CIESC Journal ›› 2019, Vol. 70 ›› Issue (5): 1858-1867.doi: 10.11949/j.issn.0438-1157.20181245

• Process system engineering • Previous Articles     Next Articles

CFD simulation on hydrogenation of acetylene to ethylene in slurry bed

Wu SU(),Xiaogang SHI,Yingya WU,Jinsen GAO,Xingying LAN()   

  1. State Key Laboratory of Heavy Oil Processing, China University of Petroleum, Beijing 102249, China
  • Received:2018-10-22 Revised:2019-02-21 Online:2019-05-05 Published:2019-05-10
  • Contact: Xingying LAN E-mail:suwucup@163.com;lanxy@cup.edu.cn

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Abstract:

The simulation of hydrogenation of acetylene in slurry reactor was carried out. The TFM-PBM coupling method was used to describe the flow of gas phase and slurry phase in slurry bed, and the kinetics of acetylene hydrogenation reaction was coupled to establish flow-reaction synthesis. The model was validated in a lab-scale slurry bed reactor and was then applied to the simulation of a bench-scale slurry bed reactor with respect to the function mechanisms of internals and the effects of operating conditions. Simulation results showed that vertical tube in the bench-scale reactor can break up bubbles and suppress the radial flow of gas phase, which benefits the uniform and sufficient conversion of acetylene. The conversion of acetylene is closely related to the residence time of gas phase and the reaction temperature. In order to obtain complete conversion of acetylene and high selectivity of ethylene when the slurry bed reactor was scaled-up to an industrial scale, it is critical to control the reaction temperature and the residence time of gas phase which can be regulated by changing the height of the liquid phase.

Key words: slurry bed, hydrogenation of acetylene, CFD, multiphase flow, multiphase reactor

CLC Number: 

  • TQ 021.1

Fig.1

Geometric structure of bench-scale slurry bed reactor"

Table 1

Equipment parameters and operating conditions"

项目 催化剂量/kg 催化剂浓度/%(vol) 气体流量/(m3/h) 入口H2:C2H2 (vol.) 压力/kPa 温度/℃
小试装置 0.002 2.4 0.09 4:01 101 150
中试装置 13 2 165, 300 4.45:1 450 123, 140

Table 2

Mesh independency"

项目 网格数/万 床层平均气含率 乙炔转化率/% 乙烯选择性/%

小试装置[border:border-top:solid;]

 0.54 0.112 93.49 97.42
1.15 0.118 93.08 95.13
3.56 0.120 93.36 95.75

中试装置

 4.5 0.211 97.84 91.42
24 0.203 99.43 85.88
34 0.207 99.65 89.60

Table 3

Comparisons between simulation results and experimental data in lab-scale equipment"

项目 床层整体气含率 C2H2转化率/% C2H4选择性/%
实验结果 0.125 100 95.51
模拟结果 0.118 93.08 95.13

Fig.2

Instantaneous iso-surface of gas hold-up (α g=0.15)"

Fig.3

C2H2 and C2H4 concentration at different heights"

Table 4

Comparisons between simulation results and experimental data in bench-scale equipment"

项目 工况1 工况2
实验结果 模拟结果 实验结果 模拟结果
温度/℃ 140 123
气体流量/(m3/h) 300 165
床层平均气含率 0.19 0.20 — 0.12
C2H2转化率/% 98.71 99.43 98.34 90.91
C2H4选择性/% 91.04 85.88 92.14 85.24

Fig.4

Instantaneous distribution of gas hold-up"

Fig.5

Instantaneous iso-surface of gas hold-up"

Fig.6

Radial distribution of time-averaged gas hold-up"

Fig.7

Radial distribution of time-averaged gas axial velocity"

Fig.8

Radial distribution of time-averaged liquid axial velocity"

Fig.9

Radial distribution of mean bubble size at different heights"

Fig.10

Axial distribution of C2H2 conversion"

Fig.11

Axial distribution of C2H4 mole fraction"

Fig.12

Axial distribution of C2H2 mole fraction under different condition"

Table 5

Conversion of C2H2 and selectivity of C2H4 at outlet"

项目 C2H2转化率/% C2H4选择性/%
工况1 99.43 85.88
工况3 99.99 69.49

Fig.13

Axial distribution of C2H2 and C2H4 mole fraction"

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