乙炔二聚合成乙烯基乙炔外循环型鼓泡式反应器

乙炔二聚合成乙烯基乙炔（ＭＶＡ）的４种鼓泡式反应器，其效果按填料型，外循环型，直筒标准型，内循环型顺序递减。ＭＶＡ／ＤＶＡ（二乙烯基乙炔）与乙炔气体空塔线速Ｕｇ和乙炔部转化率ｘ的关联式为：对单管外循环型，ＭＶＡ／ＤＶＡ＝１．１９２８Ｕｇ０．６６０７Ｘ－０．０８１８；对直筒标准型，ＭＶＡ／ＤＶＡ＝１．５５１８Ｕｇ０．４３６８ｘ－０．０６０８。外循环型鼓泡式反应器的液体空塔线速Ｕ１与Ｕｇ的关联式为Ｕ１     

三相淤浆床冷态特性研究—气体—石腊油—催化剂系统

本文研究了气体－石腊油－催化剂三相体系在淤浆床反应器中的流体力学特性，考察了各种因素对气含率和压降的影响，并回归得到如下关联式：εｇ＝０．１１５２ｕｇ＾０．４１ｃｓ＾０．０９３ρ＾０．０１８。     

并流下行循环流化床反应器中的气固传质特性

采用稳态吸附方法，测定了示踪剂在下行式流化床反应器中的轴向浓度分布，并与理论分布进行拟合，利用Ｍａｒｑｕａｒｄｔ法，求取了不同操作条件下的轴向扩散系数与气固传质系数，藉以揭示并流下行循环流化床反应器中的气固传质特性．基于实验结果，通过因次分析与线性回归，得到了轴向扩散系数Ｅａ及传质系数ＫＦａ与操作条件的经验关联式：Ｐｅ１≡（Ｌｕｆ）／Ｅａ＝０．２２６Ｒｅ０．４９９ＰΘ－０．３０２Ｐｅ２≡ｕｆ／（ＫＦａ．Ｌ）＝０．０００１８５Ｒｅ０．６１８ｐΘ－０．９８３Θ≡Ｇｓ／（ｕｆρｐ）＝ｕｓ（１－ε）／（ｕｇε）关联式与实验数据拟合较好．     

喷流床中喷动气入口出料规律的研究

在φ３００ｍｍ的喷流床中,用砂作流化颗粒,以空气作为流化和喷动气、考察了流化气速、喷动气速、静床高、大颗粒深度及锥形气体分布器开孔率等对大颗业在喷动气入口管出料的影响,从而提出大颗粒下料速率的经验关联式为ｖｐ＝１．９５３×１０＾－９ｃｂ（Ｕｓ／ｕｔ）＾－１４．３５ｅｘｐ（－１．３２Ｕｔ／Ｕｍｆ）维持喷动流化床不出料的最小喷动气速计算式为Ｕｓｍｉｎ／ｕｔ＝０．２３１Ｕｔ／Ｕｍｆ＋０．７７１。     

带水平吹气管L阀的特性及公式

针对带水平吹气管Ｌ阀吹气量、水平管吹气管的伸入深度、管径以及不同高度吹气口地循环流化床（ＣＦＢ）固体颗粒循环的影响进行了研究。根据实验数据得出适合于带有水平吹气管Ｌ阀的经验关联式Ｇ２／Ａ＝０．０１５６ＣＤ√２ｐｓ（１－εｍｆ）△ＰＬＶ（１－ＸＬ）＾０．３３３（ＵＬ／Ｕｔ）＾０．８１８。     

多管环流反应器的气含率研究

提出了一种新型结构的多管式环流反应器,对于空气－水体系,在每个上升管气速为０～０．１６ｍ／ｓ和管径比Ｄｄ／Ｄｒ＝０．３～１．０范围内,研究了两个上升管气速及不同管径比时上升管气含率的变化规律,同时研究了分离箱中静液高及分离箱结构参数与下降管气含率之间的关系。提出了在鼓泡流区域内上升管气含率模型方程：Ｅ１＝αＵｂｇ１－ｃＵｇ３     

多段内导流筒气升式反应器中气体分布器对气含率和气液传质特性的影响

在为微生物高密度培养而设计的１０Ｌ多段内导流筒气升式生物反应器中，研究了Ｎａ２ＳＯ３－空气体系单孔喷嘴和烧结金属管等不同气体分布器对气含率ε、体积氧传质系数ＫＬａ和流动特性的影响．结果表明，孔径为２０～２５μｍ的烧结金属管的整体性能最好，在最佳操作气速３．７～４．０ｃｍ／ｓ下，ε超过１９％，ＫＬａ可达０．２９ｓ－１．其ε和ＫＬａ随Ｕｇ有如变化规律：ε＝０．１９５２－１．５３５１０－２ｅ－１．３９１ＵｇＫＬａ＝０．２７＋２．９７１０－２Ｕｇ－７．２３１０－３Ｕ２ｇ（１．５＜Ｕｇ＜６ｃｍ／ｓ     

通气式搅拌釜功率消耗的探讨

评估了通气式搅拌釜较有代表性的搅拌功耗关联式，指出大气穴形成之前，气体再循环将导致关系联式预测值偏离实际值４０％以上。用气体再循环系数对关联式进行修正，可得到适用于装有涡轮搅拌器的低粘体系的新的搅拌功耗关联式：当Ｇ≤２．５４时，Ｐｇ／Ｐ０＝０．７１Ｇ－０．８０；当Ｇ〉２．５４时，Ｐｇ／Ｐ０＝１．０；式中，Ｇ＝（Ｎｐ０／Ｎｐ０＾＊）＾０．６（ｄ／Ｄ）＾０．１５Ｆｒ＾０．０５［（１＋α）Ｎｑ］＾－０．     

液固流态化两元粒子的逆转现象研究

对两元混合粒子体系的液固流态化中的逆转现象进行了研究，定义了两元混合粒子在床中的混合程度，在实验的基础上提出两元混合粒子体系的混合程度Ｍ的关联式为：Ｍ＝１．４０８（１－ｘ２）／ｘ２）＾０．１６５（ｄｐ２／ｄｐ１）＾０．３１５（Ｕ／Ｕｔ１）＾０．９１并利用随机游动模型计算文献及本研究的实验数据，经多元线性回归得到液固两元粒子混合体系的临界逆转速度为Ｕｃ＝２．３３１（ρＰ２／ρＰ１）＾１．４８４（ｄＰ     

用先锋优质褐煤制取活性炭的研究

利用云南先锋优质褐煤，采用优化工艺制备出碘值大于８００ｍｇ／ｇ，比表面积１３３５．５ｍ＾２／ｇ和孔容积０．７８５ｍｌ／ｇ的活性炭。进行了ＣＯ２气体的饱和吸附，快速吸附和脱附试验；在不同ｐＨ值下对水中Ｃｒ＾６＾＋的吸附能力和Ｆｒｅｕｎｄｌｉｃｈ等温线评价试验：Ｋ＝３６．３，１／ｎ＝０．６９１，最佳ｐＨ＝５。     

EFFECTS OF AERATED LIQUID LEVEL ABOVE DOWNCOMER ON HYDRODYNAMIC CHARACTERISTICS OF AN EXTERNAL-LOOP AIRLIFT REACTOR

Effects of the aerated liquid level above the downcomer on riser superficial liquid velocity, gas flow rates, and gas holdups in individual sections were investigated in an external-loop airlift reactor. The aerated liquid level is an important operating parameter, and the valve connected to the extension tube could adjust it. As the aerated liquid level was increased up to 0.158 m, which was slightly larger than the diameter of the riser, both the liquid circulation velocity and the gas flow rate in the extension tube increased, whereas the riser gas holdup, the downcomer gas holdup, and the gas flow rate in other individual sections except the extension tube decreased. A combination of the gas-liquid separation ability and hydraulic resistance of the head region and the surface aeration could explain the impact of the aerated liquid level on the hydrodynamic characteristics. However, the effect was negligible when the aerated liquid level was higher than 0.158 m.     

EFFECTS OF AERATED LIQUID LEVEL ABOVE DOWNCOMER ON HYDRODYNAMIC CHARACTERISTICS OF AN EXTERNAL-LOOP AIRLIFT REACTOR

Effects of the aerated liquid level above the downcomer on riser superficial liquid velocity, gas flow rates, and gas holdups in individual sections were investigated in an external-loop airlift reactor. The aerated liquid level is an important operating parameter, and the valve connected to the extension tube could adjust it. As the aerated liquid level was increased up to 0.158 m, which was slightly larger than the diameter of the riser, both the liquid circulation velocity and the gas flow rate in the extension tube increased, whereas the riser gas holdup, the downcomer gas holdup, and the gas flow rate in other individual sections except the extension tube decreased. A combination of the gas-liquid separation ability and hydraulic resistance of the head region and the surface aeration could explain the impact of the aerated liquid level on the hydrodynamic characteristics. However, the effect was negligible when the aerated liquid level was higher than 0.158 m.     

加压气升式内环流反应器流动特性

在连续进料的操作条件下,选用水、氮气等作为实验介质,在Φ600mm?000mm的耐压不锈钢环流反应器内进行了实验。获得了下降环隙以及中心导流筒气含率的实验数据,并根据所获得的实验数据给出了中心导流筒以及下降环隙的关联式。从能量衡算的角度出发,对中心气升式加压环流反应器进行了理论分析,根据能量平衡推导出了连续操作模式下液相循环速度模型。同时根据实验所获得的数据确定了模型参数,通过计算可以发现,循环液速会随空塔气速以及体系压力的增加而增大,但是液相循环速度不会随着这两个操作工况无限制的变化,当体系压力与空塔气速大于某个值之后,液相循环速度的基本趋于平缓     

环隙气提式环流反应器中的气含率和液相循环流动

在筒体直径310mm、高2000mm的环隙气提式环流反应器实验装置中,对上流区的气含率、液相循环流动等流体力学特性作了研究.用漂流通量模型描述了上流区的气含率;通过对体系的能量耗散机理进行分析,基于体系总能耗最小的原理推导出液相循环流动方程,结果表明:用此方程能较好地模拟这种反应器内的液相循环状况.     

三相连续环流反应器中氧的液相传质过程

在空气-水-玻璃珠三相连续操作环流反应器中,利用动态溶氧方法研究了表观气速(Ug=0.01~0.13 m/s)、进料浆速(USL=0.001~0.011 m/s)、浆相质量固含率(es=0~30%, w)和固相颗粒大小(dp=59, 200 mm)对环流反应器内氧的液相传质性能的影响. 结果表明,在考察范围内,环流反应器传质系数随表观气速增大而增大,受进料浆速变化的影响较小,随浆相固含率增大呈现先增大后减小的趋势,但在高固含率下(es≥10%, w)的影响不显著;随固相颗粒粒径增大而减小. 同时得到了液相体积传质系数的经验关联式.     

EFFECTS OF GEOMETRY ON HYDRODYNAMICS IN EXTERNAL-LOOP AIRLIFT REACTORS

Experimental investigations were carried out in model external-loop airlift reactors. Two reactors of laboratory scale (riser liquid height ranged between 1.16-1.56 m, riser diameter 0.03 m, A_D/A_R ratio between 0.111-1,000, total liquid volume V_T = (1.189-2.446).10^-3m³) and pilot-plant scale (riser liquid height of 4.4 and 4.7 m, respectively, riser diameter 0.200 m, A_D/A_R ratio of 0.1225 and 0.040 m, total liquid volume, V_T = (0.144-0.170) m³) were used.

The influences of reactor geometry characterized by some parameter as: A_D/A_R ratio, liquid height in riser and downcomer and liquid height in gas separator, together with the amount of introduced air, on the basic hydrodynamic design parameters: gas holdup and liquid circulation velocity were analysed.

The influence of gas sparger design on gas holdup and liquid velocity was found to be negligible.

The experimental liquid circulation velocity was correlated using a simplified form of the energy balance in airlift reactors, valid for external-loop airlift reactors with almost complete phase separation at the top.

An original dimensionless correlation for gas holdup prediction involving superficial velocities of gas and liquid, cross sectional areas, dispersion height, riser diameter, as well as Froude number, was obtained.     

78.5升气升式环流反应器内构件优化

研究了78.5L气升式环流反应器内部结构对流动性能的影响规律, 并给出最佳区间来为工业装置提供理论指导。利用Fluent软件建立数学模型与实验装置作对比, 模拟了不同气液分离区高度与外筒高度比、导流筒长度与外筒长度比和筒内外直径比对流动行为的影响规律。结果表明:数学模型和实验结果误差较小, 可以用来预测气升式环流反应器流动行为。气液分离区高度与外筒高度比值过大会导致环流阻力增大, 从而不利于流动, 比值为0.34~0.36时流动性能最佳;导流筒长度与外筒长度的比值增大可增加气含率和环流液速, 但是比值过大会引起气泡的聚合, 从而影响流动性能, 当比值为0.60~0.62时流动性能最佳;在一定范围内增加内外筒直径比会改善流动效果, 但环隙面积过小会增加环形阻力, 内外筒直径比为0.73~0.77时流动效果比较理想。     

气升式内循环反应器的数值模拟和结构参数

采用Euler-Euler双流体模型对内循环反应器(高1240 mm,直径165 mm,导流筒高590 mm)进行数值模拟,考察了表观气速、导流筒结构(导流筒内径比Dt/D,底隙高度)对反应器内上升区、下降区流体力学参数(气含率、液体速度)的影响. 结果显示,表观气速、导流筒内径、底隙高度对反应器气含率、液体速度有很大影响,随表观气速增加,反应器上升区、下降区气含率都增加,导流筒内径比为0.58时更易实现气液循环,底隙高度为30 mm时反应器内下降区气含率、气液速度都最小;气液分离器角度越大,进入下降区的气体越多,当气液分离器角度为45o时,能更好地实现气液循环.     

Liquid circulation hydrodynamics in an external loop airlift reactor

The radial profiles of axial liquid velocity and gas hold‐ups are investigated in the riser of a pilot plant scale external loop airlift reactor (ELAR) using a modified Pavlov tube and differential pressure technique. The experimental investigation reveals that there exist two different kinds of liquid circulation structures in an ELAR, which has rarely been reported in the literature, namely internal liquid circulation, which exists only in the riser and external liquid circulation, which circulates through the downcomer. A power–law relationship is used to correlate the gas hold‐up and superficial gas velocity, which gives good agreement with experimental data. Experiments for axial liquid velocity profiles are analysed in analogy to a model described for a conventional bubble column. The results predicted by the model are in excellent agreement with the experimental data obtained under various operating conditions. © 2011 Canadian Society for Chemical Engineering