Combined method for preparing ethylbenzene by fully utilizing refinery dry gas
A refinery dry gas and combined method technology, applied in the direction of chemical instruments and methods, hydrocarbons, hydrocarbons, etc., to achieve the effect of improving utilization rate, reducing equipment investment and energy consumption per unit product, and reducing the number of equipment
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Embodiment 1
[0066] In this embodiment, the FCC dry gas of the refinery is processed as a resource, and ethylbenzene is produced by utilizing ethane and ethylene therein. The composition of the FCC dry gas (mol.%): H 2 : 35.1,N 2 : 13.7, CO: 2.8, CO 2 : 1.7, CH 4 : 22.2, C 2 h 6 : 10.5, C 2 h 4 :12.8,C 3 h 8 : 0.2, C 3 h 6 : 0.7, C4+: 0.3, the process flow chart is as follows figure 1 shown.
[0067] The whole method of the present embodiment includes the following steps:
[0068] The dry gas raw material 1 is sent to the MDEA acid gas removal device 2 to obtain the acid gas 3 and the purified dry gas 4, wherein the H in the purified dry gas 4 2 S content is less than 20mg / Nm 3 , MDEA content is less than 1ppm. Pressurize the purified dry gas 4 to 1.70MPaG through the compressor 5 to obtain the pressurized purified dry gas 6, and then cool it to 10°C through the heat exchanger a 7 (to obtain the cooled and purified dry gas 8) and send it to the carbon dioxide absorption tower...
Embodiment 2
[0077] In embodiment 2, adopt the ethane and ethylene in the refinery FCC dry gas to produce ethylbenzene, FCC dry gas composition (mol.%): H 2 : 35.1,N 2 : 13.7, CO: 2.8, CO 2 : 1.7, CH 4 : 22.2, C 2 h 6 : 10.5, C 2 h 4 :12.8,C 3 h 8 : 0.2, C 3 h 6 : 0.7, C4+: 0.3, the process flow chart is as follows figure 1 Shown, embodiment 2 of the present invention comprises the following steps:
[0078] The dry gas raw material 1 is sent to the MDEA acid gas removal device 2 to obtain the acid gas 3 and the purified dry gas 4, wherein the H in the purified dry gas 4 2 S content is less than 20mg / Nm 3 , MDEA content is less than 1ppm. The purified dry gas 4 is pressurized to 2.50MPaG through the compressor 5, and the heat exchanger a 7 is cooled to 20° C. and then sent to the bottom of the carbon dioxide absorption tower 9. At the same time, the carbon dioxide absorber 10 (preferred in this embodiment) at 20° C. be ethylbenzene) into the top of the carbon dioxide absorptio...
Embodiment 3
[0087] The difference between embodiment 3 and embodiment 1 is:
[0088] The purified dry gas 4 is pressurized to 1.50MPaG, cooled to -20°C and sent to the bottom of the carbon dioxide absorption tower 9, the temperature of the absorbent ethylbenzene 10 is -20°C, and the desorption absorbent a 16 is cooled to -20°C by heat recovery After returning to the top of the carbon dioxide absorption tower 9;
[0089] The operating pressure of the carbon dioxide absorption tower 9 is 1.10MPaG, the tower top temperature is -17°C, and the tower bottom temperature is 0°C; the operating pressure of the carbon dioxide desorption tower 13 is 0.90MPaG, and the tower top temperature is 27°C. The temperature is 243°C;
[0090] The carbon-rich gas 15 is cooled to 10°C by the heat exchanger 18 and sent to the bottom of the propylene absorption tower 20, the temperature of the absorbent benzene 21 is 10°C, and the desorbing absorbent b33 is cooled to 10°C by heat recovery and then returned to the ...
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