Separating and refining method for preparing ethylene by dehydrating biomass ethanol

A technology of biomass ethanol and refining method, which is applied in the field of separation and refining of biomass ethanol dehydration to ethylene, can solve problems such as low recovery efficiency and ethylene loss, and achieve easy operation, reduced energy consumption for separation, purity and yield of ethylene products rate-enhancing effect

Active Publication Date: 2014-03-26
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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  • Separating and refining method for preparing ethylene by dehydrating biomass ethanol

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0015] 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.

[0016] 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

[0022] Same as [Example 1], only the theoretical number of stages of the ethylene rectification tower is changed: 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].

[0023] 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.

[0024] 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 ...

Embodiment 3

[0029] Same as [Example 1], only change the theoretical number of stages of the light fraction rectifying tower: the number of theoretical plates in the whole column is 25, the feeding position is in the middle and upper part, and others are the same as [Example 1].

[0030] 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.

[0031] 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 o...

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Abstract

The invention relates to a separating and refining method for preparing ethylene by dehydrating biomass ethanol, which is mainly used for solving the problems that a process for separating a product in preparation of ethylene from dehydrating ethanol and a way for increasing the yield of the ethylene are not related in the previous literatures, particularly the technical problem of the recovery of the ethylene from light-component material flow and heavy-component materials. According to the separating and refining method disclosed by the invention, the technical scheme of a three-tower flow is adopted to well solve the problems. According to the technical scheme, the method comprises the following steps: separating ethylene-containing heavy components out of the tower kettle of an ethylene refining tower, feeding the ethylene-containing heavy components into the top of a stripping tower, separating ethylene containing light components out of the tower top, and feeding to the middle part of a light-component tower; returning a vapor phase on the top of the stripping tower to the middle lower part of the ethylene refining tower, and discharging heavy components from the tower bottom; and partially condensing top material flow of a light-component refining tower, refluxing a liquid phase, and discharging a gas phase to obtain an ethylene product from the tower kettle. The method can be applied to industrial production of ethylene prepared by dehydrating ethanol.

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 邵百祥周斌
Owner CHINA PETROLEUM & CHEM CORP
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