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Combined catforming of high-production low carbon alkene

A catalytic conversion method and technology of low-carbon olefins, which are applied in the fields of hydrocarbon cracking to produce hydrocarbons, chemical recovery, organic chemistry, etc. , easy desorption, the effect of improving yield

Active Publication Date: 2007-10-03
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
Comparison scheme
Effect test

Embodiment approach 1

[0032] As shown in Figure 1, the first stream of regenerated catalyst at about 720 °C enters the pre-lift section 4 of the downcomer reactor through the delivery pipeline 6 and the flow control valve 7, and the pre-lift medium from the pipeline 8 enters the pre-lift section through the distributor 5 4. Lift the catalyst in the pre-lift section 4 to the inlet of the downcomer reactor 3 . The pre-lifting medium can be water vapor, dry gas from or outside the device, C4 components in cracked gas or a mixture of these gases. The preheated heavy oil raw material is injected into the downcomer reactor 3 through the pipeline 1 and the nozzle 2 after being atomized by atomized water vapor, and then contacts and reacts 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; the reaction time is 0.1-1.5 seconds, preferably 0.15-1 seconds; the weight fl...

Embodiment approach 2

[0035] Figure 2 shows a 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 directly enter the catalyst regeneration system after being pre-stripped by the water vapor injected by the distribution pipe 27 at the lower part of the settler 25 , but enter the stripper 11 below the gas-solid separation system of the downcomer reactor through the delivery pipeline 28 and the catalyst flow control valve 29, and after mixing with the catalyst collected by the gas-solid separation system of the downcomer reactor, they are together in the stripper 11 accepts water vapor stripping, and then enters the regenerator through the delivery pipeline 12 and the catalyst flow control valve 13 and returns to the reaction system for recycling. Because the reaction temperature of the riser is higher than the reaction temperature of the down...

Embodiment approach 3

[0037] Fig. 3 shows a 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 does not directly enter the catalyst regeneration system after being pre-stripped by the water vapor injected by the distribution pipe 27 at the lower part of the settler 25 , but enters the catalyst pre-lift section 4 of the downcomer reactor through the pipeline 30 and the catalyst flow control valve 31. Reactor feed oil contact. Because the raw material for the riser reaction is relatively light 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. Introducing this catalyst into the downcomer not only helps to increase the catalyst-oil ratio of the downcomer reaction, but also increases the contact opportunity between the heavy oil feedstock an...

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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 deposited catalyst 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 of said 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 invention belongs to a method for catalytic conversion of hydrocarbon oil in the absence of hydrogen, more specifically, the invention is a combined catalytic conversion method for producing more 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; while in my country, due to the rapid growth of the national economy, the annual growth rate of demand for low-carbon olefins will exceed the world average level, and the demand for propylene will increase. The growth rate exceeded the growth rate of ethylene demand. There are many methods for preparing 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 produc...

Claims

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Application Information

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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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