Catalytic conversion method for preparing propylene and butylene
A catalytic conversion and catalytic cracking technology, which is applied in organic chemistry, hydrocarbon cracking to produce hydrocarbons, and hydrocarbon oil treatment, can solve the problems of small ethylene/propylene, low reaction selectivity, and flexible adjustment, so as to increase yield and suppress methane The generation and realization of the effect of effective utilization
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[0088] In a specific embodiment, the present disclosure also provides a method for producing olefin-rich feedstocks by dehydrogenation of alkanes, including:
[0089] Under catalytic dehydrogenation reaction conditions, alkane and dehydrogenation catalyst are contacted and reacted in a dehydrogenation treatment reactor to obtain alkene-rich feedstock.
[0090] Wherein, the dehydrogenation reaction conditions include: the inlet temperature of the dehydrogenation treatment reactor is 400-700°C, and the volumetric space velocity of the alkane is 200-5000h -1 , the pressure of the contact reaction is 0-0.1MPa.
[0091] Wherein, the dehydrogenation catalyst is composed of a carrier, active components and auxiliary agents supported on the carrier; optionally, based on the total weight of the dehydrogenation catalyst, the content of the carrier is 60-90% by weight, The content of the active component is 8-35% by weight, and the content of the auxiliary agent is 0.1-5% by weight;
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Embodiment 1
[0146] see figure 1 The procedure shown was tested on a mid-scale unit of a riser reactor.
[0147] The heavy oil I and the high temperature catalytic conversion catalyst I (≥650°C) are contacted at the bottom of the first reaction zone, the reaction temperature is 600°C, the reaction pressure is 0.1MPa, the reaction time is 3 seconds, and the weight ratio of the catalyst to the raw material is 5:1. Conversion reaction; 1-pentene and catalytic conversion catalyst I (stream from the first reaction zone) are contacted at the bottom of the second reaction zone, at a reaction temperature of 530 ° C, a reaction pressure of 0.1 MPa, a reaction time of 10 seconds, the catalyst and the raw material The catalytic conversion reaction occurs at a weight ratio of 45:1, and the ratio of 1-pentene to heavy feedstock is 1:9.
[0148] The reaction product of the reaction and the catalyst to be formed are separated, the obtained catalyst to be formed is introduced into the regenerator togethe...
Embodiment 2
[0154] see figure 1 The procedure shown, was tested on a mid-scale unit of a riser reactor.
[0155] The heavy oil I and the catalytic conversion catalyst I are contacted at the bottom of the first reaction zone, the reaction temperature is 600 ° C, the reaction pressure is 0.1 MPa, the reaction time is 3 seconds, and the catalytic conversion reaction occurs under the weight ratio of the catalyst to the raw material 5:1, and the reaction is separated. The reaction product and the to-be-generated catalyst are introduced into the regenerator together for coke regeneration, and the obtained reaction product is introduced into the combined separation system together to obtain a stream comprising ethylene, propylene, butene, olefin-rich streams and a stream with a boiling point greater than 250°C. The second catalytic cracking distillate oil and other products, the catalytic cracking distillate oil and hydrogenation catalyst IV are at 350 ° C, hydrogen partial pressure 18 MPa, volu...
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Abstract
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