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Continuous aromatization modification method for hydrocarbons

An aromatization and hydrocarbon technology, which is used in the production of aromatic hydrocarbons or high-octane gasoline components and liquefied gas with low olefin content, can solve the problem of no catalyst regeneration method, and achieve reasonable optimization of product distribution and use. The effect of long life and reduced energy consumption for regeneration

Active Publication Date: 2008-12-03
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The aromatization reaction can be carried out in moving bed, fluidized bed or fixed bed, but no specific catalyst regeneration method is given

Method used

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  • Continuous aromatization modification method for hydrocarbons
  • Continuous aromatization modification method for hydrocarbons
  • Continuous aromatization modification method for hydrocarbons

Examples

Experimental program
Comparison scheme
Effect test

example 1

[0050] Catalysts used in the present invention are prepared.

[0051] (1) Preparation of composite carrier

[0052] Get 67.6 kilograms of pseudo-boehmite powder (production of Sasol company, PURAL SB, alumina content 74% by mass), under stirring, add 300 kg of nitric acid aqueous solution with a concentration of 1.1% by mass, stir for 2 hours to peptize, add 55.0 kg of HZSM-5 zeolite with a silica / alumina molar ratio of 60 powder (91% zeolite content), stirred at high speed for 3 hours. Drop the prepared slurry into an oily ammonia column containing 8% by mass of ammonia water, take out the wet bulb formed in the oily ammonia column, dry at 60°C for 10 hours, and roast at 550°C for 3 hours to obtain a composite carrier, which is a composite carrier containing HZSM- 5 zeolite 50% by mass alumina pellets.

[0053] (2) Preparation of catalyst

[0054] Get 50 kilograms of composite carriers, use 50 kilograms containing 4.7 mass % of zinc nitrate, 3.0 mass % of mixed rare eart...

example 2

[0057] according to figure 1 In the process flow shown, catalyst A is used, and the straight-run naphtha shown in Table 1 is used as the raw material, and the aromatization reaction test is carried out under non-hydrogenation conditions, and the inlet temperature of each reactor is controlled at 400 °C and the reaction pressure 0.5MPa, feed mass space velocity is 0.5h -1 , The straight-run naphtha enters the reaction zone in the order of the heating furnace, the first reactor, the heating furnace and the second reactor for aromatization. The main operating conditions of the catalyst regenerator are as follows: the pressure of the regenerator is 0.7MPa, the inlet temperature of the regeneration gas in the first-stage coking zone is 470°C, and the oxygen content in the regeneration gas is 0.5% by volume; the inlet temperature of the regeneration gas in the second-stage burnt zone is 480°C, The oxygen content in the regenerated gas is 0.6% by volume, the volume ratio of the rege...

example 3

[0059] according to figure 2 In the process flow shown, catalyst A is used to carry out aromatization reaction with the straight-run naphtha shown in Table 1 as raw material, and the reaction is carried out under non-hydrogen-facing conditions. The operating conditions of the reaction part and the regenerator, the residence time of the ungenerated catalyst in the coking zone, the gas inlet temperature in the drying zone and the gas outlet temperature in the cooling zone are all the same as in Example 2, except that the regeneration gas enters the two-stage coking zone from the middle. , the test results are shown in Table 2.

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Abstract

A continuous hydrocarbon aromatization and modification method comprises the following steps: (1) heating hydrocarbon materials, and feeding into a moving bed reactor from the top to contact and react with an aromatization catalyst, (2) lifting the spent catalyst from the bottom of the moving bed reactor by a spent catalyst elevator through a riser line to a spent catalyst separation hopper, separating with the lifting gas, feeding into a catalyst regenerator from the top through a pressure transformation and flow control region, passing through the buffer zone, the burning region, the drying zone and the cooling zone in the catalyst regenerator sequentially from top to bottom, and introducing oxygen-containing regeneration gas into the burning zone to burn and regenerate the spent catalyst, and (3) lifting the regenerated catalyst flowing from the bottom of the catalyst regenerator and adding into the moving bed reactor from the top. The method is suitable for aromatization reaction of naphtha with low octane number, and has the advantages of sufficient regeneration and burning of catalyst, less specific area loss of catalyst, long service life of the regenerated catalyst and low energy consumption of the regeneration operation.

Description

technical field [0001] The present invention is a continuous aromatization upgrading method for hydrocarbons, specifically, it uses low-octane naphtha as a raw material to produce high aromatics or low olefin content in a moving bed reactor-continuous regeneration device. Octane gasoline components and liquefied gas methods. Background technique [0002] With the introduction of unleaded gasoline and new gasoline standards, some low-octane gasoline, such as reformed top oil, condensate, partially hydrocoked gasoline and straight-run gasoline, need to find suitable processing technology. Although this part of naphtha is suitable as ethylene raw material, it is difficult to transport because of its high vapor pressure. If there is no ethylene plant near the enterprise, it is difficult to be used as ethylene raw material. At present, catalytic reforming is the main device used by refineries to produce aromatics and high-octane clean gasoline blending components. However, cata...

Claims

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Application Information

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IPC IPC(8): C10G35/12C10G35/095
Inventor 王杰广马爱增于中伟任坚强
Owner CHINA PETROLEUM & CHEM CORP
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