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Catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons

A catalytic conversion method and low-carbon olefin technology, which is applied in the direction of hydrocarbon cracking, production of bulk chemicals, and treatment of hydrocarbon oil, etc., can solve the problems of low straight-run naphtha production, economical impact, and insufficient coke production. Achieve the effects of improving operational stability, overcoming high dry gas yield, and reducing the possibility

Active Publication Date: 2015-03-18
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0012] From the perspective of existing technologies, the development of catalytic conversion of hydrocarbons to produce low-carbon olefins and aromatics mainly focuses on the catalytic cracking technology of heavy oil. Due to the wide distillation range of heavy oil and the large hydrocarbon molecules, the product structure is complicated. , the yield of non-target products is high. In order to increase the yield of low-carbon olefins, a higher reaction temperature is usually used, resulting in a significant increase in dry gas yield, especially methane yield, under the condition of increasing olefin yield.
[0013] The catalytic cracking technology using light feedstock oil such as naphtha as raw material is in the research and development stage. Worldwide, light hydrocarbons and naphtha are the main cracking raw materials for ethylene production, and straight-run diesel oil is the main raw material for cracking. The proportion is very small, but my country's light hydrocarbon raw material oil resources are limited, and most of the crude oil is heavy oil, and the output of straight-run naphtha is very small, forcing the proportion of diesel raw material in ethylene production to be relatively high
[0014] At present, the catalytic cracking technology of straight-run diesel oil has been developing slowly. The reasons are that, firstly, the yield ratio of propylene and ethylene is relatively low, while the yield of by-products is too high, which affects its economic efficiency; Insufficient coke, the heat generated during the regeneration process of the standby catalyst is difficult to meet the demand for reaction heat
[0015] Aiming at the heat balance problem of the straight-run diesel catalytic cracking unit, the existing technology mainly adopts the technology of injecting or mixing fuel oil or coal powder in the stripping section, the spent agent delivery pipeline and the regenerator. These methods generally cause local If the temperature is too high, the device will be damaged, and it will also lead to catalyst deactivation, catalyst skeleton structure collapse and other adverse results

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  • Catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons
  • Catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons
  • Catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons

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Embodiment approach

[0089] According to one embodiment of the present invention, when the method of the present invention is carried out in riser reactor, generally carry out as follows:

[0090] The regenerated catalyst rich in mesoporous zeolite enters the pre-lift section of the riser reactor and flows upward under the action of the pre-lift medium. After the preheated hydrocarbon oil feedstock is mixed with part of methane, it is injected into the riser together with atomized steam The lower part of the reactor is in contact with the regenerated catalyst for catalytic cracking reaction and flows upwards at the same time; the post-reaction stream enters the cyclone separator through the outlet of the riser reactor, and the separated reaction oil and gas extraction device is further separated to obtain methane, C2-C3 olefins, C2 -C4 alkanes, C4 olefins, pyrolysis gasoline and pyrolysis diesel oil and other fractions; part of the methane and / or C4 olefins return to the riser reactor, the separate...

Embodiment 1

[0108] This example follows figure 2 The process of Yanshan straight-run diesel oil is used as the raw material of catalytic cracking, and the test is carried out on the medium-sized device of the riser reactor. After the preheated feed oil is mixed with part of methane (the mass ratio of methane to feed oil is 5:100) Entering the bottom of the riser, the cracking reaction is carried out at the reaction temperature of 620°C, the reaction time of 2.5 seconds, the weight ratio of catalytic cracking catalyst to raw oil is 25, and the weight ratio of water vapor to raw oil is 0.30. The reaction product is oil gas It is separated from the raw catalyst in the settler, and the raw catalyst enters the stripping section under the action of gravity, and the hydrocarbon products adsorbed on the raw catalyst are stripped by water vapor. After stripping, the raw catalyst and the high temperature from the regenerator After the flue gas is heat exchanged (the temperature of the catalyst to ...

Embodiment 2

[0110] This example follows figure 2 The flow process of Yanshan straight-run diesel oil is directly used as the feed oil of catalytic cracking, and the test is carried out on a medium-sized device with a riser reactor. The preheated feed oil is mixed with part of methane (the mass ratio of methane to feed oil is 7.5: 100) into the bottom of the riser, the cracking reaction is carried out under the conditions of a reaction temperature of 640°C, a reaction time of 2 seconds, a weight ratio of catalytic cracking catalyst to raw oil of 20, and a weight ratio of water vapor to raw oil of 0.30. The reaction product oil gas and the unused catalyst are separated in the settler, and the unused catalyst enters the stripping section under the action of gravity, and the hydrocarbon products adsorbed on the unused catalyst are stripped by the water vapor, and the unused catalyst after stripping is separated from the regenerated catalyst. The high-temperature flue gas from the regenerator...

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Abstract

The invention provides a catalytic conversion method for production of low-carbon olefins and light aromatic hydrocarbons. The catalytic conversion method comprises the following steps: enabling methane and raw oil containing 30-90% by mass of alkanes to be in contact with a catalytic pyrolysis catalyst under a catalytic pyrolysis condition, separating pyrolysis gasoline from a mixture after contact, hydrotreating the pyrolysis gasoline, and separating a product obtained by hydrotreating to obtain the hydrotreated pyrolysis gasoline. The catalytic conversion method provided by the invention can be used for high-selectively producing low-carbon olefins, particularly propylene and light aromatic hydrocarbons by taking the raw oil such as straight-run diesel with relatively high content of alkanes as a raw material. By adopting the catalytic conversion method, the problem of shortage of petrochemical raw materials can be solved, and the economic benefit of a refinery can be improved.

Description

technical field [0001] The invention relates to a catalytic conversion method for producing light olefins and light aromatics. Background technique [0002] Ethylene and propylene are important organic chemical raw materials. According to analysis, the global ethylene demand in 2012 increased by 3.9%, about 132Mt; the propylene demand increased by 4.0%, about 83Mt, and the demand ratio of propylene and ethylene was about 1.0. In the past 10 years, the growth rate of world propylene demand has been higher than that of ethylene. It is estimated that in the next 20 years, the growth rate of world propylene demand will still exceed the growth rate of ethylene demand. [0003] Using the traditional steam cracking route to produce ethylene and propylene, there is a large demand for chemical light hydrocarbons such as light hydrocarbons and naphtha. It is estimated that 700,000 tons / year of chemical light oil will be needed in 2020. However, domestic crude oil is generally heavy, a...

Claims

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Application Information

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IPC IPC(8): C07C4/06C07C11/02C07C11/06C07C15/02C10G69/04
CPCY02P20/52Y02P20/584
Inventor 毛安国魏晓丽张久顺
Owner CHINA PETROLEUM & CHEM CORP