A method for catalytic conversion of hydrocarbons with multiple yields of light olefins and light aromatics
A technology for low-carbon olefins and light aromatic hydrocarbons, which is applied in the field of hydrocarbon catalytic conversion, can solve the problems of increasing selectivity and the limitations of catalytically cracked propylene, etc., and achieves the effect of inhibiting hydrogen transfer reaction and high process flexibility.
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Embodiment 1
[0092]The cracking catalyst used in this embodiment is: based on the total weight of the cracking catalyst, the cracking catalyst used contains 10% by weight of beta zeolite, 20% by weight of ZSM-5 zeolite (the ratio of silicon to aluminum is 40), 45% by weight of Kaolin and 25% by weight of alumina binder, wherein the beta zeolite contains 1% by weight of iron and 1.5% by weight of phosphorus in terms of elements. The cracking catalyst is aged for 10 hours at 800°C and 100% water vapor atmosphere, and the catalyst loading in the device (system catalyst storage) is 60 kg.
[0093] The heavy hydrocarbon oil raw material (its properties are shown in Table 1) is introduced into the riser reactor 1, and after being contacted with the hot catalyst from the regenerator 6, the reaction oil gas is separated from the catalyst, and the reaction oil gas leaves the reactor and is introduced into the fractionation device, separated The obtained coke catalyst is introduced into the stripper...
Embodiment 2
[0095] The process flow and the cracking catalyst used in this example are the same as in Example 1, except that light gasoline (see Table 2 for properties) is used at a reaction temperature of 40°C, a reaction pressure of 0.5MPa, and a molar ratio of hydrogen to olefins of 4:1. After selective hydrogenation reaction on the hydrogenation catalyst (purchased from Sinopec Changling Catalyst Branch, the brand is RDD-1), dienes and alkynes are converted into monoolefins and introduced into riser reactor 2, and the remaining reaction conditions and The reaction results are shown in Table 4.
Embodiment 3
[0101] The flow process of this embodiment is the same as that of Example 1. The difference is that the cracking catalyst used is: based on the total weight of the cracking catalyst, the cracking catalyst used contains 15% by weight of zeolite beta, 15% by weight of ZSM-5 zeolite (silicon Aluminum ratio is 40), 45% by weight of kaolin and 25% by weight of alumina binder, wherein, zeolite beta contains 1% by weight of iron and 1.5% by weight of phosphorus in terms of elements; and, reaction conditions and reaction results See Table 6.
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