FIGURE CAPTIONS
FIGURE 1 Comparison of the overall atom economy and per pass
yield of cyclohexanol/cyclohexanone of the current industrial processes
and the novel cyclohexene esterification–hydrogenation process from
benzene.
FIGURE 2 (A) Effects of reaction temperature and acetic
acid/cyclohexene molar ratio on cyclohexene conversion in cyclohexene
esterification, and (B) a plot of lnK against 1/T .
FIGURE 3 Influence of the acetic acid/cyclohexene molar ratio
on the esterification rate of cyclohexene at various reaction
temperatures. The curves are simulated by the LHHW-type kinetics model.
FIGURE 4 The chromatogram of the hydrogenation products of
cyclohexyl acetate over the
Cu1Zn1Si2La0.1catalyst.
FIGURE 5 (A) The XRD patterns of the
Cu1Zn1Si2 and
Cu1Zn1Si2La0.1catalysts, (B) the HRTEM image, (C) the TEM image and particle size
distribution histogram, (D) the HAADF–STEM image and the corresponding
EDS mappings of (E) Si, (F) Cu, (G) Zn, (H) La, and (I) the overlapping
of these elements of the
Cu1Zn1Si2La0.1catalyst.
FIGURE 6 (A) The long-term evolutions of the conversion of
cyclohexene and the selectivity to cyclohexyl acetate in the
esterification of cyclohexene with acetic acid on the pilot-scale
reactive distillation reactor. Reaction conditions: reboiler duty of
1050 W, total reflux at ambient pressure, acetic acid feed at the top of
the column at 2.59 kg h–1, cyclohexene feed at the
middle of the catalytic section at 3.54 kg h–1, and
total catalyst loading of 2.65 kg, and (B) the long-term evolutions of
the conversion of cyclohexyl acetate and the selectivities to
cyclohexanol and ethanol in the hydrogenation of cyclohexyl acetate on
the pilot-scale fixed-bed reactor. Reaction conditions: temperature of
473 K, pressure of 6.2 MPa, H2 flow rate of 100 L
min–1, cyclohexyl acetate feed rate of 870 g
h–1, and catalyst loading of 1.0 kg.