Catalytic conversion method for preparing propylene and high-octane gasoline with crude oil

A technology of high-octane gasoline and catalytic conversion method, applied in catalytic cracking, cracking, petroleum industry and other directions, can solve the problems of underutilization of gasoline potential content, low propylene yield, increased dry gas yield and the like

Active Publication Date: 2011-07-27
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] The above-mentioned prior art still has deficiencies in the design of the alkane molecular cracking reaction, resulting in a substantial increase in the dry gas yie

Method used

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  • Catalytic conversion method for preparing propylene and high-octane gasoline with crude oil
  • Catalytic conversion method for preparing propylene and high-octane gasoline with crude oil
  • Catalytic conversion method for preparing propylene and high-octane gasoline with crude oil

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0081] This example follows figure 1 The process of the test is carried out, and the raw material oil A is directly used as the raw material oil of catalytic cracking, and the test is carried out on the medium-sized device of the riser reactor, and the raw material oil A enters the reaction zone I. Reaction temperature 530°C, weight hourly space velocity 30h-1 , the weight ratio of catalyst to raw oil is 10, and the weight ratio of water vapor to raw oil is 0.15. The cracking reaction is carried out. The reaction product oil gas and the catalyst with charcoal to be born are separated in the settler, and the products are separated in the separation system according to the distillation range. cutting to obtain products such as propylene, gasoline and catalytic wax oil. The operating conditions and product distribution are listed in Table 2.

[0082] As can be seen from Table 2, the propylene yield is as high as 21.38% by weight; the gasoline yield is 23.23% by weight, its resea...

Embodiment 2

[0084] This example follows the attached image 3 The test is carried out according to the process, the raw material oil A is directly used as the refractory raw material oil of catalytic cracking, and the test is carried out on a medium-sized device with a riser reactor. The easy-to-crackable raw material oil enters the middle and upper part of the reaction zone I, and the difficult-to-crackable raw material oil enters the reaction zone I. Bottom, at the bottom of reaction zone I, the difficult-to-crack raw oil is -1 , the weight ratio of catalytic cracking catalyst to difficult-to-crack raw oil is 30, and the weight ratio of water vapor to difficult-to-crack raw oil is 0.20 to carry out the cracking reaction; Hourly space velocity 90h -1 , the weight ratio of the catalytic cracking catalyst to the easy-to-crack raw oil is 10, and the weight ratio of water vapor to the easy-to-crack raw oil is 0.15 to carry out the cracking reaction. In the reaction zone II, the reactant str...

Embodiment 3

[0087] This embodiment is identical with the test apparatus of embodiment 2, and stock oil B is directly used as the difficult-to-crack stock oil of catalytic cracking, and is tested on the medium-sized device by riser reactor, and easy-to-crack stock oil enters the upper part of reaction zone I, and is hard to crack. The cracked raw oil enters the bottom of reaction zone I, where the difficult-to-crack raw oil is heated at a reaction temperature of 650°C and a weight hourly space velocity of 180h -1 , the weight ratio of catalytic cracking catalyst to difficult-to-crack raw oil is 90, and the weight ratio of water vapor to difficult-to-crack raw oil is 0.20 to carry out the cracking reaction; Hourly space velocity 60h -1 , the weight ratio of the catalytic cracking catalyst to the easy-to-crack raw oil is 10, and the weight ratio of water vapor to the easy-to-crack raw oil is 0.15 to carry out the cracking reaction. II bottom, to reduce the temperature and reaction space vel...

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Abstract

The invention relates to a catalytic conversion method for preparing propylene and high-octane gasolinel with crude oil. The method comprises the following steps: using pretreated crude oil as raw oil, and contacting and carrying out reaction on the pretreated crude oil and catalyst rich in mesopore zeolite in a catalytic conversion reactor; and obtaining the reaction product comprising catalytic wax oil the weight of which accounts for 12 to 60 percent of that of the raw oil after reaction due to the reaction temperature, the residence time of oil gas and the weight ratio of the catalyst to the raw oil, wherein the weight hourly space velocity ranges from 25 to 100 h-1, the reaction temperature ranges from 450 to 700 DEG C, and the weight ratio of the catalyst to the raw oil ranges from 1 to 30. The method converts inferior crude oil into the propylene and the high-octane gasoline, and greatly reduces the yield of dry gas and coke, thus realizing the efficient utilization of oil resources.

Description

technical field [0001] The invention relates to a method for catalytic conversion of crude oil, in particular to a method for converting heavy crude oil into propylene and high-octane gasoline while greatly reducing dry gas and coke yields so as to realize efficient utilization of petroleum resources. Background technique [0002] Propylene and other low-carbon olefins are important organic chemical raw materials, and propylene is a synthetic monomer for products such as polypropylene and acrylonitrile. With the rapid growth of demand for derivatives such as polypropylene, the demand for propylene is also increasing year by year. The demand in the world propylene market has increased from 15.2 million tons 20 years ago to 51.2 million tons in 2000, with an average annual growth rate of 6.3%. [0003] The methods for producing propylene are mainly steam cracking and catalytic cracking (FCC), wherein steam cracking uses naphtha and other light oils as raw materials to produce...

Claims

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Application Information

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IPC IPC(8): C10G69/04C10G55/06C10G11/05C10G11/20
Inventor 唐津莲许友好崔守业汪燮卿
Owner CHINA PETROLEUM & CHEM CORP
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