渣油悬浮床加氢工艺研究

介绍了渣油悬浮床加氢技术领域的现状及抚顺石油化工研究院渣油悬浮床加氢技术特点。在不同反应器规模的连续式悬浮床加氢装置上的试验结果表明，研制的水溶性催化剂具有较强的原料适应性，在中等压力、空速约1.0 h^－1、催化剂加入量低于300 μg/g和一次通过的条件下处理常压渣油，小于500℃馏分油收率为70%～90%；处理减压渣油，小于500 ℃馏分油收率可达60%～80%，而过程甲苯不溶物质量分数低于10%。将悬浮床加氢技术与其他重油加工过程组合，可增加悬浮床加氢技术的灵活性，并有利于提高过程的总液体收率和经济性。     

悬浮床渣油加氢技术简介

悬浮床加氢技术也称浆液床加氢技术，最早始于30年代的煤和煤焦油加氢。50年代初，德国将硫酸亚铁担载在褐煤或焦粉上用于煤焦油加氢，但其加氢活性很低。联合裂化过程(VCC)，是德国VEBA公司在煤和煤焦油加氢技术的基础上开发的，是一种高转化率的渣油热氢解过程。悬浮床渣油加氢使     

煤焦油重组分加氢技术现状及研究趋势探讨

为了解决固定床加氢技术难以加工沥青质、金属以及N、S等杂原子含量高的煤焦油重组分的问题,对可适用于煤焦油重馏分或全馏分加工的沸腾床加氢及悬浮床加氢技术的研究进展、技术特点及工业应用情况进行了系统阐述,并对煤焦油重组分加氢技术研究趋势进行了探讨,认为悬浮床加氢预处理-固定床加氢联合工艺的优化、悬浮床加氢廉价高效催化剂的研究、煤焦油与煤或渣油共加工工艺的开发及产品的高附加值利用将成为煤焦油重组分加氢技术未来研究开发的重点。     

渣油热反应性能与悬浮床加氢反应机理

介绍了渣油的组成性质及其与渣油热反应性能的关系,浅析了悬浮床渣油加氢的反应机理,为渣油加工技术的开发和悬浮床渣油加氢技术的深入研究提供理论依据.     

重油悬浮床加氢循环尾油旋流分离技术应用研究 Ⅱ.热模试验

针对重油悬浮床加氢工艺条件,在冷模试验的基础上,设计加工了热模试验用旋流器,建立了旋流分离热模试验装置,并利用重油悬浮床加氢循环尾油和一次通过尾油进行了旋流分离高温试验。试验结果表明,采用旋流分离技术能够满足悬浮床加氢循环尾油的分离要求。     

浅议催化剂对悬浮床加氢裂化的影响

随着重质原料油轻质化技术的不断发展,悬浮床加氢技术变成了煤焦油加氢的核心技术。针对现有悬浮床加氢装置,催化剂的添加起着至关重要的作用。本文主要介绍了现有的催化剂种类、最常用的催化剂的特点、以及悬浮床装置催化剂的工艺流程以及催化剂对工艺设备管线、重馏分油的转化率和轻油液收率的影响。催化剂的最佳添加量,仍然需要在实际生产中探索出适中用量,这对企业生产的综合效益至关重要。     

煤焦油加氢技术与工艺选择

介绍煤焦油加氢技术产业现状和主要技术路线;结合煤焦油特性和煤焦油加氢工艺,对悬浮床/浆态床反应器加氢工艺工业应用可能性进行分析.     

悬浮床加氢技术进展

综述国内外悬浮床加氢技术研究现状,从如何解决如何改善体系生焦、提高尾油利用率、降低催化成本三个方面,介绍了近几年悬浮床加氢技术所取得的系列成果,并指出如何解决这三个问题仍是未来较长时间悬浮床研究的重点。     

悬浮床加氢技术进展

综述国内外悬浮床加氢技术研究现状,从如何解决如何改善体系生焦、提高尾油利用率、降低催化成本三个方面,介绍了近几年悬浮床加氢技术所取得的系列成果,并指出如何解决这三个问题仍是未来较长时间悬浮床研究的重点。     

MCT悬浮床加氢工艺的研究及工业化进展

介绍了当前国内外主要的重油加氢工艺,以及悬浮床加氢工艺技术的研究及发展现状,重点叙述了国内首套MCT超级悬浮床重油加氢工艺技术研究和投产情况,通过MCT工艺在重油加工深度、轻油收率、物料衡算等方面的描述,总结MCT悬浮床加氢工业生产装置的运行情况,阐明了悬浮床加氢工艺未来的攻关方向和发展趋势.     

碳酸二甲酯的生产与技术经济

介绍了ＤＭＣ的用途、国内外市场需求及生产方法，对ＥＮＩ的液相氧化羰基化法和日本宇部兴产的气相氧化羰基化法进行了技术经济比较，并从工程设计角度对国内建设氧化羰基化法ＤＭＣ装置进行了经济评价。     

Practical aspects of hydrogenation and soybean salad oil manufacture

Most edible oils are hydrogenated in batch-type slurry converters similar in basic design to those employed when the process was first commercialized in 1911. One major company uses a proprietary continuous slurry process. Other novel batch and continuous slurry systems are available but have not enjoyed significant commercial success. Fixed bed hydrogenation has not been seriously investigated but offers intriguing possibilities. Energy economy is assuming ever greater importance in the design of hardening systems. The accelerated growth of hydrogenation since the 1940s parallels the rapid increase in soybean oil use. In part, it reflects the flavor instability of soybean oil caused by its linolenic ester. When this triunsaturate is lowered by hydrogenation to ca. 3%, a high-quality soybean salad oil can be produced. Standard hydrogenation and separation techniques work well. New separation equipment and processes are entering the marketplace.     

中低温煤焦油加氢技术进展及应用分析

介绍了煤焦油切割轻馏分加氢、延迟焦化加氢、悬浮床加氢、沸腾床加氢、宽馏分加氢、全馏分加氢等几种中低温煤焦油加氢技术的流程及特点。以40万t/a某煤焦油加氢装置为例,对比了各种技术的工艺流程、工业装置运行、建设投资、主要产品收率等情况,着重分析了沸腾床及全馏分加氢工艺技术的消耗和成本。通过分析得出全馏分加氢技术氢气消耗低于沸腾床加氢技术,公用工程指标中生产水、凝结水、低压蒸汽消耗略高于沸腾床加氢技术;加氢成本较沸腾床加氢技术低约100元/t,全馏分加氢技术煤焦油加氢总成本近4000元/t。     

浆态床渣油加氢催化剂研究进展

渣油加氢技术主要有固定床、沸腾床、移动床和浆态床。浆态床技术不存在催化剂的失活问题,几乎能处理各种性质的原料,是近年来的研究热点。浆态床技术通过加入催化剂达到劣质渣油改质的目的,使用的催化剂可分为不具有加氢活性的添加剂和具有加氢活性的催化剂两大类,添加剂的作用在渣油高转化率下较明显,所起的作用是阻隔生焦中间相的聚集以减少生焦;催化剂主要通过提供活性氢抑制大分子自由基的缩合和生焦并改质劣质渣油。对浆态床渣油加氢催化剂和添加剂的使用情况与机理进行总结,对未来发展进行展望,认为低成本有加氢活性的催化剂是未来浆态床渣油加氢催化剂的研究重点。     

加氢原料掺炼催化油浆的性质分析

催化油浆是催化裂化装置的塔底重质组分,其残炭高、黏度大且含有大量催化剂粉末,深加工困难.由于油浆内含有30％ ～50％的饱和烃,将其处理后返回装置加工就有很好的经济效益.本文探讨了催化油浆处理的可行性,分析了加氢原料与催化油浆混合后原料油的性质,从理论上给出了加氢原料掺炼催化油浆的可行性.     

多喷嘴对置式水煤浆气化技术的工程应用及其优势

介绍了华东理工大学和兖矿集团合作开发的具有完全自主知识产权、国际首创的多喷嘴对置式水煤浆气化技术工程应用及其优势,同时对其关键工艺指标与Texaco水煤浆气化技术进行了对照比较。     

Similar effect of carbon and silica catalyst support on the hydrogenation reaction rate in organic slurry reactors

This paper investigates the influence of the catalyst support type on mass transport and reaction rate for the case of hydrogenation of α-methylstyrene to cumene in a gas inducing stirred slurry reactor and in a slurry bubble column. The reaction is carried out in the presence of 3% Pd/carbon and 3% Pd/silica catalyst particles. The lyophobicity of the two catalyst supports in the cumene slurry is found to be similar. The overall rate of the hydrogenation reaction is described by the classical transport and reaction resistances-in-series model. The rate of gas-to-liquid mass transfer is somewhat larger during reaction than without reaction. This enhanced mass transfer points to particle-to-bubble adhesion as a result of the relative affinity of both catalyst supports to the gas phase. The observed reaction enhancements are similar for both Pd/carbon and Pd/silica catalyst/cumene slurries.     

Regeneration of used nickel catalyst

Regeneration of used nickel catalyst from a hydrogenation plant has been achieved by converting the nickel content of slurry into NiO and Ni(OH)₂, and the subsequent reduction of these compounds by hydrogen gas at temperatures of 450 C and 290 C respectively. A laboratory and plant apparatus for reduction are designed. Activity of regenerated catalyst was measured in comparison with reference catalyst (G15). Pretreatment of discarded catalyst prior to reduction is described.     

Fluid to particle mass transport in slurries

Equations are derived giving the relationship between the electrochemical potential of the catalyst and mass transport of hydrogen in liquid phase hydrogenation. The result provides a method for measuring local fluid to particle mass transfer coefficients in a slurry reactor. The method is illustrated by evaluating local Sherwood numbers for hydrogen transfer during hydrogenation of nitrobenzoic acid in water medium in the presence of 5% Pd/C.     

Hydrogenation active sites of unsupported molybdenum sulfide catalysts for hydroprocessing heavy oils

The purpose of the present study was to elucidate the nature of the hydrogenation active sites on unsupported molybdenum sulfide catalysts, aimed at the improvement of the catalysts for the slurry processes. The number of hydrogenation active sites was found to relate to the “inflection” on the basal plane of the catalyst particles. The comparison of the catalytic activity to that of an oil-soluble catalyst in the hydroprocessing of heavy oils suggests that the performance of the oil-soluble catalyst was near the maximum, unless another component such as Ni or Co was incorporated.