Catalytic cracking process with increased production of a gasoline having a low olefin content and a high octane number

Patent metadata

Field	Value
Publication number	US-10808188-B2
Application number	US-201816141619-A
Country	US
Kind code	B2
Filing date	Sep 25, 2018
Priority date	Sep 26, 2017
Publication date	Oct 20, 2020
Grant date	Oct 20, 2020

Abstract

A catalytic cracking process includes the following steps: i) subjecting a heavy feedstock oil to flail catalytic cracking; ii) separating the catalytic cracking reaction product obtained from step i) to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil; iii) splitting the catalytic cracking gasoline to obtain a light gasoline fraction, a medium gasoline fraction and a heavy gasoline fraction; iv) subjecting the catalytic cracking light cycle oil to hydrogenation to obtain a hydrogenated light cycle oil); v) mixing a portion of the light gasoline fraction with at least a portion of the hydrogenated light cycle oil to obtain a mixed fraction; vi) subjecting the mixed fraction to catalytic cracking; and vii) subjecting a portion of the medium gasoline fraction to flail catalytic cracking. The process is capable of producing more catalytic cracking gasoline, reducing the olefin content of the catalytic cracking gasoline, and increasing its octane number.

First claim

What is claimed:

1. A catalytic cracking process, comprising:
i) feeding a heavy feedstock oil into a first riser reactor via a first nozzle for catalytic cracking therein to obtain a catalytic cracking reaction product;
ii) separating the catalytic cracking reaction product to obtain a catalytic cracking gasoline and a catalytic cracking light cycle oil;
iii) separating the catalytic cracking gasoline obtained in step ii) to obtain a light gasoline fraction, a medium gasoline fraction, and a heavy gasoline fraction;
iv) subjecting the catalytic cracking light cycle oil obtained in step ii) to hydrotreating to obtain a hydrogenated light cycle oil;
v) mixing a portion of the light gasoline fraction obtained in step iii) with at least a portion of the hydrogenated light cycle oil obtained in step iv) to obtain a mixed fraction;
vi) feeding the mixed fraction obtained in step v) into jja the first riser reactor or a second reactor via a second nozzle for catalytic cracking therein; and
vii) feeding a portion of the medium gasoline fraction obtained in step iii) into the first riser reactor or the second riser reactor via a third nozzle for catalytic cracking therein,
wherein a cut point between the light gasoline fraction and the medium gasoline fraction is between about 60° C. and about 80° C., and a cut point between the medium gasoline fraction and the heavy gasoline fraction is between about 120° C. and about 130° C.

2. The process according to claim 1 , wherein the heavy feedstock oil, the mixed fraction, and the portion of medium gasoline fraction are respectively fed into the first riser reactor via the first nozzle, the second nozzle, and the third nozzle, disposed along a vertical direction of the riser reactor, wherein the first nozzle is disposed above the second nozzle, and the second nozzle is disposed above the third nozzle.

3. The process according to claim 1 , wherein the heavy feedstock oil is fed into flail the first riser reactor via the first nozzle; and wherein the mixed fraction and the portion of medium gasoline fraction are respectively fed into Hall the second riser reactor via the second nozzle and the third nozzle disposed along a vertical direction of the second riser reactor, and wherein the second nozzle is disposed above the third nozzle.

4. The process according to claim 2 , wherein a reaction time in the riser reactor section between the second nozzle and the first nozzle is between about 0.01 and about 3 seconds.

5. The process according to claim 2 , wherein reaction conditions in the riser reactor comprises a reaction temperature ranging from about 480 to about 650° C., a weight ratio of catalytic cracking catalyst to the heavy feedstock oil ranging from about 2 to about 100, a reaction time of the heavy feedstock oil ranging from about 1 to about 10 seconds, a reaction pressure ranging from about 0.15 to about 0.4 MPa, a weight ratio of steam to the heavy feedstock oil ranging from about 0.01 to about 0.5, and a micro-activity (MAT) of catalytic cracking catalyst of not less than about 55.

6. The process according to claim 3 , wherein reaction conditions in the first riser reactor comprises a reaction temperature ranging from about 480 to about 650° C., catalyst-to-oil ratio ranging from about 2 to about 100, a reaction time ranging from about 1 to about 10 seconds, a reaction pressure ranging from about 0.15 to about 0.4 MPa, and a weight ratio of steam to the heavy feedstock oil ranging from about 0.01 to about 0.5, a micro-activity (MAT) of catalytic cracking catalyst of not less than about 55, and, reaction conditions in the second riser reactor comprises a reaction temperature ranging from about 400 to about 650° C., a catalyst-to-oil ratio ranging from about 5 to about 100, a reaction time ranging from about 0.01 to 10 seconds, a reaction pressure ranging from about 0.15 to about 0.4 MPa, a weight ratio of steam to the total amount of the feedstock oil ranging from about 0.01 to about 0.5, and a micro-activity (MAT) of catalytic cracking catalyst of not less than about 55.

7. The process according to claim 2 , wherein a reaction time in the riser reactor section between the third nozzle and the second nozzle is in a range from about 0.01 to about 2 seconds.

8. The process according to claim 3 , wherein a reaction time in the riser reactor section between the third nozzle and the second nozzle is in a range from about 0.01 to about 2 seconds.

9. The process according to claim 1 , wherein the medium gasoline fraction subjected to flail catalytic cracking in step vii) has a distillation range within a range from about 90 to 130° C.

10. The process according to claim 1 , wherein about 2% to about 90% by weight, of the medium gasoline fraction is subjected to Hail catalytic cracking in step vii).

11. The process according to claim 2 , wherein in step v), about 2% to about 90% by weight of the light gasoline fraction is mixed with about 10% to about 100% by weight of the hydrogenated light cycle oil to obtain the mixed fraction.

12. The process according to claim 1 , in, wherein the hydrotreating step iv) is carried out in the presence of a hydrogenation catalyst comprising a support and an active component supported thereon, the active component is selected from the group consisting of a Group VIB metal, a Group VIII non-noble metal, and combinations thereof, and the support is selected from the group consisting of alumina, silica, amorphous silica-alumina, and combinations thereof.

13. The process according to claim 1 , wherein the hydrotreating step iv) is carried out under conditions comprising a reaction temperature ranging from about 330 to about 450° C., a hydrogen partial pressure ranging from about 6 to about 25 MPa, a volume space velocity ranging from about 0.1 to about 20 h −1 , and a hydrogen-to-oil volume ratio ranging from about 1000 to about 2000 Nm 3 /m 3 .

14. The process according to claim 1 , wherein the hydrotreating step iv) is carried out to an extent that the resultant hydrogenated light cycle oil has a bicyclic aromatics content of no more than about 20% by weight, a hydrogen content of no less than about 11% A by weight, and an initial boiling point of greater than about 165° C.

15. The process according to claim 1 , wherein the first riser reactor and the second riser reactor are independently an equal-diameter riser reactor with or without a fluidized bed reactor, or a variable-diameter riser reactor with or without a fluidized bed reactor.

16. The process according to claim 1 , wherein the catalytic cracking reactions of steps i), vi) and vii) are carried out in the presence of a catalytic cracking catalyst, and the catalytic cracking catalysts used in steps i), vi) and vii) each independently comprises, on a dry basis, about 10% to about 50% by weight of a zeolite, about 5% to about 90% by weight of an inorganic oxide and about 0% to about 70% by weight of a clay, based on the weight of the catalytic cracking catalyst; the zeolite is selected from the group consisting of a Y zeolite with or without a rare earth element, an HY zeolite with or without a rare earth element, a USY zeolite with or without a rare earth element, a Beta zeolite with or without a rare earth element, and combinations thereof; the inorganic oxide is selected from the group consisting of silica, alumina, and combinations thereof; and the clay is kaolin, halloysite, or a mixture thereof.

17. The process according to claim 12 , wherein the active component is nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, or cobalt-molybdenum.

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

• Gong Jianhong
• Li Zekun
• Tang Jinlian
• Mao Anguo
• Zhang Jiushun
• Zhang Yuying
• Long Jun

Classifications

• C10G47/00

  Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06) · CPC title

• C10G45/60 Primary

  characterised by the catalyst used · CPC title

• C10G2300/1048

  Middle distillates · CPC title

• C10G2400/02

  Gasoline · CPC title

• C10G51/026

  only catalytic cracking steps · CPC title