Combined catforming of high-production low carbon alkene

A catalytic conversion method and technology of low-carbon olefins, applied in the direction of hydrocarbon cracking, chemical recovery, organic chemistry, etc., can solve the problems of longer residence time, intensified thermal cracking, and increased dry gas yield, so as to achieve easy desorption, The effect of increasing the ratio of agent to oil and increasing the yield

Active Publication Date: 2010-05-12
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Although the process and device provided by this patent can greatly improve the operational flexibility of the ultra-short contact time catalytic cracking unit, the product and catalyst after the cracking of the first hydrocarbon oil raw material in this patent need to be separated by sedimentation in the settler. Therefore, the settler must have a larger volume so that the oil and gas can reach the superficial gas velocity that causes the catalyst to settle down when the oil and gas rise in the settler. As a result, the oil and gas must stay in the high temperature environment in the settler for a long time, thereby Lead to intensified thermal cracking and increased yield of dry gas

Method used

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  • Combined catforming of high-production low carbon alkene
  • Combined catforming of high-production low carbon alkene
  • Combined catforming of high-production low carbon alkene

Examples

Experimental program
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Effect test

Embodiment approach 1

[0032] Such as figure 1 As shown, the first regenerated catalyst at about 720°C enters the pre-elevating section 4 of the down tube reactor through the transfer line 6 and the flow control valve 7, and the pre-elevating medium from the pipeline 8 enters the pre-elevating section 4 through the distributor 5. The catalyst in the pre-lift section 4 is lifted to the inlet of the down tube reactor 3. The pre-lifting medium can be water vapor, dry gas from or outside the device, C4 component in cracked gas, or a mixture of these gases. The preheated heavy oil feedstock is atomized by atomizing water vapor through the pipeline 1 and nozzle 2 and then injected into the down tube reactor 3 to contact and react with the hot catalyst from the catalyst pre-lifting section 4. The reaction temperature is 500-650°C, preferably 520-620°C; the reaction pressure is 1.5-5×10 5 Pa, preferably 1.8-4×10 5 Pa; reaction time is 0.1-1.5 seconds, preferably 0.15-1 second; the weight flow ratio of catal...

Embodiment approach 2

[0035] figure 2 Shown is the second embodiment of the present invention. The difference between this embodiment and the first embodiment is that the catalyst separated by the gas-solid separation device 20 at the outlet of the riser does not enter the catalyst regeneration system directly after being pre-stripped with steam injected through the distribution pipe 27 at the lower part of the settler 25 , It enters the stripper 11 below the gas-solid separation system of the down tube reactor through the transfer line 28 and the catalyst flow control valve 29, and mixes with the catalyst collected by the gas-solid separation system of the down tube reactor, and then enters the stripper together. 11 receives steam stripping, and then enters the regenerator through the transfer line 12 and the catalyst flow control valve 13 to be burnt and regenerated, and then returns to the reaction system for recycling. Because the reaction temperature of the riser is higher than that of the dow...

Embodiment approach

[0037] image 3 Shown is the third embodiment of the present invention. The difference between this embodiment and the first embodiment is that the catalyst separated by the gas-solid separation device 20 at the outlet of the riser is injected into the lower part of the settler 25 through the distribution pipe 27 After the steam is pre-stripped, it does not directly enter the catalyst regeneration system, but enters the catalyst pre-lift section 4 of the down tube reactor through the pipeline 30 and the catalyst flow control valve 31. In the pre-lift section 4, the first regenerated catalyst passes through the reactor. After mixing for less than two seconds, it comes into contact with the feed oil injected into the down tube reactor. Because the raw material for the riser reaction is lighter and the reaction temperature is relatively high, the catalyst after the reaction has less carbon deposits and still has a relatively high Activity and temperature. The introduction of this ...

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Abstract

A combined catalytic converting process for preparing low-carbon olefin with high output includes such steps as contacting between heavy oil as raw material, regenerated catalyst and carbon depositedcatalyst in flow-down tube reactor, cracking reaction, separating the cracked product from the catalyst to be regenerated, separating low-carbon olefin from cracked product, contacting between rest ofsaid product and regenerated catalyst in flow-up tube reactor, reaction, separating oil gas from catalyst, separating low-carbon olefin from oil gas, and regenerating the catalyst.

Description

Technical field [0001] The present invention belongs to a method for the catalytic conversion of hydrocarbon oil in the absence of hydrogen. More specifically, the present invention is a combined catalytic conversion method for producing low-carbon olefins. Background technique [0002] The development of the world economy has driven the continuous growth of global demand for low-carbon olefins. It is estimated that by 2010, the total global demand for ethylene and propylene will reach 140Mt / a and 86Mt / a. In my country, due to the rapid growth of the national economy, the annual growth rate of low-carbon olefin demand will exceed the world average, and the demand for propylene will increase The growth rate has exceeded the growth rate of ethylene demand. There are many preparation methods for low-carbon olefins, and steam cracking technology using light raw materials such as naphtha is widely used in the world. More than 90% of the world's total production of ethylene and about ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C4/06C07C11/00C07C11/06
CPCY02P20/52Y02P20/584
Inventor 许克家侯栓弟龙军达志坚张久顺谢朝钢张占柱武雪峰何峻
Owner CHINA PETROLEUM & CHEM CORP
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