Alcohol and/or ether propylene product separation method
A separation method and propylene technology, applied in absorption purification/separation, chemical instruments and methods, hydrocarbon purification/separation, etc., can solve the problems of poor economic effect and high energy consumption of devices, and reduce the consumption of refrigeration and energy consumption. Low, reduced process energy consumption
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Embodiment 1
[0031] See the process flow figure 1 . Methanol is converted into propylene as the main reaction product in the methanol-to-propylene reactor, and the gas phase hydrocarbon stream 1 is obtained after dehydration and acid gas carbon dioxide. Gas-phase hydrocarbon stream 1 has a temperature of 43°C, a pressure of 0.13MPa, and a molar composition of 18.7% carbon one to carbon two components, 45.9% carbon three components, 27.5% carbon four carbon five components, 7.9% carbon six and more Minute. The gas-phase hydrocarbon stream 1 is separated into low-pressure carbon five and lighter components 2 and carbon six and heavier components 12 in the pre-separation tower T1. The low-pressure carbon five and lighter component 2 are pressurized to 2 MPa through compressor C1 to obtain high-pressure carbon five and lighter component 3 and then sent to the desorption tower T2. In the desorption tower, 70.5% by mass of the carbon tricomponent is extracted from the bottom of the tower to obt...
Embodiment 2
[0034] The same process flow as in Example 1 was adopted. In the methanol-to-propylene reactor, it is converted into propylene as the main reaction product, and the gaseous hydrocarbon stream 1 is obtained after dehydration and acid gas carbon dioxide. Gas-phase hydrocarbon stream 1 has a temperature of 43°C, a pressure of 0.12 MPa, and a molar composition of 22.3% carbon one to carbon two components, 46.4% carbon three components, 24.3% carbon four carbon five components, 7.0% carbon six and more Minute. The gas-phase hydrocarbon stream 1 is pressurized to 0.55 MPa by a compressor, and then separated into low-pressure C5 and lighter components 2 and C6 and heavier components 12 in the pre-separation tower T1. The low-pressure carbon five and lighter component 2 are pressurized to 1.5 MPa through compressor C1 to obtain high-pressure carbon five and lighter component 3 and then sent to the desorption tower T2. In the desorption tower, 72.7% of the carbon tri-component is extr...
Embodiment 3
[0037] The same process flow as in Example 1 was adopted. Dimethyl ether is converted into propylene as the main reaction product in the dimethyl ether to propylene reactor, and the gas phase hydrocarbon stream 1 is obtained after dehydration and acid gas carbon dioxide. Gas-phase hydrocarbon stream 1 has a temperature of 43°C, a pressure of 0.14 MPa, and a molar composition of 21.5% carbon one to carbon two components, 46.9% carbon three components, 25.4% carbon four carbon five components, 6.2% carbon six and more. Minute. The gas-phase hydrocarbon stream 1 is separated into low-pressure carbon five and lighter components 2 and carbon six and heavier components 12 in the pre-separation tower T1. The low-pressure carbon five and lighter component 2 are pressurized to 1.7 MPa through compressor C1 to obtain high-pressure carbon five and lighter component 3 and then sent to the desorption tower T2. In the desorption tower, 72.9% of the carbon tri-component by mass is extracted...
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