The mercaptan in FCC gasoline can be removed and dienes can be reduced by sulfur etherification reaction of dienes and mercaptan in FCC gasoline.The investigation by laboratory testing of sulfur etherification using pre-hydrotreating catalyst for FCC gasoline was performed.The test results show that,for the FCC gasoline with 2.63 gI/(100g) dienes value,158 ppm mercaptan,680 ppm sulfur,the optimum reaction conditions are 130 ℃ temperature,5 hydrogen to oil ratio,3 h-1 space velocity and 2.0 MPa pressure.And the parameters optimization test results demonstrate that,under the optimum reaction conditions,the removal rate of dienes in FCC gasoline is 59%,the mercaptan removal rate is 97%,the RON loss is 0.2 units,and the olefin reduction is 0.3%.There is no change in total sulfur before and after pre-treatment of FCC gasoline.

The isohexane product of over 95% purity can be produced by hydrofining of reforming raffinate oil to remove olefins and aromatics followed by distillation to cut appropriate fraction. The process scheme developed is economically feasible. When the reforming raffinate oil is hydrofined with high-activity nickel catalyst with 30% ∼35% NiO prepared in the laboratory, the bromine number of hydrofined product is no greater than 5. 0 mgBr/(100 g), the maximum benzene content is 0. 001%. When the hydrogenated oil is distillated in the distillation unit with 24 theoretical plates to cut the isohexane, the high-purity isohexane of 60 ∼62. 5 °C distillation is obtained by utilizing small bottles to collect distillate products per 0.5 ∼Cfraction. Separation of high-purity fraction of isohexane products can be realized in the commercial units. The economic benefit of the aromatic extraction workshop can be improved if isohexane by-product production scheme is adopted.

分析了FCC汽油不同切割馏分的硫形态分布,对比汽油重馏分选择性加氢脱硫反应前后的硫形态分布变化,并考察了反应温度对加氢汽油中硫形态分布的影响.结果表明:FCC汽油中的硫主要分布在高沸点馏分中,且主要为C2～C4噻吩和苯并噻吩类；加氢反应后,汽油中的硫醇、四氢噻吩、苯并噻吩较易脱除,2-甲基噻吩和C2噻吩较难脱除；反应温度对FCC重汽油加氢产物硫形态分布具有重要的影响,温度高于265℃时,汽油脱硫率达到99％,加氢汽油中仅有少量的2-甲基噻吩和C2噻吩未被脱除,温度低于265℃时,汽油中硫化物的脱除率较低,并随反应温度的升高而增加.

以含K2O的Al2O3-TiO2复合物为催化剂载体,考察了浸渍液pH值、浸渍液浓度、浸渍时间和焙烧温度对Pd/Al2O3 -TiO2催化剂颗粒的蛋壳厚度、Pd粒子粒径等的影响.采用BET、TEM等方法对所制备的催化剂进行了表征,选择较佳制备条件的Pd/Al2O3-TiO2催化剂进行了C4馏分选择加氢活性评价.结果表明,随着浸渍液pH值的减小,催化剂颗粒的蛋壳厚度增加；浸渍溶液的浓度越高,浸渍时间越长,越有利于金属在催化剂内层的分布；浸渍液的pN值并不会影响Pd/Al2O3-TiO2催化剂Pd粒子最终的大小.催化剂焙烧温度越高,Pd粒子的平均直径越大,Pd的分散度越小.在反应温度40℃、压力1.5 MPa、体积空速8.0 h-1、氢/炔摩尔比2.5的条件下,较佳制备条件的Pd/Al2O3-TiO2催化剂催化C4馏分加氢的炔烃转化率73％、丁二烯选择性85％、丁二烯损失率2.5％.

The percent of alkene in hydrogented C_5 fraction by blending refine is less than 2%,which can be used as ethylene cracking feed.This paper tests the influence of different blending ratio of pyrolysis C_5 fractions on the performance of catalyst LY-9702/LY-9802 used in the second section hydrogenation of pyrolysis gasoline.The experimental results show that the suitable blending ratio of pyrolysis C_5 fractions is 5%-8%,and that the hydrogenated C_5 fractions was used as ethylene cracking feed,which can improve the yield of the double diene and the economic benefits.

分别采用浸渍法和混捏法对载体进行碱性助剂改性,再以浸渍法制备出Pd/Al2O3-TiO2催化剂；采用BET,XRD,Py-IR,NH3-TPD等方法对载体和催化剂进行表征；以含炔碳四馏分为原料,考察碱性助剂改性对Pd/Al2O3-TiO2催化剂选择性加氢活性和选择性的影响.结果表明:改性方法对载体的晶相结构没有影响,载体的XRD谱图均存在明显的锐钛矿和氧化铝特征峰；与浸渍法相比,混捏法改性载体的孔体积、平均孔径和最可几孔径较大,总酸量、中强酸量和强酸量较低,有助于提高加氢催化剂的选择性和稳定性.用混捏法改性载体制备催化剂的炔烃转化率为73％,丁二烯选择性为85％,丁二烯损失为2.5％,选择性高于未改性催化剂.

The tests on one-stage hydrogenation of cracked gasoline using catalyst Ni-1 were performed on a 500 mL adiabatic bed testing plant.The results demonstrated that the appropriate operating conditions were: 50 T inlet temperature,2.5-3.0 MPa operating pressure,1.5-2.5 h~(-1) space velocity of fresh oil,150-250 volumetric ratio of hydrogen to fresh oil and 2- 1-4:1 feed oil dilution ratio.The catalyst has been operated under these conditions for one operating cycle and diolefins is no greater than 2.0 g/(100 g).

The experiments for the alkylation of benzene with ethylene was performed in lab in order to decide a proper reaction conditions,the results showed that the reaction is firstly operated at a low space velocity for some hours and then shift to high space velocity,the activity stability of the beta zeolite catalyst will be improved remarkably. The analysis of physical chemistry characterization showed that the velocity of the carbon deposit in the pore was restrained and the passivation of acid sites was slowed down when the beta zeolite catalyst is first exposed to the lower air speed for some time.

The present invention relates to a low-grade diesel hydrogenation catalyst and a preparation method; the catalyst to W-Mo-Ni-P as the active component, an alkali metal, alkaline earth metal or rare earth metal-promoted, silica-alumina in the carrier, by weight percentage of alkali, alkaline earth or rare earth metal is 0.2 ~ 10%, WO3 was 5% ~ 25%, MoO3 was 8 ~ 20%, NiO of 2 ~ 9%, P of 1.0 to 5%, the balance being alumina oxide support; evaluation for catalytic cracking feedstock oil is a mixed oil and coker gas oil, the catalyst exhibits excellent activity and stability in the reaction conditions and the stability test, can remove a hybrid diesel inferior more than 90% of sulfur ,nitrogen.

The hydrogenation performances of nickle based catalyst LY-2008 for the first stage hydrogenation of pyrolysis gasoline were evaluated in a 500 mL industrial side stream reactor,by using C5-C9 fraction of Ethylene Factory of Dushanzi Petrochemical Company as feedstock and under the process conditions based on that of the pyrolysis gasoline hydrogenation unit.Stability constrast test of 1000h was carried out between LY2008 and an advanced catalyst HTC-200 imported from abroad.The results showed that the optimum conditions for LY-2008 catalyst were:inlet temperature 55100℃,pressure 2.5-3.0MPa,liquid space velocity 1.5-2.5h-1,the volume ratio of hydrogen to oil 150-250,feed stock dilution ratio 3-5.Under the above process conditions that hydrogenation activity and stability of LY-2008 approached to that of HTC-200.

It is a process with low investment and great profit to use the C_5 etherealization product as the blending component of gasoline with high octane number.The C_5 fraction is cut from steam cracking and it's diolefins are saturated by selective hydrogenation. This paper mainly studies the effect of pressure, LHSV, temperature and mole ratio of alcohol and alkene on conversion ratio of tertiary amylene. After methanol is taken out, the research octane number of C_5 etherealization product is about 95. The alkene content is less than 35%, the sulfur content is less than 10μg/g and the aromatics content is less than 1%, it is a clean and high quality gasoline component with high octane number. It will improve gasoline quality and increase the octane number and the oxygen content after it is blended with FCC gasoline.

裂解C5馏分选择性加氢饱和二烯烃后,醚化产物作为高辛烷值汽油调合组分是一条投资少、见效快的工艺路线.本文主要考察和研究了反应压力、空速、反应温度、醇烯摩尔比对叔戊烯转化率的影响.脱除甲醇后,裂解C5馏分选择性加氢后的醚化产物的研究法辛烷值为95左右,烯烃含量小于35%(ω),硫含量小于10×10-6(w),芳烃含量小于1%(w),是一种优质、清洁的高辛烷值汽油组分.与FCC汽油组分调合,可以提高汽油辛烷值,增加汽油氧含量,改善汽油的性能.

Etherification of the C5 cut from steam cracking for the synthesis of high octane number composite of gasoline after selective hydrogenation is a high profit process with low investment. In or-der to meet the requirement of the catalyst for etherification, di-olefin selective hydrogenation of the C5 cut from steam cracking was studied. After evaluating the catalyst, process parameters such as re-action pressure, LHSV, temperature and H/oil molar ratio on the di-olefin selective hydrogenation were optimized and the following optimal values were obtained: 0.5-1.5 MPa, 45-80℃, LHSV= 1.0-2.0 h-1 and H/oil molar ratio＞1.1.

综合分析了国内外裂解C5的利用情况,以及研究开发方面的动向.针对目前国内裂解C5资源利用率低,经济效益差的现状,结合国内乙烯工业的发展情况,提出了国内裂解C5馏分资源利用的建议.