A型沸石膜管失效后α-Al_2O_3载体管的再处理与性能
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摘要
使用后的废弃沸石膜管难以处理,而α-Al_20_3作为沸石膜的载体,使用寿命长于沸石膜。因此,以工业应用中被糖类损环的A型沸石膜管载体为对象,进行废弃膜管α-Al_2O_3载体的回收,并以二次生长法为基础,在回收载体上二次制备A型沸石膜。研究了酸种类、酸浓度,酸洗时间等条件对沸石膜渗透汽化性能的影响。结果表明:经去离子水及0.2mol/L的氢氧化钠预处理后,用浓度为0.8%硝酸超声酸洗5min,得到的载体性能最佳,采用此载体合成的A型沸石膜渗透通量和分离因数分别为1.14kg/(m~2·h)和3649,且重复性较好。
It is difficult to deal with abandoned zeolite membrane tube. α-Al_2O_3 as a carrier of zeolite membrane has a longer service life than zeolite membrane. Therefore, we recycled the wasted membrane tube with A-type zeolite membrane carrier, which was broken by saccharide in industrial application, and managed the secondary preparation of A-type zeolite membrane on recycled carrier based on the secondary growth. Effects of acid species, acid concentration and acid pickling time on the pervaporation performance of prepared zeolite membrane were investigated. The results show that the optimum carrier properties are obtained after pretreatment with deionized water and 0.2mol/L sodium hydroxide, and then ultrasonic cleaning in 0.8% nitric acid for 5min. The permeation flux and separation factor of A-type zeolite membrane synthesized by this carrier are 1.14kg/(m~2·h) and 3649, respectively.
It is difficult to deal with abandoned zeolite membrane tube. α-Al_2O_3 as a carrier of zeolite membrane has a longer service life than zeolite membrane. Therefore, we recycled the wasted membrane tube with A-type zeolite membrane carrier, which was broken by saccharide in industrial application, and managed the secondary preparation of A-type zeolite membrane on recycled carrier based on the secondary growth. Effects of acid species, acid concentration and acid pickling time on the pervaporation performance of prepared zeolite membrane were investigated. The results show that the optimum carrier properties are obtained after pretreatment with deionized water and 0.2mol/L sodium hydroxide, and then ultrasonic cleaning in 0.8% nitric acid for 5min. The permeation flux and separation factor of A-type zeolite membrane synthesized by this carrier are 1.14kg/(m~2·h) and 3649, respectively.
引文
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[3]郭大鹏,周志辉,吴建雄,等.氟离子与氧化铝摩尔比对丝光沸石膜及其渗透汽化性能的影响[J].硅酸盐学报,2015,43(1):28-34.GUO Dapeng,ZHOU Zhihui,WU Jianxiong,et al.J Chin Ceram Soc,2015,43(1):28-34.
[4]SMITHA B,SUHANYA D.Separation of organic-organic mixtures by pervaporation-A review[J].J Membr Sci,2004,241(1):1-21.
[5]顾学红,徐南平.渗透汽化脱水分子筛膜的制备与应用研究[J].中国工程科学,2014,16(12):52-58.GU Xuehong,XU Nanping.J Eng Sci(in Chinese),2014,16(12):52-58.
[6]张庆武曹蕊,陈翠仙,等.渗透汽化膜技术及其在有机溶剂脱水领域的应用[J].过滤与分离,2008,18(1):31-33.ZHANG Qingwu,CAO Rui,CHEN Cuixian,et al.J Filtr Sep(in Chinese),2008,18(1):31-33.
[7]梅金凤,周志辉,刘红,等.NaA沸石膜的制备及在一氯甲烷脱水中的应用[J].硅酸盐学报,2012,40(9):1363-1368.MEI Jinfeng,ZHOU Zhihui,LIU Hong,et al.J Chin Ceram Soc,2012,40(9):1363-1368.
[8]徐如人,庞文琴,霍启升,等.分子筛与多孔材料化学[M].科学出版社,2015.
[9]MORIGAMI Y,KONDO M,ABE J,et al.The first large-scale pervaporation plant using tubular-type module with zeolite NaA membrane[J].Sep Purif Technol,2001,25(1-3):251-260.
[10]KITA H,OKAMOTO K,YAMAMURA T,et al.Zeolite membranes for fuel ethanol production[J].Polym Prepr(Am Chem Soc,Div Polym Chem),2003,48(1):438.
[11]RICHTER H,VOIGT I,K(U|¨)HNERT J T.Dewatering of ethanol by pervaporation and vapour permeation with industrial scale NaA-membranes[J].Desalination,2006,199(1/3):92-93.
[12]周贤铮.广州市再生资源回收利用管理问题与对策研究[D].广州:中山大学,2009.ZHOU Xianzeng.Problems and counter-measures on the management of resources recycling industry in Guangzhou.(in Chinese,dissertation),Guangzhou:Sun Yat-Sen University,2009.
[13]陈静.我国再生资源回收体系的研究[D].天津:南开大学,2014.CHEN Jing.Research on China's recyclable resource recycling system.(in Chinese,dissertation),Tianjin:Nankai University,2014
[14]黄仲涛.无机膜技术及其应用[M].中国石化出版社,1999.
[15]周志辉,丁武龙,王涛,等.NaA分子筛膜渗透蒸发制备高纯糠醛[J].石油化工,2013,42(3):292-297.ZHOU Zhihui,DING Wulong,WANG Tao,et al.J Petrochem Technol(in Chinese),2013,42(3):292-297.