Energy recycling method for process for preparing propylene from oxygenated compounds
An energy recovery and compound technology, which is applied in the field of propylene production, can solve the problems of low energy utilization rate, large heating furnace load, and low overall energy efficiency level of the process, so as to improve the energy efficiency level of the process, deepen the heat exchange depth, and save energy. consumption effect
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[0022] Example 1
[0023] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=2.0h -1 , Using as figure 1 The process flow shown. The inlet gas temperature of the reactor 5 is 450°C, the temperature of the reaction product after compression by the compressor is 600°C, and the pressure is 0.70 MPa in gauge. The reaction product first exchanges heat with the stream flowing out of the pre-reactor 3 and heats it to 450 ℃, after passing through two-stage heat recovery unit of methanol vaporizer and circulating water preheater, the temperature out of the circulating water preheater is 130℃, enters the air cooler to be cooled to 30℃, and finally enters the phase separator to separate the oil and water , Qi three-phase. The water content of the exported gas hydrocarbon product is 0.2wt%, and the water content of the oil phase product is 0.6wt%.
[0024] Through this scheme, the stream flowing out of the pre-reactor 3 is directly heated ...
Example Embodiment
[0027] Example 2
[0028] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=1.0h -1 , Using as figure 1 The process flow shown. The inlet gas temperature of the reactor 5 is 400°C, the temperature of the reaction product after compression by the compressor is 550°C, and the pressure is 0.60 MPa in gauge pressure. The reaction product first exchanges heat with the stream flowing out of the pre-reactor 3 and heats it to 400 ℃, after passing through two-stage heat recovery unit of methanol vaporizer and circulating water preheater, the temperature out of circulating water preheater is 110℃, it enters air cooler to cool to 40℃, and finally enters phase separator to separate oil and water , Qi three-phase. The water content in the exported gaseous hydrocarbon product is 0.3wt%, and the water content in the oil phase product is 0.7wt%.
[0029] Through this scheme, the stream flowing out of the pre-reactor 3 is directly heated to 40...
Example Embodiment
[0032] Example 3
[0033] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=2.0h -1 , Using as figure 1 The process flow shown. The temperature of the inlet gas of the reactor 5 is 380°C, the temperature of the reaction product after compression by the compressor is 530°C, and the pressure is 0.55MPa in gauge. The reaction product first exchanges heat with the stream flowing out of the pre-reactor 3 and heats it to 380 ℃, after passing through two-stage heat recovery unit of methanol vaporizer and circulating water preheater, the temperature out of the circulating water preheater is 100℃, it enters the air cooler to cool to 40℃, and finally enters the phase separator to separate the oil and water , Qi three-phase. The water content in the exported gas hydrocarbon product is 0.35 wt%, and the water content in the oil phase product is 0.72 wt%.
[0034] Through this scheme, the stream flowing out of the pre-reactor 3 is directly...
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