重烷基苯供料泵超压分析

第40卷第5期日用化学工业Vol 40 No 52010年10月China Surfactant Detergent Cosmetics0ct.2010重烷基苯供料泵超压分析刘忠和,康万利2(1.大庆油田化工有限公司技术开发研究院,黑龙江大庆163453;2.中国石油大学(华东)石油工程学院中石化提高采收率研究所,山东青岛266553摘要:对正常停产按操作规程停泵后,出现重烷基苯供料泵泵盖崩开泵出口压力表因超量程损坏现象进行了分析。通过排查管线测量重烷基苯密度随温度的变化计算重烷基苯热膨胀系数后发现问题所在:输出管线内重烷基苯加热后体积膨胀管内压强增大,泵出口阀关闭不严,致使泵体压强升高泵损坏。提出了两种解决方法:停泵后放出计算量的液体或在输出管线上加安全阀关键词:重烷基苯;热膨胀系数;超压中图分类号:TQ649.4文献标识码:A文章编号:1001-1803(2010)05-0390-03Analysis of over-pressure failure of heavy -alkylbenzene feed pumpLIU Zhong-he, KANG Wan-li(1. Technology and Development Institute of Daging Oil-Field Chemical Industry Co Ltd., DaqingHeilongjiang 163453, China; 2. SinoPec EOR Research Center, School of Petroleum EngineeringChina University of Petroleum, Qingdao, Shandong 266555, China)Abstract: A heavy-alkylbenzene( HAB)feed pump was shut down in accordance with the normal operatingrules. However, under such normal conditions, the pump casing broke and the pressure gage at the dischargeend of the hAB pump damaged due to the pressure to be measured was beyond the rated pressure range of thepressure gage. Such phenomena showed that the pump casing has been over pressurized. In order to find thereason of such over-pressure phenomenon, a thorough study with respect to the whole system as well as thephysical - chemical properties of working medium, including the troubleshooting of the pump and theconcerning piping as well as measurement of the density -temperature profile and the calculation of thermalexpansion coefficient of HAB, was carried out. Results showed that this problem is due to the expansion of theHAB liquid in the pump discharge piping system caused by temperature rise; while the block valve at theharge end of the pump was not tightly closed. Then the expanded HAB liquid flowed into the pump, andcaused the over-pressurizing of the pump casing. Two ways were suggested for avoiding the re-happening ofsuch failure. One is during the shut down of the pump, a calculated amount of the HAB liquid should beKey words heavy -alkylbenzene; thermal expansion coeficient; over pressure泵是化工生产常见的设备,常用泵有离心泵、柱塞的是出口压力高时防止憋坏泵体。按双凸齿轮泵的操泵和齿轮泵等。重烷基苯因其常温下黏度为16Pa·8作中国煤化工管线时,要将的进左右而使用齿轮泵。泵本身有循环泄压装置,其目出东昊表面活性剂分公CNMHG收稿日期:200928;修回日期:2010-07-22基金项目:国家自然科学基金资助项目(20873181);山东省泰山学者建设T程资助项目(t0070704)作者简介:刘忠和(1970-),男(汉),黑龙江人,工程师,硕士,电话:1383689第5刘忠和,等:重烷基苯供料泵超压分析生产与技术司出现停泵后1h内重烷基苯原料泵泵盖崩开、泵出为了更好地说明这一情况,作者测定不同温度下口压力表损坏事故。针对这一现象作者对事故原因进两种重烷基苯的密度,从而计算重烷基苯的膨胀系数行了查找。实验结果见图1。由图1可知,烷基苯的密度随温度1实验部分的升高而降低。1.1试剂及仪器重烷基苯(1号重烷基苯,平均相对分子质量280;2号重烷基苯,平均相对分子质量340),抚顺化工公司洗化厂。DCW-3506低温恒温槽,宁波天恒仪器厂;DMA4500型密度计, Anton Paar公司12密度测定10010203040慢慢将重烷基苯倒入量筒,将量筒置于恒温槽中,15min后放入密度计,读取弯月面下部刻度线数值图1重烷基苯密度随温度的变化曲线2结果与讨论膨胀系数称“体积膨胀系数”,无论物质是哪种泵压升高来自两个方面:液体被压缩,即泵偷转;(固体液体或气体)形态变化,都称之为体积膨胀,体液体体积膨胀,即温度升高。积膨胀系数计算公式为:2.1模拟泵偷转关闭泵进出口阀门启动泵,虽然是违反操作规程,式中:V为0℃时物质的体积;但是为模拟泵偷转只能如此,有人监护。压力表读数v为t℃时物质的体积是0.5MPa,压力表损坏的压力要超过1.2MPa。由此a为体积膨胀系数。可知,泵盖崩开不是泵偷转引起的。由于固体或液体的膨胀系数很小,在温度不是很2.2重烷基苯热膨胀系数测定高时,可直接用式(2)计算体积膨胀系数。V2=v[1+a(k2-1)]泵盖崩开和出口压力表损坏,用手测试了泵体温式中:V是在4℃时物质的体积;度,没有产生高温。已经排除泵偷转,不存在压缩问V2是在2℃时物质的体积题,只有液体(即重烷基苯)膨胀。泵体不热,但泵的如果用密度来表示a,则:出口阀关闭不严,问题就出在阀关闭不严上。泵出口到反应器大约有120m,供料管直径为50.8mm,附属热水伴热保温管线,热水温度在55℃-60℃。冬季式中:p0为起始温度时重烷基苯的密度;北方户外温度低于-20℃,从泵出口到反应器之前换p2为终了温度时重烷基苯的密度;热器,管线内重烷基苯温度升至约10℃~15℃,这是Δt为温差。传输管线伴热的结果。按正常操作规程停车或者换传输管线,从泵出口到换热器之前,两阀门之间关闭成从图1可知,(p-p2)/M近似为一常数C,则封闭管线。关闭阀门瞬间传输管线内重烷基苯平均a=C/pp随温度升高而降低膨胀系数在此温度区温度不会超过10℃,热水伴热会使管线内重烷基苯升间随温度升高而增大。在此温度区间里膨胀系数可温到40℃-50℃,温度上升管线内重烷基苯的体积近似为宾会膨胀。液体压缩需较大的压力,因泵出口阀关闭不中国煤化工=620×10-,a在严,则泵体压强会随着传输管线一起上升,管线耐压强.07CNMH度高于泵头盖密封处,所以在薄弱点泄压,泵头盖密封C2=(0.894-0.855)/(50+20)=5.57×10泄露。623×104-6.51×10-(-20℃-50℃)生产与技术日用化学工业第40卷相比较于水,重烷基苯的膨胀系数要大几倍。其安全受热膨胀体积更大,产生的压强更大,在现有的生产条件下,北方冬季停车后关闭阀门,其产生的压强一定会超过0.8MPa(冬季室外水管会冻裂,管线耐压强度为重烷基苯管线08MPa,水0℃膨胀系数为1.3×10-4)2.3解决问题的方法1)放一定体积原料:按正常操作程序停车或换输图2管线改造示意图出管线后,所停泵的出口阀不能立即关闭,在泵出口底阀放出计算量体积(膨胀体积V2-V1=aH1(l2-t1))综上所述,北方冬季化工原料传输管线法兰泄漏的烷基苯,然后再关闭泵的出口阀。以及户外管线连接的化工设备出现泄露,多考虑一些2)管线上加安全阀:在距不合格酸储罐就近管线传输介质的体积膨胀特别是有伴热的户外管线在设上接一安全阀跳阀压力设为0.4MPa,阀出口至不合计的时候要多考虑冬夏温差带来的不利影响。格酸储罐,这样管线的压力升高,重烷基苯就进入不合參考文献:格酸储罐。安全阀安装如图2所示。[1]栾振辉齿轮泵研究的现状与发展[]起重运输机械m06(6):ll-13.(上接第380页)[19] SONG Y S, CHUNG B Y, PARK M E, et al. 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