摘要
中国石油化工集团公司中原石化有限责任公司建设的0.6Mt/a甲醇制低碳烯烃（S-MTO）装置运用催化裂化反应-再生动力学原理,采用专有设备和内构件;快速床流态化气相进料;高选择性和稳定性的SAPO-34分子筛催化剂;反应-再生控制原理;反应及产品气的急冷系统;急冷塔底渣浆过滤和废水处理等环保设施。产品分离系统采用前脱乙烷深冷分离工艺,设置了加氢、干燥、萃取、汽提分离、丙烯制冷等单元,深冷分离温度在-40℃左右,用精馏原理逐一分离,获得纯度符合要求的乙烯、丙烯和一些副产品。运行结果表明,催化剂上带有一定量的积炭,可提高低炭烯烃选择性,在完全和不完全再生模式下,开车和运行方式均能维持再生催化剂定碳1%～2%,反应器内催化剂平均定碳控制在4.5%～6.0%,双烯收率33.59%（以甲醇原料计）,产品总液体收率42.86%,甲醇转化率99.93%,S-MTO装置开车运行需要关注两器进料前升温措施、催化剂的选择性和碳含量控制、烟气和产品气能量回收综合利用、后续工艺催化剂的携带、污水处理达标排放、关键高温耐磨设备等因素。
The FCC reaction and regeneration kinetics, special equipment and internals have been applied in the first 600,000 TPY methanol to olefin （S-MTO） unit in SINOPEC Zhongyuan Petrochemical Co. , Ltd.. The fast-bed fluidized gas-phase feed and high-selectivity and high-stability SAPO-34 molecular sieve catalysts are selected for the operation. The reaction-regeneration control principles are adopted, the quench system for reactor vapor products is added, and the facilities for environmental protection such as bottom slurry filter for quench tower and waste water treatment plant are installed. Refrigeration process is applied for product separa- tion system. The hydrogenation, drying, extraction, stripping and propylene refrigeration units are provided, and refrigeration temperature is controlled at about -40 ℃. The products are separated by fractionators to get the required ethylene and propylene products as well as some by-products. The operation shows that the catalyst with certain amount of carbon deposit can improve the selectivity for low-carben olefins. Under both the full re- generation and semi-regeneration modes, a fixed carbon of 1% -2% on regenerated catalysts can be main- tained. When the average carbon deposit on the catalysts in the reactor is controlled at 4.5% ～ 6.0%, the yield of ethylene and propylene is 33.59% （based upon methanol feed）, the total product yield is 42.86%, and the methanol conversion is 99.93%. During the start-up of the S-MTO unit, attention should be paid to the meas- ures for elevating the temperature of reactor and regenerator before introducing the feed, control of catalyst selec- tivity and carbon deposit, waste heat recovery from flue gas and products and utilization, catalyst carry-over, waste water treatment and operation of critical high-temperature equipment in wearing operating conditions, etc.
出处
《炼油技术与工程》
CAS
2015年第11期13-16,共4页
Petroleum Refinery Engineering
