicon-aluminum ratio of 50,and the compound The crystal form,acidity,pore data and morphology of the carrier are analyzed and characterized,and the hydrogenation saturation performance is tested to obtain the best ratio of the compound carrier;secondly,the active compound component loaded on the preferred compound carrier is catalyzed by FCC to refining the oil Evaluation of hydrogenation saturation performance,in which the active components are selected from the combination of Mo,W in Group VIB and Co,Ni in Group VIII,and two transition metals are loaded in combination to obtain a supported dual active component hydrogenation catalyst.Analyze the four-component yield of hydrogenated oil,gaschromatography simulated distillation,and elemental composition and distribution to determine the hydrogenation saturation performance of the supported dual active component hydrogenation catalyst,and obtain a suitable active component combination ratio and load the amount.Finally,the process conditions for obtaining a prolific kerosene fraction were determined and evaluated.At a reaction temperature of 360 ?,a reaction hydrogen initial pressure of 8 MPa,and a reaction time of 1 h,the catalyst could achieve the maximum hydrogenation effect and more output The capacity of kerosene fractions,and the saturation fraction of generated oils increased by 21.39%,the aromatic fraction decreased by 15.87%,and the yield of kerosene fractions was 11.10%.In the analysis of the final product oil,it was found that heavy aromatics such as tricyclic,tetracyclic,and pentacyclic decreased by 37.79%,light aromatics decreased by 2.21%,and alkanes increased by 28.32%,and 10.32%hydroanthracenes were generated,Hydrophenanthrenes,Hydrofluorenes and other products.After the 140-240 ? fraction of the refined oil is separated,all the indexes of the fraction are higher than the kerosene fraction of the raw oil,and all the indexes conform to the No.3 jet fuel national standard.