Separation refinement method for ethylene preparation through biomass ethanol dehydration

A technology of biomass ethanol and refining method, which is applied in the field of separation and refining of biomass ethanol dehydration to ethylene, which can solve the problems of ethylene loss and low recovery efficiency, and achieve the effects of reduced energy consumption for separation, easy operation, and improved purity of ethylene products

Active Publication Date: 2013-12-04
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Although this process can obtain 99.99% refined ethylene, there is a problem of ethylene loss due to the removal of light components by the process of stripping distillation tower and the failure to recover the ethylene in the heavy component stream.
The patent (ZL200710040705.64) proposes the method of adiabatic flash evaporation to recover ethylene in the still liquid of the ethylene rectification tower. Although part of the ethylene can be recovered, the recovery efficiency is not high

Method used

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  • Separation refinement method for ethylene preparation through biomass ethanol dehydration

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0016] Crude ethylene from the ethylene drying system enters the ethylene rectification tower for separation, ethylene containing light components is separated at the top of the tower, and 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 1274.518 kg / h, ethane 7.060 kg / h, propane 1.555 kg / h, acetaldehyde 0.113 kg / h Hours, ether 5.631 kg / hour, heavy component 33.957 kg / hour.

[0017] The heavy component of the ethylene rectification tower tank is 83.866 kg / hour, of which ethylene is 18.593 kg / hour, and the light component of the ethylene rectification tower top is 4712.040 kg / hour, of which ethylene is 4709.413 kg / hour. After condensation, it is divided into Two streams, the reflux of the ethylene rectification tower is 3438.507 kg / hour, the feed of the light component rectification tower is 1273.520 kg / hour, and the light components disch...

Embodiment 2

[0023] Same as Example 1, only change the theoretical number of stages of the ethylene rectification tower: the number of theoretical plates in the whole column is 92, the feeding position is in the middle and lower part, and the others are the same as Example 1.

[0024] The weight fraction of the ethylene rectification tower still is 83.939 kg / h, of which ethylene is 18.609 kg / h, the overhead reflux of the ethylene rectification tower is 3438.539 kg / h, and the feed to the light end rectification tower is 1273.531 kg / h. The temperature at the top of the ethylene rectification tower is -25.0°C, the pressure is 2.15MPaG, and the temperature at the bottom of the tower is 9.3°C. The heat load of the condenser of the ethylene rectification tower is 434.503kw.

[0025] The top temperature of the stripping distillation tower is 9.6°C, the pressure is 2.16MPaG, and the temperature of the bottom of the tower is 59°C. The material mainly containing ethylene evaporated from the top of t...

Embodiment 3

[0030] Same as Example 1, only change the theoretical number of stages of the light fraction rectifying column: the number of theoretical plates in the whole column is 25, the feeding position is in the middle and upper part, and the others are the same as Example 1.

[0031] The weight fraction of the ethylene rectification tower still is 83.871 kg / h, of which ethylene is 18.594 kg / h, the overhead reflux of the ethylene rectification tower is 3438.540 kg / h, and the feed to the light end rectification tower is 1273.531 kg / h. The temperature at the top of the ethylene rectification tower is -25.0°C, the pressure is 2.15MPaG, and the temperature at the bottom of the tower is 9.3°C. The heat load of the condenser of the ethylene rectification tower is 434.504kw.

[0032] The top temperature of the stripping distillation tower is 9.6°C, the pressure is 2.16MPaG, and the temperature of the bottom of the tower is 59°C. The material mainly containing ethylene evaporated from the top ...

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Abstract

The present invention relates to a separation refinement method for ethylene preparation through biomass ethanol dehydration, wherein problems of product separation and ethylene yield increase in ethylene preparation through ethanol dehydration, especially the technical problem of recovery of ethylene from a light component stream and a heavy component material, are mainly solved with the present invention. According to the present invention, the three tower process technical scheme is adopted, wherein the tower kettle of an ethylene rectification tower separates an ethylene-containing heavy component, the ethylene-containing heavy component enters the top of a steam stripping distillation tower, light component-containing ethylene is separated from the tower top, and is conveyed to the middle portion of a light component tower, the vapor phase on the steam stripping distillation tower top returns to the middle-lower portion of the ethylene rectification tower, a heavy component is discharged from the tower bottom, a stream on the light component rectification tower top is subjected to partial condensation, the liquid phase is refluxed, the gas phase is externally discharged, and the ethylene product is obtained from the tower kettle. With the technical scheme, the problems in the prior art are well solved, and the separation refinement 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 biomass 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 gu...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C11/04C07C7/04
Inventor 邵百祥沈伟
Owner CHINA PETROLEUM & CHEM CORP
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