入口结构对18 m气固循环流化床提升管内颗粒流动特性的影响
|
摘要
在高18 m、内径80 mm的循环流化床提升管内分别考察了三种入口结构对颗粒流动特性的影响。实验结果表明:入口结构主要影响提升管底部区域的颗粒流动特性,不同入口结构对颗粒流动影响不同。相同操作条件下,当采用多管式入口结构时,径向上提升管底部区域的颗粒浓度分布相对均匀,轴向上颗粒能够迅速达到充分发展状态,充分发展高度在9 m左右;当采用多孔板入口结构时,径向上提升管底部颗粒浓度差别较大,轴向上颗粒发展较慢,需要更高高度才能达到充分发展,充分发展高度约为11 m;当采用单管式入口结构时,径向上颗粒浓度分布和轴向上颗粒充分发展速度均处于前两者之间,底部颗粒浓度径向分布仍为中间稀、边壁浓的不均匀分布,颗粒浓度轴向充分发展高度约为10 m。
Three kinds of riser inlet distributors were designed to investigate their effects on particle flow characteristics in a CFB riser with 18 m in height and 80 mm in diameter. The results show that inlet distributors have significant impact on particle hydrodynamics at the bottom region of the riser and different inlet distributors have different effects as indicated by characteristic length of the developing section. At the same operating condition, multiple tube inlet had uniform radial distribution of solid holdup and particle movement reached fully-developed state at about 9 m in axial direction, whereas perforated plate inlet had large concentration difference at bottom and particle movement developed slowly in axial direction requiring about 11 m in length to reach fully-developed state. On the other hand, single tube inlet had radial solid holdup and axial development region somewhere between those of the other two inlets. The single tube inlet had non-uniform radial solid holdup distribution of dilute center and dense side at the bottom of the riser and required 10 m axial length to reach fullydevelopment state.
Three kinds of riser inlet distributors were designed to investigate their effects on particle flow characteristics in a CFB riser with 18 m in height and 80 mm in diameter. The results show that inlet distributors have significant impact on particle hydrodynamics at the bottom region of the riser and different inlet distributors have different effects as indicated by characteristic length of the developing section. At the same operating condition, multiple tube inlet had uniform radial distribution of solid holdup and particle movement reached fully-developed state at about 9 m in axial direction, whereas perforated plate inlet had large concentration difference at bottom and particle movement developed slowly in axial direction requiring about 11 m in length to reach fully-developed state. On the other hand, single tube inlet had radial solid holdup and axial development region somewhere between those of the other two inlets. The single tube inlet had non-uniform radial solid holdup distribution of dilute center and dense side at the bottom of the riser and required 10 m axial length to reach fullydevelopment state.
引文
[1]金涌,祝京旭,汪展文,等.流态化工程原理[M].北京:清华大学出版社,2001.JIN Y,ZHU J X,WANG Z W,et al.Fluidization Engineering Principles[M].Beijing:Tsinghua University Press,2001.
[2]杨勇林.低密度循环流化床气固两相流体力学行为的研究[D].北京:清华大学,1989.YANG Y L.Fluid flow structure in a dilute two-phase suspension system in a circulating fluidized bed[D].Beijing:Tsinghua University,1989.
[3]燕兰玲,祝京旭,蓝兴英,等.两种新型流化床——高密度循环流化床和循环湍动流化床的对比分析[J].化工学报,2014,65(7):2495-2503.YAN L L,ZHU J X,LAN X Y,et al.Comparative study of two novel fluidized beds—HDCFB and CTFB[J].CIESC Journal,2014,65(7):2495-2503.
[4]徐令宝.小型提升管冷模实验研究[D].北京:中国石油大学,2011.XU L B.Experimental study of mini-riser cold model[D].Beijing:China University of Petroleum,2011.
[5]GENG Q,WANG L,LI Z C,et al.Radial non-uniformity index research on high-density,high-flux CFB riser with stratified injection[J].China Petroleum Processing&Petrochemical Technology,2012,14(4):64-72.
[6]ZHU J,XU J,PENG B,et al.The effects of distributor design on the solids distribution in a CFB riser[C]//The 13th International Conference on Fluidization-New Paradigm in Fluidization Engineering.Art.53.Korea:ECI Digital Archives,2010:1-9.
[7]YAN A,P?RSSINEN J H,ZHU J X.Flow properties in the entrance and exit regions of a high-flux circulating fluidized bed riser[J].Powder Technology,2003,131(2):256-263.
[8]YOU J,WANG D,ZHU C.Entrance effects on gas-solid riser flow structure[J].Industrial&Engineering Chemistry Research,2008,48(1):310-319.
[9]CHENG Y,WEI F,YANG G,et al.Inlet and outlet effects on flow patterns in gas-solid risers[J].Powder Technology,1998,98(2):151-156.
[10]白丁荣,易江林,金涌,等.快速流化床入口结构对床层流动特性的影响[J].化工机械,1995,(2):10-14.BAI D R,YI J L,JIN Y,et al.Effects of inlet structure on bed flow characteristics in the fast fluidized bed[J].Chemical Engineering&Machinery,1995,(2):10-14.
[11]KIM J S,TACHINO R,TSUTSUMI A.Effects of solids feeder and riser exit configuration on establishing high density circulating fluidized beds[J].Powder Technology,2008,187(1):37-45.
[12]MARZOCCHELLA A,ARENA U.Hydrodynamics of a circulating fluidized bed operated with different secondary air injection devices[J].Powder Technology,1996,87(3):185-191.
[13]GRACE J R,ISSANGYA A S,BAI D,et al.Situating the high-density circulating fluidized bed[J].AICh E Journal,1999,45(10):2108-2116.
[14]ISSANGYA A S.Flow dynamics in high density circulating fluidized beds[D].Canada:The University of British Columbia Vancouver,1998.
[15]ISSANGYA A S,BAI D,BI H T,et al.Suspension densities in a highdensity circulating fluidized bed riser[J].Chemical Engineering Science,1999,54(22):5451-5460.
[16]ISSANGYA A S,BAI D,GRACE J R,et al.Flow behavior in the riser of a high-density circulating fluidized bed[C]//AICh E Symp.Ser.93.1999:25-30.
[17]ISSANGYA A S,GRACE J R,BAI D,et al.Further measurements of flow dynamics in a high-density circulating fluidized bed riser[J].Powder Technology,2000,111(1/2):104-113.
[18]ISSANGYA A S,ZHU J X,BAI D R,et al.Solids radial flux profiles in a high density circulating fluidized bed riser[C]//FluidizationⅨ.New York:Engineering Foundation,1998:197-204.
[19]郭慕孙.流态化手册[M].北京:化学工业出版社,2008.GUO M S.Handbook of Fluidization[M].Beijing:Chemical Industry Press,2008.
[20]李鹏飞,章敬泉,朱晓华.循环流化床入口结构对流态化效果影响比较[J].环境工程,2011,29(4):82-85.LI P F,ZHANG J Q,ZHU X H.Effect of entrance structure on fluidization of circulating fluidized bed[J].Environmental Engineering,2011,29(4):82-85.
[21]PENG B,ZHANG C,ZHU J,et al.New approaches to improve the uniformity of the radial solids concentration distribution in CFB risers[C]//Proceedings of the ASME 2012 Fluids Engineering Summer Meeting.FEDSM2012.Rio Grande Puerto Rico:ASME,2012:1351-1357.
[22]ZHANG H,JOHNSTON P M,ZHU J X,et al.A novel calibration procedure for a fiber optic solids concentration probe[J].Powder Technology,1998,100(2/3):260-272.
[23]黄卫星,漆小波,潘永亮,等.气固循环床提升管内的局部颗粒浓度及流动发展[J].高校化学工程学报,2002,16(6):626-631.HUANG W X,QI X B,PAN Y L,et al.Local solid-particle concentration and flow development in a long CFB riser[J].Journal of Chemical Engineering of Chinese Universities,2002,16(6):626-631.
[24]林海波,孔春林,黄卫星.气固循环流化床提升管颗粒速度和浓度的测量技术[J].四川理工学院学报(自然科学版),2002,15(4):28-33.LIN H B,KONG C L,HUANG W X.Measurement techniques of solids concentration and solids velocity in circulating fluid beds riser[J].Journal of Sichuan Institute of Light Industry and Chemical Technology,2002,15(4):28-33.
[25]漆小波.循环流化床提升管气固两相流动力学研究[D].成都:四川大学,2003.QI X B.Hydrodynamics of gas-solid two-phase flow in circulating fluidized bed risers[D].Chengdu:Sichuan University,2003.
[26]YAN A,P?RSSINEN J H,ZHU J X.Flow properties in the entrance and exit regions of a high-flux circulating fluidized bed riser[J].Powder Technology,2003,131(2):256-263.
[27]王成秀.循环流化床反应器的增浓——高密度提升管及下行床流体力学特性研究[D].东营:中国石油大学(华东),2014.WANG C X.Increasing the density of circulating fluidized bed reactors—hydrodynamics in high-density riser and downer[D].Dongying:China University of Petroleum,2014.
[28]ZHU H,ZHU J.Characterization of fluidization behavior in the bottom region of CFB risers[J].Chemical Engineering Journal,2008,141(1/2/3):169-179.
[29]周发戚.CFB颗粒上行系统压力脉动特性的实验研究[D].北京:中国石油大学(北京),2013.ZHOU F Q.Experimental study on the pressure fluctuation of the upstream system in CFB[D].Beijing:China University of Petroleum,2013.
[30]周发戚,陈勇,魏志刚,等.循环流化床提升管T形弯头动态压力的小波分析[J].化工学报,2015,66(5):1697-1703.ZHOU F Q,CHEN Y,WEI Z G,et al.Wavelet analysis of dynamic pressure in T-abrupt of CFB riser[J].CIESC Journal,2015,66(5):1697-1703.
[2]杨勇林.低密度循环流化床气固两相流体力学行为的研究[D].北京:清华大学,1989.YANG Y L.Fluid flow structure in a dilute two-phase suspension system in a circulating fluidized bed[D].Beijing:Tsinghua University,1989.
[3]燕兰玲,祝京旭,蓝兴英,等.两种新型流化床——高密度循环流化床和循环湍动流化床的对比分析[J].化工学报,2014,65(7):2495-2503.YAN L L,ZHU J X,LAN X Y,et al.Comparative study of two novel fluidized beds—HDCFB and CTFB[J].CIESC Journal,2014,65(7):2495-2503.
[4]徐令宝.小型提升管冷模实验研究[D].北京:中国石油大学,2011.XU L B.Experimental study of mini-riser cold model[D].Beijing:China University of Petroleum,2011.
[5]GENG Q,WANG L,LI Z C,et al.Radial non-uniformity index research on high-density,high-flux CFB riser with stratified injection[J].China Petroleum Processing&Petrochemical Technology,2012,14(4):64-72.
[6]ZHU J,XU J,PENG B,et al.The effects of distributor design on the solids distribution in a CFB riser[C]//The 13th International Conference on Fluidization-New Paradigm in Fluidization Engineering.Art.53.Korea:ECI Digital Archives,2010:1-9.
[7]YAN A,P?RSSINEN J H,ZHU J X.Flow properties in the entrance and exit regions of a high-flux circulating fluidized bed riser[J].Powder Technology,2003,131(2):256-263.
[8]YOU J,WANG D,ZHU C.Entrance effects on gas-solid riser flow structure[J].Industrial&Engineering Chemistry Research,2008,48(1):310-319.
[9]CHENG Y,WEI F,YANG G,et al.Inlet and outlet effects on flow patterns in gas-solid risers[J].Powder Technology,1998,98(2):151-156.
[10]白丁荣,易江林,金涌,等.快速流化床入口结构对床层流动特性的影响[J].化工机械,1995,(2):10-14.BAI D R,YI J L,JIN Y,et al.Effects of inlet structure on bed flow characteristics in the fast fluidized bed[J].Chemical Engineering&Machinery,1995,(2):10-14.
[11]KIM J S,TACHINO R,TSUTSUMI A.Effects of solids feeder and riser exit configuration on establishing high density circulating fluidized beds[J].Powder Technology,2008,187(1):37-45.
[12]MARZOCCHELLA A,ARENA U.Hydrodynamics of a circulating fluidized bed operated with different secondary air injection devices[J].Powder Technology,1996,87(3):185-191.
[13]GRACE J R,ISSANGYA A S,BAI D,et al.Situating the high-density circulating fluidized bed[J].AICh E Journal,1999,45(10):2108-2116.
[14]ISSANGYA A S.Flow dynamics in high density circulating fluidized beds[D].Canada:The University of British Columbia Vancouver,1998.
[15]ISSANGYA A S,BAI D,BI H T,et al.Suspension densities in a highdensity circulating fluidized bed riser[J].Chemical Engineering Science,1999,54(22):5451-5460.
[16]ISSANGYA A S,BAI D,GRACE J R,et al.Flow behavior in the riser of a high-density circulating fluidized bed[C]//AICh E Symp.Ser.93.1999:25-30.
[17]ISSANGYA A S,GRACE J R,BAI D,et al.Further measurements of flow dynamics in a high-density circulating fluidized bed riser[J].Powder Technology,2000,111(1/2):104-113.
[18]ISSANGYA A S,ZHU J X,BAI D R,et al.Solids radial flux profiles in a high density circulating fluidized bed riser[C]//FluidizationⅨ.New York:Engineering Foundation,1998:197-204.
[19]郭慕孙.流态化手册[M].北京:化学工业出版社,2008.GUO M S.Handbook of Fluidization[M].Beijing:Chemical Industry Press,2008.
[20]李鹏飞,章敬泉,朱晓华.循环流化床入口结构对流态化效果影响比较[J].环境工程,2011,29(4):82-85.LI P F,ZHANG J Q,ZHU X H.Effect of entrance structure on fluidization of circulating fluidized bed[J].Environmental Engineering,2011,29(4):82-85.
[21]PENG B,ZHANG C,ZHU J,et al.New approaches to improve the uniformity of the radial solids concentration distribution in CFB risers[C]//Proceedings of the ASME 2012 Fluids Engineering Summer Meeting.FEDSM2012.Rio Grande Puerto Rico:ASME,2012:1351-1357.
[22]ZHANG H,JOHNSTON P M,ZHU J X,et al.A novel calibration procedure for a fiber optic solids concentration probe[J].Powder Technology,1998,100(2/3):260-272.
[23]黄卫星,漆小波,潘永亮,等.气固循环床提升管内的局部颗粒浓度及流动发展[J].高校化学工程学报,2002,16(6):626-631.HUANG W X,QI X B,PAN Y L,et al.Local solid-particle concentration and flow development in a long CFB riser[J].Journal of Chemical Engineering of Chinese Universities,2002,16(6):626-631.
[24]林海波,孔春林,黄卫星.气固循环流化床提升管颗粒速度和浓度的测量技术[J].四川理工学院学报(自然科学版),2002,15(4):28-33.LIN H B,KONG C L,HUANG W X.Measurement techniques of solids concentration and solids velocity in circulating fluid beds riser[J].Journal of Sichuan Institute of Light Industry and Chemical Technology,2002,15(4):28-33.
[25]漆小波.循环流化床提升管气固两相流动力学研究[D].成都:四川大学,2003.QI X B.Hydrodynamics of gas-solid two-phase flow in circulating fluidized bed risers[D].Chengdu:Sichuan University,2003.
[26]YAN A,P?RSSINEN J H,ZHU J X.Flow properties in the entrance and exit regions of a high-flux circulating fluidized bed riser[J].Powder Technology,2003,131(2):256-263.
[27]王成秀.循环流化床反应器的增浓——高密度提升管及下行床流体力学特性研究[D].东营:中国石油大学(华东),2014.WANG C X.Increasing the density of circulating fluidized bed reactors—hydrodynamics in high-density riser and downer[D].Dongying:China University of Petroleum,2014.
[28]ZHU H,ZHU J.Characterization of fluidization behavior in the bottom region of CFB risers[J].Chemical Engineering Journal,2008,141(1/2/3):169-179.
[29]周发戚.CFB颗粒上行系统压力脉动特性的实验研究[D].北京:中国石油大学(北京),2013.ZHOU F Q.Experimental study on the pressure fluctuation of the upstream system in CFB[D].Beijing:China University of Petroleum,2013.
[30]周发戚,陈勇,魏志刚,等.循环流化床提升管T形弯头动态压力的小波分析[J].化工学报,2015,66(5):1697-1703.ZHOU F Q,CHEN Y,WEI Z G,et al.Wavelet analysis of dynamic pressure in T-abrupt of CFB riser[J].CIESC Journal,2015,66(5):1697-1703.