Alkylation of benzene and/or toluene with methanol
A technology of alkylation and toluene, which is applied in the field of improving the selectivity of para-xylene, and can solve the problems of deactivation of zeolite catalysts and the like
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Embodiment 1
[0031] A pilot scale test was conducted using a fluidized bed reactor as discussed in US Pat. No. 6,642,426 and a type of fluidized bed regenerator system known per se in the art. The fluidized bed reactor has a diameter of 10.2 cm (4 inches) and a height of 8.2 m (27 feet). The regenerator has a diameter of 15.2 cm (6 inches) and a height of 25.4 cm (10 inches). The fluidized bed catalyst used contained approximately 4 wt% phosphorus and 10 wt% 450 / 1 SiO in a binder comprising silica-alumina and clay 2 / Al 2 o 3 ZSM-5 zeolite. The catalyst was then steamed at about 1030°C for about 45 minutes before being introduced into the reactor. The reactor and regenerator were operated at 1100°F (about 593°C) and 20 psig (about 138 kPa). Water was also co-fed (cofe). The catalyst recycle rate was about 104 lb / hr (47.2 kg / hr). The results are shown in figure 2 , described below. Most conveniently, the amount of coke on the catalyst can be determined by taking a sample of the cat...
Embodiment 2
[0034] The reactor / regenerator in Example 1 above was run under the same initial conditions and the catalyst circulation rate was reduced from 104 lb / hr to 12 lb / hr (5.4 kg / hr) over time. as in image 3 As shown in , the p-xylene selectivity increased from 88% to 90%.
Embodiment 3
[0036] The same reactor / regenerator and coke on catalyst were increased from 0.5% to 5% in the above example run under the same initial conditions. as in Figure 4 As shown in , the C11+ yield was analyzed over the same time frame and showed a decrease from 0.45% to 0.2% (wt%, based on hydrocarbons in the effluent).
[0037] The alkylation process employed herein may employ any aromatics feed comprising toluene and / or benzene, although it is generally preferred that the aromatics feed comprise at least 90 wt%, especially at least 99 wt% benzene, toluene or mixtures thereof. Aromatics feeds comprising at least 99 wt% toluene are particularly preferred.
[0038] Similarly, while the composition of the feed comprising methanol is not critical, it is generally desirable to employ a feed comprising at least 90 wt%, especially at least 99 wt% methanol.
[0039] The catalyst employed in the process may be any catalyst suitable for converting benzene and / or toluene and methanol to x...
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Abstract
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