Process for preparing low carbon olefine by adopting methanol or dimethyl ether
A low-carbon olefin and dimethyl ether technology, which is applied in the field of chemical material preparation, can solve the problem of loss of activity and achieve high selectivity, excellent catalytic performance, and high activity.
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Embodiment 1
[0036] Catalyst pretreatment: Add 10g of fresh SAPO-34 catalyst into a fixed-bed reactor with an inner diameter of 30mm. Based on the weight of the catalyst, the initial carbon content of the catalyst is 0, the reaction temperature is 350°C, and the absolute pressure is 1MPa. First purge with high-purity N2 for 30 minutes, with a nitrogen flow rate of 100ml / min, and then add the pretreatment gas from the bottom of the reactor. The component of the pretreatment gas is ethylene, its mass space velocity is 0.2 / h, and the feeding time lasts for 20 minutes. Purge with high-purity N2 for 30 minutes. The carbon content of the treated catalyst is shown in Table 1.
[0037] MTO reaction: Put the pretreated catalyst into a quartz tube fluidized bed reactor with an inner diameter of 20mm, maintain the reaction temperature at 450℃, and an absolute pressure of 0.15MPa. The raw material methanol is vaporized through the preheater and then passed into the reactor. The mass space velocity of met...
Embodiment 2
[0039] Catalyst pretreatment: Add 10g of regenerated SAPO-34 catalyst into a quartz tube fluidized bed reactor with an inner diameter of 20mm. Based on the weight of the catalyst, the initial carbon content of the catalyst is 0.1%, and the reaction temperature is 450°C. The pressure is 0.15MPa, first purged with high-purity N2 for 30 minutes, and the nitrogen flow rate is 300ml / min, and then the pretreatment gas is added from the bottom of the reactor. The pretreatment gas is composed of propylene and its mass space velocity is 1.5 / h. The feeding time lasted for 8 minutes, and then purged with high-purity N2 for 30 minutes. The carbon content of the treated catalyst is shown in Table 1.
[0040] The MTO reaction conditions are the same as in Example 1, and the diene selectivity in the gas phase product and the coke content in the used catalyst are shown in Table 1.
Embodiment 3
[0042] Catalyst pretreatment: Add 10g of regenerated SAPO-34 catalyst into a quartz tube fluidized bed reactor with an inner diameter of 20mm. Based on the weight of the catalyst, the initial carbon content of the catalyst is 0.1%, and the reaction temperature is 500℃. The pressure is 0.15MPa, first purged with high-purity N2 for 30min, the nitrogen flow rate is 300ml / min, and then the pretreatment gas is added from the bottom of the reactor. The component of the pretreatment gas is 1-butene and its mass space velocity is 2 / h, the feeding time lasts for 5 minutes, and then purges with high purity N2 for 30 minutes. The carbon content of the treated catalyst is shown in Table 1.
[0043] The MTO reaction conditions are the same as in Example 1. The diene selectivity in the gas phase product and the coke content in the used catalyst are shown in Table 1.
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