大庆常渣催化裂化毕业设计[精选].doc

万吨/年催化裂化反-再两器工艺计算 摘 要 本设计是 万吨/年催化裂化反-再两器工艺计算，主要内容是进行反应器、再生器的物料平衡和热平衡及两器的压力平衡的计算。首先对再生器进行物料平衡计算，计算出干空气量、焦炭量、总干烟气量和生成水汽等的物质组成和流量大小，进而校核再生器物料平衡。其次根据渣油残炭值大，生焦率高等特点，可以认定该套烧焦罐装置为热过剩型，对于热过剩型装置，通过对反应器进行热平衡，计算出催化剂循环量2100t/h,并求出剂油比5.84。通过再生器热平衡计算，计算出再生器的剩余热量，取热量。由再生器的密相床层体积流量及线速确定出再生器结构尺寸：烧焦罐直径9.8m，高14.7m；稀相管直径4.8m，高9.8m；稀相段直径14.0m，高15m。反应部分工艺计算结果如下：提升管反应器直径1.5m，高27m；预提升段直径0.9m，高4m；沉降器直径7.4m，高11m；汽提段直径3.9m，高8.75m。最后进行两器压力平衡的计算,满足要求。 关键词:催化裂化；渣油；烧焦罐；设计 Abstract The design is million tons/year catalytic cracking reactor-regenerator process calculation,the the main contents are the pressure balance of the regenerator and the reactor,material balance and heat balance of the twos.First calculate regenerator material balance,calculate the amount of dry air, coke content, total dry flue gas volume and generate water vapor, such as material composition and size of the flow, thereby check the material balance of the regenerator. Secondly, according to features of the residue carbon residue value, high rate of coke, for the heat excess-type device, through the reactor heat balance the calculated catalyst circulation is 2100t/h. According to the regenerator heat balance calculation, calculate the residual heat of the regenerator to take the heat. It can be determined by the volume flow rate and the velocity of the regenerator dense bed regenerator structure size: charred tank diameter is 9.8m, height is 14.7m,thin tube diameter is 4.8m height is 9.8m; dilute segment diameter is 14.0m, height is 15m. Furthermore calculation on the reaction part of the process: the riser reactor diameter is 1.5m， height is 27m, pre-lift segment diameter is 0.9m, height is 4m. The diameter of the settlement is 7.4m, height is 11m; stripper diameter is 3.9m, height is 8.75m. The calculation of the pressure balance between the two devices showed that it can be satisfied with the demand. Key words: catalytic cracking, residue, charred tank, design 目 录 1 文献综述 1 1