Modifying method for naphtha and light hydrocarbon aromatization
A naphtha and aromatization technology, applied in the direction of naphtha catalytic reforming, etc., can solve the problem of no catalyst regeneration method, and achieve the effects of reducing energy consumption, increasing the flexibility of regeneration operation, and being easy to control.
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example 1
[0061] (1) Preparation of composite carrier
[0062] 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. The prepared slurry was dropped into an oily ammonia column containing 8% by mass of ammonia water, and the wet ball formed in the oily ammonia column was taken out, dried at 60°C for 10 hours, and roasted 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.
[0063] (2) Preparation of catalyst
[0064] Get 50 kilograms of composite carriers, use 50 kilograms containing 4.7 mass % of zinc nitrate, 3.0 mass % of mixed rare earth chl...
example 2
[0067] according to figure 1The technological process shown, uses catalyst A, carries out the 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 the cycle of hydrogen-containing gas Under conditions, the content of hydrogen in the hydrogen-containing gas is 21.4% by volume, and the volume ratio of hydrogen to naphtha is 150. 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 . The light hydrocarbons are equally divided into two streams, one stream is mixed with straight-run naphtha and enters the first reactor 108 through the heating furnace 106, 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 th...
example 3
[0069] according to figure 2 The technological process shown, uses catalyst A, carries out the 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 the cycle of hydrogen-containing gas Under conditions, the content of hydrogen in the hydrogen-containing gas is 22.0% by volume, and the volume ratio of hydrogen to naphtha is 150. 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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