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Methanol-to-gasoline combined technology

A methanol-to-gasoline and combined process technology is applied in the petroleum industry, the preparation of liquid hydrocarbon mixtures, and biological raw materials. rate, the effect of increasing the octane number

Active Publication Date: 2016-09-14
WUHAN KELIN FINE CHEM
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

This process also does not deal with the by-product gas and heavy oil, which cannot be effectively utilized, and the utilization rate of carbon is low

Method used

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  • Methanol-to-gasoline combined technology
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Examples

Experimental program
Comparison scheme
Effect test

Embodiment example

[0023] The embodiment of the scheme is described in combination with the process flow chart to further illustrate the present invention.

[0024]The methanol raw material 1 is pumped into the heating furnace 2, and part of the methanol vapor from the heating furnace 2 enters the dimethyl ether reactor 3. The dimethyl ether, water and unreacted methanol from the dimethyl ether reactor 3 enter the gasoline conversion reactors 4, 5 and 6, and the gasoline conversion reactors 4, 5 and 6 are produced by Wuhan Kelin Fine Chemical Co., Ltd. W221A type catalyst. After the product passes through the heat exchanger 7, it enters the oil-water separator 8 for oil-water separation, and the generated water 12 is separated.

[0025] The product after separating the generated water 12 from the oil-water separator 8 enters the deethanizer 9 . The separated dry gas 13 is divided into three parts: one part passes through the compressor 14 and then enters the heat exchanger 7 for preheating, an...

Embodiment example 1

[0029] In the dimethyl ether reactor 3, WD-1 catalyst produced by Wuhan Kelin Fine Chemical Co., Ltd. is used. The hot spot temperature is 260°C and the space velocity is 0.5h. -1 ， The operating pressure is 3.0MPa.

[0030] Gasoline conversion reactors 4, 5 and 6 use W221A catalyst produced by Wuhan Kelin Fine Chemical Co., Ltd., the hot spot temperature is 420°C, and the operating pressure is 3.0MPa.

[0031] Part of the separated dry gas 13 passes through the compressor 14 and then enters the heat exchanger 7 for preheating, and then enters the gasoline conversion reactors 4, 5 and 6 with the dimethyl ether, water and unreacted methanol from the dimethyl ether reactor 3 , The dry gas circulation ratio entering the compressor 14 is 1:10.

[0032] The pressure at the top of the deethanizer 9 is 400kPa, and the temperature is 40°C. The pressure at the top of the debutanizer 10 is 1200 kPa, and the temperature is 60°C.

[0033] The liquefied gas 16 exiting the debutanizer 1...

Embodiment example 2

[0039] The WD-1 catalyst produced by Wuhan Kelin Fine Chemical Co., Ltd. is used in the dimethyl ether reactor 3, the hot spot temperature is 280°C, and the space velocity is 1.2h -1 ， The operating pressure is 1.8MPa.

[0040] Gasoline conversion reactors 4, 5 and 6 use W221A catalyst produced by Wuhan Kelin Fine Chemical Co., Ltd., with a hot spot temperature of 330°C and an operating pressure of 1.8MPa.

[0041] Part of the separated dry gas 13 passes through the compressor 14 and then enters the heat exchanger 7 for preheating, and then enters the gasoline conversion reactors 4, 5 and 6 with the dimethyl ether, water and unreacted methanol from the dimethyl ether reactor 3 , The dry gas circulation ratio entering the compressor 14 is 15:1.

[0042] The pressure at the top of the deethanizer 9 is 800kPa, and the temperature is 55°C. The pressure at the top of the debutanizer 10 is 400 kPa, and the temperature is 40°C.

[0043] The liquefied gas 16 exiting the debutanize...

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Abstract

The invention relates to a methanol-to-gasoline combined production technology, and belongs to an important link of a coal-preparing high-clean energy technology. The technology includes the steps: methanol is heated, then a great part of the methanol enters a dimethyl ether reactor, is subjected to crude dehydration, then enters a gasoline transformation reactor and is further dehydrated, and the product passes through a heat exchanger and then is subjected to oil-water separation; crude gasoline is separated to obtain dry gas through a deethanizer; a part of the dry gas is subjected to heat exchange through the heat exchanger, then enters a circulation compressor and together with a dimethyl ether reactor outlet product enters a conversion reactor, so as to achieve the temperature dropping and control purposes; the gasoline having the dry gas removed enters a debutanizer, and removed liquefied gas and the other part of methanol steam undergo a superimposed etherification reaction; crude gasoline coming out of the debutanizer is separated to obtain the product gasoline and heavy oil by a gasoline separation tower; the heavy oil and the other part of the dry gas coming out of the deethanizer are together modified by a transalkylation catalyst to obtain a gasoline component, dry gas and liquefied gas.

Description

technical field [0001] The invention relates to a combination process of methanol-to-gasoline, which belongs to the coal-to-oil industry sector and belongs to the technical field of pollution-free and high-quality energy production processes. technical background [0002] At present, the rapid development of the world economy has led to an increasing consumption of refined oil, and the society's unrestricted demands have led to the depletion of oil resources. According to statistics, China consumed 439 million tons of oil in 2010, 470 million tons in 2011, and 493 million tons in 2012. China's self-produced oil is about 200 million tons per year, and its dependence on foreign crude oil in 2012 was 56.42%, the highest in history. Experts predict that based on the current global consumption rate, the existing oil resources can only last for a few decades, and finding suitable alternative oil resources has become an urgent and important mission for the whole society. In view ...

Claims

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Application Information

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IPC IPC(8): C10G3/00
CPCY02P30/20C10G3/49
Inventor 王国兴张先茂陈凯王泽瞿玖郑敏王天元赵志杰
Owner WUHAN KELIN FINE CHEM
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