南华大学化学化工学院毕业设计
致 谢
首先，本工作是在我的导师肖志海老师的亲切关怀下完成的，从课题的选定到工艺合成路线、设备以及附属设备的工艺尺寸和选型的确定，肖老师都予以悉心的指导。一个学期来，肖老师在学业和生活上都给予我极大的关怀与帮助，他渊博的知识、严谨的科研精神、宽容平和的性格都令我难以忘怀，在此仅表示我崇高的敬意和真心的谢意！本课题组的魏刚，周国梁等同学所做的工作、提出的宝贵意见使我的毕业设计能够得以顺利的完成，这里一一并表示谢意！
经历了几个月的时间，在老师的精心指导和全组成员的共同努力下，我们完成了工艺技术方案的选择、工艺流程设计、物料衡算、能量衡算、工艺设备的设计与选型、设备布置的设计、管路设计、非工艺设计项目的考虑、编写设计说明书及图表等内容。在设计的每一个阶段，我们都经过讨论，综合考虑了技术的合理性和先进性、资源情况、工艺现有水平、安全可靠性及经济等多方面的因素，处理了大批的数据并按生产经验进行了多方面的优化，得出最终方案而完成设计任务。
我们首先进行了物料衡算，主要设备反应釜筒体内径、高度、壁厚和上、下封头选取型、热量衡算与传热面积校核、非主要设备计算与选型、接管和法兰的选择。在计算与选型过程中，我们充分发挥了团队合作精神，查找了大量的数据与资料，然后设计并绘出年生产1000吨丙烯酸乙酯车间的物料流程图和带控制点的工艺流程图，对车间、设备平面、立面布置图和管路空视图，进一步巩固了《化工工程制图》所学的知识，初步将其中所学知识运用于实践中。
我们在设计过程中也存在许多不足之处。首先，由于资料不足，在查找数据时耗费大量时间并带来诸多不便；其次，由于设计经验的缺乏，使得对某些数据按工业生产经验取值不合理，导致计算过程耗费过多时间。此外，由于其他相关方面知识和经验的不足，使我们在设备安装，原料产品的运输，仪表选择与控制，经济性，环境保护等方面考虑不周。在设计过程中，在老师的精心指导下，在组员们团结协作充分发挥创新精神的努力下，我们顺利完成了此次毕业设计。在此，对指导教师的辛苦劳动，我们再次表示感谢！
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南华大学化学化工学院毕业设计
附录：一
HS/DI值大致如：
表5—1几种反应釜的HS/DI值
种类 一般反应釜 发酵釜类 釜内物料类型 液-固相或液-液相物类 气-液相物料 HS/DI值 1—1.3 1--2 1.7--2.5 附录：二
公称直径 DN（mm） （1300） 1400 (1500) 1600 （1700） 1800 （1900） 2000 曲面高度h1(mm) 325 359 375 400 425 450 475 500 直边高度h2(mm) 25 40 50 25 40 50 25 40 50 25 40 50 25 40 50 25 40 50 25 40 25 40 50 内表面积Fh(mm2) 1.93 1.99 2.03 2.23 2.29 2.33 2.55 2.62 2.67 2.89 2.97 3.02 3.25 3.34 3.39 3.64 3.73 3.78 4.05 4.14 4.48 4.57 4.63 容积Vh(mm3) 0.321 0.341 0.354 0.398 0.421 0.436 0.487 0.513 0.530 0.587 0.617 0.637 0.700 0.734 0.757 0.826 0.866 0.889 0.971 1.01 1.13 1.18 1.20
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南华大学化学化工学院毕业设计
英文原文
Ethylene recovery from ethyl acrylate process
[Abstract] Unreacted ethylene contained in a gaseous light ends stream derived from a
process for the production of ethyl acrylate from ethylene and acrylic acid utilizing a sulfuric acid catalyst, is recovered by intimately contacting, under controlled conditions of temperature and pressure, the light ends stream with the liquid sulfuric acid catalyst make-up stream which is passed to the ethyl acrylate process. Upon contact of the light ends stream with the sulfuric acid make-up stream, the ethylene reacts with sulfuric acid to form ethyl hydrogen sulfate and diethyl sulfate, both of which remain in solution in the sulfuric acid which is then passed to the ethyl acrylate process as a source of make-up sulfuric acid. Sulfur dioxide contained in the vent-gas stream is not absorbed into the sulfuric acid, and therefore not recycled to the ethyl acrylate process.
Claims
The embodiments of the invention in which an exclusive claim or privilege is claimed are:
1. In a continuous process for the production of ethyl acrylate from ethylene and acrylic acid utilizing a sulfuric acid catalyst wherein the reaction products are distilled in a vacuum distillation system at a reduced pressure less than atmospheric to obtain a liquid ethyl acrylate product and also resulting in a first gaseous light ends stream from said vacuum distillation system containing sulfur dioxide and also containing ethylene and other organic light ends, and wherein losses of sulfuric acid catalyst are replenished by continuously passing to the reaction zone of said process a sulfuric acid make-up stream consisting of concentrated sulfuric acid having less than five percent by weight of water therein, the improvement which comprises: continuously and intimately contacting in a gas-liquid contact zone said first gaseous light ends stream with a reactant liquid consisting essentially of said liquid sulfuric acid
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南华大学化学化工学院毕业设计
make-up stream and the hereafter defined liquid recycle stream, said contacting being under such conditions as to cause ethylene in said first gaseous light ends stream to react with sulfuric acid in said reactant liquid so as to form ethyl hydrogen sulfate and diethyl sulfate, the said first gaseous light ends stream being at a temperature within the range of about 25.degree. C. to 150.degree. C. when passed to said contact zone, the initial temperature of said reactant liquid being within the range of about 40.degree. C. to 150.degree. C., and the pressure in said contact zone being maintained at a superatmospheric pressure within the range of about 1.05 atmospheres absolute to 20 atmospheres absolute, said pressure being sufficient to maintain said reactant liquid in the liquid phase but insufficient to cause the gases in said first gaseous light ends stream to dissolve in said reactant liquid; continuously withdrawing as overheads from said contact zone a second gaseous light ends stream containing sulfur dioxide, ethylene and other organic light ends, the amount of ethylene in said second gaseous light ends stream being less than the amount in said first gaseous light ends stream, the amount of sulfur dioxide in said second gaseous light ends stream being substantially the same as the amount of sulfur dioxide contained in said first gaseous light ends stream, the temperature of said second gaseous light ends stream being within the range of about 50.degree. C. to 150.degree. C.; continuously withdrawing as bottoms from said contact zone a liquid bottoms product consisting essentially of sulfuric acid having ethyl hydrogen sulfate and diethyl sulfate dissolved therein, said liquid bottoms product being substantially free of sulfur dioxide; and continuously recycling a major portion of said liquid bottoms product to said contact zone as a said liquid recycle stream, and continuously passing a minor portion of said liquid bottoms product to said ethyl acrylate process as a source of make-up sulfuric acid.
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南华大学化学化工学院毕业设计
2. The process of claim 1 wherein said major portion of said liquid bottoms product comprises from about 50 to 98% by weight of the total of said liquid bottoms product.
3. The process of claim 1 wherein the said contacting of said reactant liquid with said first gaseous light ends stream is accomplished in a said contact zone consisting of a tower wherein the first gaseous light ends stream ascends in said tower counter-currently to and in intimate contact with descending reactant liquid, the weight ratio of said reactant liquid to said first gaseous light ends stream being at least 10:1.
4. The process of claim 1 wherein said first gaseous light ends stream contains at least 10% by weight of sulfur dioxide and contains at least 20% by weight of ethylene.
Description
BACKGROUND OF THE INVENTION
It is known in the prior art to produce ethyl acrylate from ethylene with acrylic acid in the presence of a sulfuric acid catalyst. By way of example, see U.S. Pat. No. 3,894,076 issued July 8, 1975 to Roger L. Van Duyne et al. wherein such a process is disclosed. In these prior art processes recovery of a liquid ethyl acrylate product is accomplished by passing the reaction mixture to a vacuum distillation system wherein, at reduced pressures less than atmospheric, the reaction mixture is distilled to obtain a liquid ethyl acrylate product. Also resulting from the vacuum distillation is a gaseous light ends stream containing sulfur dioxide and also containing ethylene, ethyl acrylate and other organic light ends. The light ends stream may also contain inerts such as nitrogen from air leaks and carbon dioxide from oxidation. The sulfur dioxide in the stream derives from the sulfuric acid catalyst used in reaction of the ethylene with the acrylic acid. Due to losses of sulfuric acid catalyst through sulfur dioxide formation and the like, it is necessary to make
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