图共 8个 表共 4
    • 图  FIG. 215.  FIG. 215.

      Figure FIG. 215..  FIG. 215.

    • 图  1  碘硫循环流程图

      Figure 1.  Iodine sulfur cycle flow chart

    • 图  2  H2O-HI气液平衡相图与实验点的对比

      Figure 2.  Comparison of H2O-HI vapor-liquid equilibrium phase diagram and experimental point

    • 图  3  HI-I2-H2O体系相平衡预测图(p=101.325 kPa)

      Figure 3.  Phase equilibrium prediction chart of HI-I2-H2O system (p=101.325 kPa)

    • 图  4  EED工艺的HI精馏流程图

      Figure 4.  HI distillation flow chart of EED process

    • 图  5  精馏塔内的模拟计算结果分布图

      Figure 5.  Distillation column simulation calculation results distribution map

    • 图  6  塔板数对精馏效果的影响曲线图

      Figure 6.  Effect of the number of plates on the rectification performance

    • 图  7  回流比对精馏效果的影响曲线图

      Figure 7.  Effect of reflux ratio on rectification performance

    • ComponentAia, ibAib, iaBia, ibBib, iaCia, ib
      iaib
      H2OHI2.080−1.702371.843−1.133×1030.300
      H2OH2O2.4222.603−297.437−1.921×1030.300
      HIHI4.529−3.1362.379×103892.9880.300

      表 1  NRTL方程的二元交互作用参数

      Table 1.  Binary interaction parameters of NRTL equation

    • MESH equationMaterial balanceEquilibriumNormalizationHeat balance
      VL phase$\normalsize { { \begin{aligned} &{V_{ {j }+ 1} }{y_{ {j + 1,i} } } + {L_{ {j} - 1} }{x_{ {j} - 1,{i} } }+\\ & {F_{j} }{z_{ {i,j} } } - \left( { {V_{j} } + S_{j}^{\rm{V}} } \right){y_{ {j,i} } }-\\ & \left( { L_{j} + S_{j}^{\rm{L}} }\right){x_{ {j,i} } } = 0 \end{aligned} } }$$\normalsize{ { y_{{j, i}}=K_{{j, i}} x_{{j, i}} }}$$ \normalsize{ { \begin{aligned} &{\sum\limits_{ {i} = 1}^3 {y_{ {j,i} } } = 1}\\ &{\sum\limits_{ {i} = 1}^3 {x_{ {j,i} } } = 1} \\ & {} \\ & {} \end{aligned} } } $$ \normalsize{ { \begin{aligned} &{ V_{ {j} + 1} H_{ {j} + 1}^{\rm{V} } + {L_{ {j} - 1} }H_{ {j} - 1}^{\rm{L} } }-\\& { {V_{j} }H_{j}^{\rm{V} } - {L_{j} }H_{j}^{\rm{L}} + {F_{j} }H_{j}^{{F} } = 0} \end{aligned} } } $

      表 2  气液两相MESH方程

      Table 2.  MESH equations of vapor-liquid(VL) phase

    • SamplesVolume flow/(m3·h–1)Enthalpy/(kJ·kg–1)Mass flow/(kg·h–1)Mass fraction
      HIH2OI2HIH2OI2
      F10149.040−843.6622.436×1052.218×1041.179×1050.3070.0580.635
      F1171.48573.7611.748×1053.623×10−22273.8830.9972.591×10−270.003
      F1296.459−1.498×1036.875×1042.218×1041.176×1050.3300.1060.564

      表 3  精馏塔进出料模拟计算结果

      Table 3.  Simulated calculation results of feed and discharge in distillation column

    • n(HI)∶n(I2)∶n(H2O)HI mass fraction of distillationQ/kW
      0.129∶0.342∶0.5299.970×10−10–598
      0.137∶0.315∶0.5489.974×10−10–572
      0.146∶0.313∶0.5419.973×10−10–577
      0.150∶0.315∶0.5359.972×10−10–582

      表 4  不同进料组分下HI精馏塔模拟结果

      Table 4.  Simulation results of HI distillation column of different feeds