催化裂化粗汽油回炼改质工艺的用能改进

 针对催化粗汽油回炼改质过程能耗偏高的现状,进行了以降低辅助提升管油/剂接触温差和优化辅助分馏塔油气热量利用为内容的过程用能改进。工程实施结果表明,利用装置低温余热提高粗汽油回炼温度,可通过多发生5.7t/h的中压蒸汽,将辅助分馏系统的较低品质热量置换出等量的反-再系统的高品质热量;同时,辅助分馏塔中段回流热和循环油浆热量的升级利用,使得催化粗汽油回炼改质工艺的用能状况大为改善。优化改进后的有效热利用提高,干气和焦炭的产率下降,使现有的50t/h粗汽油回炼改质催化装置能耗降低4.4 (kg 标油)/ (t原料),且汽油质量得到提高。     

降低催化裂化汽油烯烃含量技术进展

介绍了降低催化裂化汽油烯烃含量的途径,包括选择合适的催化裂化工艺、应用降烯烃催化剂和助剂、选择中质中间基FCC原料、对原料进行预处理以及对催化裂化汽油进行后处理等。简述了各种催化裂化工艺和降烯烃催化剂及助剂在部分FCC装置的应用效果。指出要实现油品的清洁化,应开发FCC汽油醚化工艺,建造汽油加氢、重整、异构化和烷基化装置。     

优化催化裂化操作提高重油转化率降低汽油烯烃含量

通过优化催化裂化装置的操作参数可有效提高重油转化率和降低汽油烯烃含量。在工业催化裂化装置上优化结果表明：当系统催化剂的活性由58提到62，油浆产率降低1．14％，干气产率降低0．18％，汽油烯烃含量降低4．5％；当汽油回炼量由原料量的12％增至20％，干气产率降低0-31％，汽油烯烃含量降低6．5％；当剂油接触时间延长0.2s，汽油烯烃含量降低2％；当反应温度降低5℃、再生温度降低20℃时，汽油烯烃含量降低2．2％，干气产率降低0．28％。     

Analysis of Measures and Effect on Reducing Olefin Content in Gasoline

This article refers to major measures for reducing olefin content of automotive gasoline and the effect after adoption of these measures. The key for reducing olefin content in China＇s automotive gasoline pool is to reduce the olefin content of FCC naphtha. The domestic refiners apply the olefinreducing catalyst to decrease the olefin content of FCC gasoline as a convenient and cheap means to meet the national standard for automotive gasoline at the present phase. Furthermore, the novel domestic FCC reaction processes, such as the MIP, MGD, FDFCC and other processes can also apparently reduce olefin content in FCC gasoline. In order to further reduce the olefin content in gasoline to meet more stringent standard for automotive gasoline, Chinese refiners should optimize the processing scheme while aggressively disseminating hydrogenation process along with development of catalytic reforming, alkylation, etherification and other processes to completely change the simplistic composition of domestic gasoline pool.     

降低汽油烯烃含量用RFG-NJ催化剂的工业试验

在 1.0Mt/a重油催化裂化装置上进行了降低汽油烯烃含量用RFG -NJ催化剂的工业试验 ,并进行了标定。标定结果和日常统计数据分析表明 ,RFG -NJ催化剂具有显著降低汽油烯烃含量的性能。在装置掺渣率为 2 5 %左右、反应温度下降 6℃的情况下 ,汽油烯烃含量由48.6%下降至 3 6.5 % ,下降了 12 .1个百分点 ,汽油的诱导期延长 ,安定性得到改善 ,但汽油辛烷值略有下降 ,装置的总轻烃收率变化不大 ,丙烯收率下降了 0 .13个百分点     

生产清洁汽油的新型催化裂化工艺

介绍了生产清洁汽油的4种催化裂化新工艺，并与催化裂化工艺在产率分布及汽油性质方面进行了对比。这些新工艺具有依托原提升管催化裂化工业装置，使用常规或专用裂化催化剂，通过对裂化反应、氢转移反应和异构化反应等进行控制与选择，明显降低催化汽油烯烃含量的特点。     

Investigation of the Operating Conditions on Decreasing FCC Gasoline Olefin Content by GOR-Q Catalyst

Abstract

Based on a fixed-fluid-bed reactor and a GOR-Q catalyst, the influence of process parameters on decreasing gasoline olefin content was studied. The results show that the catalyst had an obvious effect on the decreasing gasoline olefins. A higher catalyst-to-oil ratio, lower weighted hourly space velocity, and lower reactor temperature give rise to lower gasoline olefin content. The reduction of fluid catalytic cracking (FCC) gasoline olefin content is achieved by decreasing olefins of low carbon number. Reaction temperature under 520°C and catalyst-to-oil ratio = 7.0 for a GOR-Q catalyst are advantageous for decreasing olefin content of FCC gasoline.     

工艺条件对降低催化汽油烯烃过程中汽油烯烃分布的影响

着重考察了在使用降烯烃催化剂GOR-Q和常规催化剂MLC-500时工艺条件对催化汽油烯烃分布的影响。结果表明：GOR-Q催化剂具有明显降低催化汽油各类烯烃的效果。从碳数分布看,催化汽油中的烯烃主要集中在C5～C7之间。从类型看,单烯烃是催化汽油烯烃的主要存在形式,其中又以正构烯烃和单支链烯烃为主。降低催化汽油烯烃主要是通过小分子烯烃或单烯烃、正构烯烃、单支链烯烃的降低来实现。低温、低空速、高剂油比有利于降低催化汽油中单烯烃、正构烯烃、单支链烯烃和二烯烃含量,但为了减少辛烷值的损失,在降低催化汽油烯烃时首先应采用提高剂油比的方式。     

增产丙烯和生产清洁汽油组分技术的工业试验

在中国石油化工股份有限公司镇海炼油化工股份有限公司1.8M t/a的重油催化裂化装置上进行了增产丙烯和生产清洁汽油组分(M IP-CGP)技术的工业试验。工业试验结果表明,采用M IP-CGP技术,丙烯质量收率最高可达8.16%;汽油中的烯烃体积分数最低可降至18%以下。与原来采用的催化裂化工艺相比,汽油与原料油的硫含量(质量分数)之比下降50%~65%,辛烷值提高1.0~1.6个单位;总液体(液化气、汽油、柴油)质量收率约增加1%。该技术具有良好的技术经济效益和社会效益。     

催化裂化汽油在LBO-A/LBO-16催化剂上的芳构化

以催化裂化汽油为原料,LBO-A催化剂和LBO-16催化剂混合物(二者质量比为1∶1)为芳构化催化剂,在小型固定流化床反应器和中型提升管反应器上进行了芳构化反应性能研究。结果表明,在2种反应器中,产品液体收率大于89%,改质汽油烯烃体积分数下降20个百分点以上,芳烃体积分数增加10个百分点以上,产品分布和汽油质量得到改善。在小型固定流化床中的芳构化改质汽油中,烯烃体积分数下降幅度及芳烃体积分数增加幅度大于在中型提升管反应器上的。     

Catalyst Innovation for Reducing Olefin Content in MGG Gasoline

In order to reduce the olefin content in gasoline manufactured by the MGG (Maximizing Liquefied Gas and Gasoline) process while retaining the LPG yield, RIPP has developed a novel catalyst consisting of a more pore-opened matrix and the modified Y-zeolite and the ZRP zeolite modified with metal oxides. Test results have revealed that compared with the commercial catalyst RAG under comparable reaction conditions the reaction conversion rate and product distribution provided by the novel catalyst were similar, but the olefin content in gasoline obtained thereof was decreased with the octane rating unchanged along with a slight reduction of olefin content in the LPG fraction. The hydrothermal stability of the novel catalyst was better than the commercial catalyst RAG.     

RFCC汽油降烯烃前后氢平衡计算与分析

通过对中国石油化工股份有限公司北京燕山分公司三催化装置使用GOR－DQ降烯烃催化剂前后氢平衡及氢分布的计算与分析，验证了该装置物料平衡的准确性，并发现使用该催化剂在明显降低汽油烯烃的同时，使氢分布趋于合理。     

生产清洁汽油组分的催化裂化新工艺MIP

从反应机理出发,提出催化裂化反应两个反应区的概念并得到小型试验验证,据此设计了新的反应器,提出了相应的工艺措施,并在此基础上,进行了中型试验。中型试验结果表明：对于管输混合油,在保持与现有的催化裂化产物分布相同的情况下,该工艺所生产的汽油中的烯烃含量下降12．4个百分点,异构烷烃和芳烃含量分别增加约6个百分点,汽油的RON不变而MON提高1．3个单位,汽油ω（硫）下降15％,诱导期大幅增加。     

利用催化裂化技术生产低烯烃高辛烷值汽油

汽油新标准(GB17930—1999)要求汽油中烯烃含量≤35％(9),使作为车用汽油主要来源的催化裂化工艺面临新的挑战和发展机遇。通过选择具有氢转移、异构化和芳构化能力的催化裂化催化剂和优化工艺操作参数,在保证重油转化深度的前提下,促进氢转移、异构化和芳构化反应,能够在降低汽油中的烯烃含量4～6个百分点的同时,使汽油的辛烷值增加1～4个单位。     

多产异构烷烃的催化裂化工艺的研究

A concept of two different reaction zones was proposed based on the FCC reaction mechanism.The concept was used to design a novel reactor with corresponding operation measures.Experiments were conducted on the newly designed pilot-plant riser reactor.In comparison with the conventional FCC at relatively equivalent conversion,the pilot-plant test results showed that the olefin content in the cracked naphtha dropped by 12.4% ,and both cintents of iso-paraffin and aromatic increased by 6%,and its MON increased by 1.3 units while maintaining the RON of the naphtha unchanged,and its sulfur content reduced by 15% with a significant extension of its induction period for Shengli VGO VR.The run test results of commercial trial were conformable with the results of pilot -plant test.     

A New Downstream Process Design for a Fluid Catalytic Cracking Unit to Raise Propylene Yield and Decrease Gasoline Olefin Content

Abstract

Based on the paraffins, olefins, naphthenes, aromatics (PONA) composition of crude light gasoline, crude heavy gasoline, stabilized gasoline, and wet gas of a pilot plant fluid catalytic cracking (FCC) unit, it was found that the root cause of high gasoline olefin content and low propylene yield was low C₅ and C₆ olefin content of crude light gasoline. A new design for the main fractionater and absorber–stripper–stabilizer was presented to obtain stabilized light gasoline that contains more C₅ and C₆ olefins recracked in the secondary riser. Industrial studies on the revamped unit showed that gasoline olefin content was decreased markedly, though research octane number (RON) was preserved. In addition, propylene yield was raised to a higher level and unit energy consumption (or operating cost) was not increased.     

小型提升管反应器上甲醇与流化催化裂化汽油混炼改质的研究

在小型提升管流化催化裂化(FCC)装置上,使用FCC催化剂,进行了甲醇与FCC汽油的混炼实验,考察了反应温度、甲醇与FCC汽油的质量比(混炼比)及甲醇不同进料位置对精汽油族组成、裂化气组成和液体收率的影响。实验结果表明,甲醇与FCC汽油共混进料的反应效果优于甲醇提前或延后FCC汽油进料时的反应效果;甲醇与FCC汽油混炼在改善汽油质量的同时,有利于增产裂化气和提高液体收率。甲醇与FCC汽油混炼的适宜条件为:反应温度400~420℃、混炼比为5%~10%、剂油比10~12。在此条件下,FCC汽油烯烃含量下降50%以上,液体收率增加3%左右,裂化气中干气质量分数小于1.5%,精汽油与液化石油气收率之和达到98%以上。     

催化裂化汽油辅助提升管降烯烃技术的工业应用

新开发的催化裂化汽油辅助提升管改质降烯烃技术,在中国石油华北石化分公司1.0Mt／a重油催化裂化装置上进行了工业应用。该技术实施后,汽油烯烃体积分数由55％降低到35％左右,除汽油研究法辛烷值比预提升段回注下降0.3个单位外,对产品主要性质影响不大,成功实现了重油裂化主提升管和催化裂化汽油改质辅助提升管的平稳运行,与改造前采用的催化裂化汽油预提升段回注措施相比,液体收率和轻质油收率分别提高了1.5和5.7个百分点,干气和焦炭产率分别下降了0.8和1.3个百分点。     

Commercial Test on Technology for High-Temperature Cracking of C5 Fraction to Decrease Olefin Content of Gasoline in DCCU

During June and July 2003,Jingmen Petrochemical Company carried out the commercial test on technology for high-temperature cracking of C5 fraction to decrease olefin content of gasoline in DCCU.The test results showed that the olefin content of DCC gasoline had decreased from 68.32m% to 42.5m%。meanwhile the propylene yield increased by 0.90m%.     

催化裂化汽油回炼技术应用

大庆炼化公司林源生产区对其两套催化裂化装置进行了技术改造 ,Ⅰ套催化裂化直接在提升管反应器的预提升蒸汽管道上打入粗汽油进行回炼 ,柴油收率可达 36 %以上 ;Ⅱ套催化裂化装置对提升管喷嘴位置进行了适当调整 ,柴油收率达到 35 %以上 ;按柴油生产方案 ,两套催化裂化装置均可达到单装置柴汽比 0 .9以上 ,取得较好经济效益