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A catalytic cracking method for producing light olefins and light aromatics

A technology for catalytic cracking and low-carbon olefins, applied in chemical instruments and methods, multi-stage series-connected refining and cracking process treatment, hydrocarbon cracking to produce hydrocarbons, etc. The effect of high yield, rich mesoporous structure and high yield

Active Publication Date: 2021-08-06
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] In summary, the existing technologies all take low-carbon olefins as the main target yield and co-produce light aromatics, so the increase in the yield of light aromatics is limited. It is necessary to develop a catalytic cracking method with higher yields of low-carbon olefins and light aromatics on the basis of current technology and catalytic materials

Method used

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  • A catalytic cracking method for producing light olefins and light aromatics

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preparation example Construction

[0069] The preparation method of catalytic cracking catalyst of the present invention comprises preparation and comprises Y-type molecular sieve, aperture is less than The microspherical composition of molecular sieves, natural minerals, and oxide binders, the present invention is called the first composition microspheres, and the first composition microspheres are modified; the first composition microspheres are modified; The ball modification process includes the following steps:

[0070] a. Put the microspheres of the first composition into an alkaline solution for treatment, filter and wash to obtain the microspheres of the first composition of alkali treatment;

[0071] b. Treat the alkali-treated first composition microspheres obtained in step a in a compound acid solution composed of fluosilicic acid, organic acid and inorganic acid, filter and wash, optionally exchange ammonium for sodium treatment, and optionally filter and optionally washed, optionally dried, to ob...

Embodiment approach

[0091] 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:

[0092] The regenerated catalyst (catalyst for catalytic cracking) enters the pre-lift section of the riser reactor and flows upward under the action of the pre-lift medium. The preheated raw oil and atomized steam are injected into the lower part of the riser reactor to contact the regenerated catalyst. The catalytic cracking reaction flows upward at the same time; the reacted oil and gas and the catalyst to be produced enter the fluidized bed reactor through the outlet of the riser reactor, and the reacted oil and gas react again, and the reacted stream enters the cyclone separator through the outlet of the riser reactor, and the separated reaction The oil and gas extraction device is further separated to obtain fractions such as methane, ethylene, propylene, C4 hydrocarbons, and pyrolysis gasoline rich in ligh...

Embodiment

[0113] according to figure 1 The process is tested, the feed oil is vacuum distillate oil, MMC-2 catalyst is used, and the test is carried out on a medium-sized device. The three reactors are all operated under normal pressure. The hydrocracking tail oil enters the riser 1, and the reaction temperature is 580 ℃, reaction time 2.0 seconds, the weight ratio of regenerated catalyst and raw catalyst mixture (wherein the raw catalyst accounts for 20% by weight of the catalyst mixture) to raw oil is 10, and the weight ratio of water vapor to raw oil is 0.25 to carry out the cracking reaction , the reaction oil gas and water vapor and the spent catalyst enter the cyclone separator from the reactor outlet.

[0114] Aromatic raffinate oil (saturated hydrocarbon content is 87% by weight) enters the bottom of the riser 2, and at a reaction temperature of 625°C and a reaction time of 1.8 seconds, the weight ratio of the regenerated catalyst to the feedstock oil is 15, and the weight ratio...

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Abstract

A catalytic cracking method for producing low-carbon olefins and light aromatics. The heavy raw materials are reacted in the first reactor in contact with the first part of the catalytic cracking catalyst. The light raw materials rich in saturated hydrocarbons and the light raw materials rich in olefins are The second reactor and the third reactor are contacted with the second part of the catalytic cracking catalyst to react, and all the reacted oil gas and the unborn catalyst are subjected to gas-solid separation, wherein the reacted oil gas is further separated to obtain products containing light olefins and light aromatics; After being stripped, the raw catalyst enters the catalyst regenerator for coke regeneration, and the regenerated catalyst is returned to the reactor for recycling; the catalytic cracking catalyst contains 5% to 65% of natural minerals in terms of weight percentage, and 10% to 60% of Oxides and 24% to 74% of Y-type molecular sieves and at least one molecular sieve with a pore size smaller than 0.1% to 15% of phosphorus additives. The method of the invention has higher yields of light olefins and light aromatics.

Description

technical field [0001] The present invention relates to a method for catalytic conversion of hydrocarbon oil in the absence of hydrogen, and more particularly to a catalytic cracking method for producing light olefins and light aromatics. Background technique [0002] Low-carbon olefins represented by ethylene and propylene are the most basic raw materials in the chemical industry. Natural gas or light petroleum fractions are mostly used as raw materials at home and abroad, and low-carbon olefins are produced by steam cracking technology in ethylene complexes. In addition to the production of ethylene, about 70% of propylene, 90% of butadiene, and 30% of aromatics come from steam cracking by-products. Although the steam cracking technology has been developed for decades and the technology has been continuously improved, it still has high energy consumption, high production cost, and CO 2 Due to technical limitations such as large emissions and difficult adjustment of produc...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G55/06C10G3/00C07C4/06C07C4/18C07C11/04C07C11/06C07C15/02B01J29/80
CPCB01J29/084B01J29/405B01J29/7007B01J29/80C07C4/06C07C4/18C10G3/49C10G55/06C10G2300/70C10G2400/02C10G2400/04C10G2400/30C07C11/04C07C11/06C07C15/02Y02P20/52Y02P20/584
Inventor 谢朝钢魏晓丽陈学峰张久顺罗一斌田辉平张执刚刘银亮李福超
Owner CHINA PETROLEUM & CHEM CORP
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