Separation refining method for ethylene preparation through ethanol dehydration

A technology of ethanol dehydration and refining method, applied in the direction of distillation purification/separation, organic chemistry, etc., which can solve the problems of high energy consumption, complicated process, low recovery efficiency, etc., and achieve improved ethylene yield, good technical effect, and easy operation Effect

Active Publication Date: 2014-05-07
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

This process adopts a double-tower process, which has the problems of relatively complicated process and high energy consumption
The patent (ZL200710040705.64) proposes the method of adi

Method used

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  • Separation refining method for ethylene preparation through ethanol dehydration
  • Separation refining method for ethylene preparation through ethanol dehydration

Examples

Experimental program
Comparison scheme
Effect test

Example Embodiment

[0018] [Example 1]

[0019] The crude ethylene from the ethylene drying system enters the ethylene rectification tower for separation, the ethylene containing light components is separated at the top of the tower, and the heavy components are separated at the bottom of the tower. The flow rate of each component of crude ethylene is: hydrogen 0.070 kg / h, methane 0.070 kg / h, carbon monoxide 0.557 kg / h, ethylene 1,274.518 kg / h, ethane 7.060 kg / h, propane 1.555 kg / h, acetaldehyde 0.113 kg / h Hour, ether 5.631 kg / h, heavy component 33.957 kg / h. The reorganization of the ethylene rectification tower bottom is 83.977 kg / h, of which ethylene is 18.618 kg / h. The vapor phase at the top of the ethylene rectification tower enters the bottom of the light-removing tower with a flow rate of 5060.536 kg / h. The top temperature of the ethylene rectification tower is -24.8°C, the pressure is 2.15MPaG, the bottom temperature is 9.5°C, the number of theoretical plates in the whole tower is 80, and t...

Example Embodiment

[0024] [Example 2]

[0025] Same as Example 1, only changing the theoretical number of stages of the ethylene rectification tower: the number of theoretical plates in the whole tower is 92, the feed position is in the middle and lower part, and the others are the same as in Example 1. The reorganization of the ethylene rectification tower bottom is divided into 84.035 kg / h, of which ethylene is 18.631 kg / h. The vapor phase flow rate at the top of the ethylene rectification tower is 5061.121 kg / h, the temperature at the top of the ethylene rectification tower is -24.8°C, the pressure is 2.15MPaG, and the bottom temperature is 9.5°C.

[0026] The material mainly containing ethylene steamed from the top of the stripping distillation tower is recycled into the lower part of the ethylene rectification tower with a flow rate of 34.036 kg / h. The bottom of the tower discharges mainly containing ethane and C 3 + The flow rate is 50.0 kg / h, which contains 1.686 kg / h of ethylene. The top tem...

Example Embodiment

[0030] [Example 3]

[0031] Same as Example 1, only changing the theoretical stages of the stripping distillation column: the theoretical plate number of the whole column is 20, and the others are the same as in Example 1. The reorganization of the ethylene rectification tower and the bottom is divided into 82.667 kg / h, of which ethylene is 18.327 kg / h. The vapor phase flow rate of the top of the ethylene rectification tower is 5059.727 kg / h, the top temperature of the ethylene rectification tower is -24.8°C, the pressure is 2.15MPaG, and the bottom temperature is 10.0°C.

[0032] The material mainly containing ethylene steamed from the top of the stripping distillation tower is recycled into the lower part of the ethylene rectification tower with a flow rate of 32.667 kg / h. The bottom of the tower discharges mainly containing ethane and C 3 + The flow rate is 50.0 kg / h, which contains 1.691 kg / h of ethylene. The top temperature of the distillation column is 10.1°C, the pressure i...

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Abstract

The invention relates to a separation refining method for ethylene preparation through ethanol dehydration, and mainly solves the problems of separation of products in ethylene preparation through ethanol dehydration, especially low ethylene yield and high energy consumption which exist in former literatures. A mixture containing ethylene, ethane and C3 and C3+ hydrocarbons and light components go into an ethylene rectification tower, light component-containing ethylene is separated out at the tower top, the gas phase goes into a light component-removing tower, and a heavy component rich in ethylene is discharged from a tower kettle; after the light component-containing gas-phase ethylene is rectified by the light component-removing tower, a tower top gas phase is congealed to separate out gas-phase light components, the congealed liquid is used as a reflux and returns to the light component-removing tower, a bottom liquid phase in the light component-removing tower is partially used as a reflux and sent to the top of the ethylene rectification tower through compression by a pump, and the rest is an ethylene product; the heavy component rich in ethylene goes into the top of a heavy component steam stripping distillation tower, a tower top gas phase of the steam stripping distillation tower returns to the middle-lower part of the ethylene rectification tower, and a heavy component containing a little ethylene is obtained at the tower bottom. With adopting of the above technical scheme, the problems in the prior art are relatively well solved, and the separation refining method can be used for industrial production of ethylene preparation through ethanol dehydration.

Description

technical field [0001] The invention relates to a separation and refining method for producing ethylene by dehydrating ethanol. Background technique [0002] Ethylene is an important bulk organic chemical raw material, mainly used to produce polyethylene, polyvinyl chloride, ethylene oxide / ethylene glycol, ethylbenzene / styrene, vinyl acetate and other organic chemical products. At present, ethylene production methods at home and abroad are mainly produced by catalytic cracking of petroleum raw materials. In recent years, new breakthroughs have been made in the research on the production of ethylene from non-petroleum raw materials, especially the technology of ethanol dehydration to produce ethylene. This technology is based on ethanol derived from agricultural by-products, which can avoid dependence on petroleum resources. For countries and regions that are poor in oil and dominated by agriculture, the raw materials for ethanol production are easy to obtain and guaranteed...

Claims

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Application Information

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IPC IPC(8): C07C11/04C07C7/04C07C7/05
Inventor 邵百祥黄云群
Owner CHINA PETROLEUM & CHEM CORP
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