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Aromatization modifying catalyst for catalytic gasoline and preocess

A technology for catalytic cracking gasoline and a catalyst, which is applied in the field of high olefin content catalytic gasoline hydrogenation-upgrading combined catalyst and high sulfur content, can solve the problem of catalyst coking, weaken the catalytic activity of the catalyst, reduce the octane number and restore the stability of the catalytic performance, etc. The problem is to reduce carbon deposition, facilitate molecular diffusion, and reduce the loss of anti-knock index.

Inactive Publication Date: 2006-12-20
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

At high temperature, diolefins are easy to polymerize on the strong acid sites on the surface of the acidic molecular sieve catalyst, causing coking of the catalyst, weakening the catalytic activity of the catalyst, reducing the effect of octane recovery and the stability of catalytic performance

Method used

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Examples

Experimental program
Comparison scheme
Effect test

example 1

[0030] This example prepares 2.0m%NiO-0.50m%K 2 O-0.50m%La 2 o 3 / The grain size is 100nm~500nmHZSM-5 aromatization catalyst.

[0031] Weigh 229.6g HZSM-5 (SiO 2 / Al 2 o 3 The molar ratio is 27), 140.0g Al 2 o 3 , and grind and mix them evenly, add 150ml of dilute nitric acid solution with a concentration of 5.6g / 100ml, and grind them into a powder cake with suitable humidity. Extrude into rods with a diameter of 2.0 mm on a rod extruder. After drying at room temperature, dry at 120°C for 10 hours, and bake at 520°C for 8 hours to prepare an aromatization catalyst carrier, coded as SZ.

[0032] Weigh the catalyst carrier SZ 100g and put it into the spray tank, and start the rotary pump. 65ml containing 0.5g K in 30 minutes 2 O Potassium nitrate solution is sprayed into the catalyst support SZ. After drying at room temperature, it was dried at 120°C for 10 hours, and calcined at 500°C for 8 hours to prepare an aromatization catalyst intermediate, numbered IZ.

[003...

example 2

[0035] This example prepares 4.0m%NiO-1.0m%K 2 O-1.0m%La 2 o 3 / HBeta aromatization catalyst with a grain size of 70nm to 150nm.

[0036] Weigh 239.6g HBeta(SiO 2 / Al 2 o 3 The molar ratio is 33), 140.0g Al 2 o 3 , and grind and mix them evenly, add 180ml of dilute nitric acid solution with a concentration of 3.6g / 100ml, and grind them into a powder cake with suitable humidity. Extrude into rods with a diameter of 2.0 mm on a rod extruder. After drying at room temperature, dry at 120°C for 10 hours, and bake at 520°C for 8 hours to prepare an aromatization catalyst carrier, coded as SB.

[0037] Weigh the catalyst carrier SB 100g and put it into the spray tank, and start the rotary pump. 52ml containing 1.0g K in 30 minutes 2 The potassium nitrate solution of O is sprayed onto the catalyst support SB. After drying at room temperature, dry at 120°C for 10 hours, and bake at 500°C for 8 hours to prepare an aromatization catalyst intermediate, coded as IB.

[0038] We...

example 3

[0040] This example prepares 6.0m%NiO-1.5m%La 2 o 3 -1.5m%K 2 O / HBeta+HZSM-5 (HBeta / HZSM-5 mass percent: 50% / 50%) aromatization catalyst. Among them, the grain size of HBeta is 70nm-150nm; the grain size of HZSM-5 is 100nm-500nm.

[0041] Weigh 118.8g HBeta(SiO 2 / Al 2 o 3 The molar ratio is 33), 106.0g HZSM-5 (SiO 2 / Al 2 o 3 The molar ratio is 27), 140.0g Al 2 o 3 , and grind and mix them evenly, add 170ml of dilute nitric acid solution with a concentration of 7.6g / 100ml, and grind them into a powder cake with suitable humidity. Extrude into rods with a diameter of 2.0 mm on a rod extruder. After drying at room temperature, it was dried at 120°C for 10 hours, and then calcined at 520°C for 8 hours to prepare an aromatization catalyst carrier, coded as SZB.

[0042] Weigh the catalyst carrier SZB 100g and put it into the spray tank, start the rotary pump. 57ml containing 1.5g K in 30 minutes 2 The potassium nitrate solution of O was sprayed onto the catalyst sup...

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Abstract

The present invention relates to a technological process for producing low-sulfur low-olefin clean gasoline by using catalytic cracked gasoline and catalyst used by said process. Said invention adopts hydrofinishing and aromatization combined process, in which the aromatization adopts small-grain hydrogen type molecular sieve catalyst including IA group metal, transition metal and lanthanide series rare-earth metal oxide, and the crystal grain size of the molecular sieve is in the range of 20nm-800 nm. Said invented catalyst can reduce cracking reaction and can raise the yield of the gasoline.

Description

1. Technical field [0001] The invention relates to a high-flexibility high-sulfur-content, high-olefin-content catalytic gasoline hydrogenation-upgrading combined catalyst and process. 2. Background technology [0002] With the rapid improvement of people's awareness of environmental protection, the air pollution caused by automobile exhaust has attracted more and more attention. Since the reduction of sulfur and olefin content in gasoline can reduce the restorative organic compounds (VOCs), nitrogen oxides (NO X ) and emissions of harmful substances such as sulfur dioxide. At present, major developed countries in the world limit the sulfur content of motor gasoline to less than 200 μg / g, and the olefin content to less than 30.0 (v)%. Catalytic gasoline usually accounts for a large proportion of gasoline blending, and the blending ratio of gasoline in diesel oil refineries reaches 80% to 90%. The sulfur content of catalytic gasoline is 500μg / g~2000μg / g, and the olefin cont...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G45/70
Inventor 赵乐平周勇段为宇庞宏房莹
Owner CHINA PETROLEUM & CHEM CORP
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