Low energy consumption method for producing propylene through catalytic reforming of Fischer-Tropsch synthesis oil
A Fischer-Tropsch synthetic oil and Fischer-Tropsch synthesis technology, applied in the production of bulk chemicals, chemical recovery, organic chemistry, etc., can solve the problems of low propylene yield, high energy consumption, unsuitable for olefin production, etc., and achieve high propylene Productivity, the effect of reducing energy consumption
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Embodiment 1
[0061] The purpose of this example is to illustrate the effect of the method provided by the present invention on separating the synthetic products obtained by the high-temperature Fischer-Tropsch synthesis process into different fractions of raw materials, each of which enters different reaction zones for catalytic cracking.
[0062] The experiment was carried out in a medium-sized riser catalytic cracking unit. Such as figure 1 As shown, the internal diameter of riser reactor 1 of this medium-sized device is 16 mm, and the length is 3800 mm. The internal diameter of riser reactor 2 is 16 mm, and the length is 3200 mm. The inner diameter of the fluidized bed reactor is 64 mm, and the height is 600 mm. The test is operated in a single pass mode. The high-temperature regenerant at 700°C is introduced into the bottom of riser reactor 1 and 2 from the regenerator through the regenerating inclined pipe, and flows upward under the action of the pre-lift medium. Raw material 1-1 i...
Embodiment 2
[0064] This example illustrates the effect that the catalyst introduced into the riser reactor 2 is a mixed catalyst of regenerated agent and spent agent.
[0065] The experimental setup is roughly the same as in Example 1. Raw material 1-1 is preheated to 120°C and mixed with atomized water vapor, then enters riser reactor 1 through the feed nozzle to contact with hot regenerant and undergoes catalytic conversion reaction, and the mixture of reaction oil gas and catalyst goes up, raw material 1 -3 After being preheated to 250°C and mixed with atomized water vapor, it enters the middle part of riser reactor 1 through the feed nozzle to contact with the upward reaction oil gas and catalyst mixture to carry out catalytic conversion reaction, and the formed reaction oil gas and catalyst The mixture continues to go up the riser reactor 1, and is separated from gas and solid through the rapid separation equipment installed at the outlet of riser reactor 1. The separated reaction oi...
Embodiment 3
[0071] As shown in Example 2, the difference is that the recycled pyrolysis light gasoline (distillation range 32~88°C) is mixed with raw material 1-2, preheated to 195°C by flue gas, and introduced into riser reactor 2 through the feed nozzle Lower part (introduced at the same height position as raw material 1-2). The mixture of reaction oil gas and catalyst goes up the riser reactor 2 and enters the fluidized bed reactor 3 through the outlet of riser reactor 2 to continue to participate in the cracking reaction. The reaction oil gas is introduced into the settler, and then introduced into the product separation system to be separated into gas and liquid products. The proportion by weight of refractory cracked light gasoline to the total feed (including raw material 1-1, raw material 1-2 and raw material 1-3) is 10%.
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