Aromatization method without hydrogen for light hydrocarbon

An aromatization and non-hydrogenation technology, which is applied in the production of aromatics or clean gasoline components, as well as in the field of high-quality liquefied gas, can solve the problems of catalyst regeneration methods not given, and achieve easy control of reaction temperature, increased flexibility, and use long life effect

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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  • Aromatization method without hydrogen for light hydrocarbon
  • Aromatization method without hydrogen for light hydrocarbon
  • Aromatization method without hydrogen for light hydrocarbon

Examples

Experimental program
Comparison scheme
Effect test

example 1

[0058] (1) Preparation of composite carrier

[0059] Get 67.6 kilograms of pseudo-boehmite powder (production of Sasol company, PURAL SB, the alumina content is 74% by mass), under stirring condition, join 300 kilograms concentration and be in the nitric acid aqueous solution of 1.1 mass %, after stirring for 2 hours peptization, add 55.0 kilograms of silica / alumina molar ratio is 60 HZSM- 5 Zeolite powder (zeolite content 91%), 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.

[0060] (2) Preparation of catalyst

[0061] Get 50 kilograms of composite carriers, use 50 kilograms containing 4.7 mass % of zinc nitrate, 3.0 mass % of mixed rare earth chloride (wherein lanth...

example 2

[0064] according to figure 1 Shown technological process, use the catalyst that example 1 makes, carry out aromatization reaction test with the straight-run naphtha shown in 60 mass % table 1 and the light hydrocarbon shown in 40 mass % table 2 as raw material, react in carried out under non-hydrogen conditions. Control the raw material inlet temperature of each reactor to be 400°C, the reaction pressure to be 0.5MPa, and the mass space velocity of raw material feed to be 0.5h -1 . Light hydrocarbons are equally divided into two streams, one stream is mixed with straight-run naphtha and enters the first reactor through a heating furnace, and the other stream of light hydrocarbons directly enters the second reactor 111 in the form of cold material. The pressure of the regenerator is 0.7MPa, the inlet temperature of regeneration gas in the first-stage coking zone is 470°C, and the oxygen content is 0.5% by volume; the inlet temperature of regeneration gas in the second-stage b...

example 3

[0066] according to figure 2The technological process shown, uses catalyst A, carries out aromatization reaction test with the straight-run naphtha shown in 60 mass % table 1 and the light hydrocarbon shown in 40 mass % table 2 as raw material, reacts in non-hydrogenation under conditions. The operating conditions of the reaction part and the regenerator, the residence time of the ungenerated catalyst in the coking zone, the temperature of the drying zone and the cooling zone are all the same as in Example 2, the difference is that the regeneration gas enters the two-stage coking zone from the middle, and the test results are shown in table 3.

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Abstract

A non-hydrogen aromatization method of light hydrocarbons comprises the following steps: (1) mixing naphtha with C3 to C5 light hydrocarbons, adding into a moving bed reaction zone, contacting with aromatization catalyst to carry out aromatization reaction, adding the spent catalyst flowing from the bottom of the moving bed reaction zone into a catalyst regenerator from the top through a spent catalyst elevator, a spent catalyst riser pipe, a spent catalyst separation hopper and a pressure transformation and flow control zone, passing through the buffer zone, a burning zone, a drying zone and a cooling zone in the catalyst regenerator sequentially from top to bottom, introducing oxygen-containing regeneration gas in the burning zone to burn and regenerate the spent catalyst, lifting the regenerated catalyst, and adding into the moving bed reactor from the top. The method can transform low-octane naphtha and low-carbon hydrocarbons into high-octane petrol and high-quality liquefied gas, and has the advantages of large generation operation flexibility, low energy consumption, good catalyst regeneration effect and long service life.

Description

technical field [0001] The invention relates to a method for non-hydrogenation aromatization of light hydrocarbons. Specifically, it is a moving bed reaction-continuous regeneration unit, with low octane naphtha and C 3 ~C 5 The mixture of light hydrocarbons is used as raw material to produce aromatic hydrocarbons or clean gasoline components, and at the same time, it is a method of producing high-quality liquefied gas. 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 b...

Claims

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Application Information

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