IPC분류정보
국가/구분 |
United States(US) Patent
등록
|
국제특허분류(IPC7판) |
|
출원번호 |
US-0035195
(2002-01-04)
|
우선권정보 |
CN-2001106017 (2001-01-15) |
발명자
/ 주소 |
- Han, Baoping
- Jiang, Lijing
- Shi, Youliang
- Peng, Pai
- Jin, Mei
- Han, Zhaoming
|
출원인 / 주소 |
- China Petroleum & Chemical Corporation, Fushun Research Institute of Petroleum & Petrochemicals, SINOPEC Corporation
|
대리인 / 주소 |
Birch, Stewart, Kolasch & Birch, LLP
|
인용정보 |
피인용 횟수 :
2 인용 특허 :
5 |
초록
▼
The present invention discloses a process for hydroconverting a heavy hydrocarbon chargestock, wherein said chargestock oil is first contacted with a highly active homogeneous hydrogenation catalyst to effect the hydrogenation reaction so that macromolecular radicals of the residue (the precursor of
The present invention discloses a process for hydroconverting a heavy hydrocarbon chargestock, wherein said chargestock oil is first contacted with a highly active homogeneous hydrogenation catalyst to effect the hydrogenation reaction so that macromolecular radicals of the residue (the precursor of coke) form as less as possible, thereby decreasing the output of coke in the hydrocracking of the residue; when the reaction proceeds to a certain extent, a solid powder is added to adsorb the macromolecular radicals of the residue formed during the reaction and lower their reaction activity, thereby preventing them from further condensing to coke and/or depositing due to polymerization. The synergetic action of the two sorts of substances makes it possible to produce substantively no coke or less coke during the hydrogenation of residue in a suspension bed and prolong the operation lifetime of the unit.
대표청구항
▼
1. A process for hydroconverting a heavy hydrocarbon chargestock, which comprises: feeding in an upward way a mixture of a homogeneous catalyst, a heavy hydrocarbon chargestock and hydrogen which is pre-heated to a required temperature into a reactor to carry out a hydrocracking reaction, andintrodu
1. A process for hydroconverting a heavy hydrocarbon chargestock, which comprises: feeding in an upward way a mixture of a homogeneous catalyst, a heavy hydrocarbon chargestock and hydrogen which is pre-heated to a required temperature into a reactor to carry out a hydrocracking reaction, andintroducing a solid powder at the position ¼ to ¾ of a total length of the reactor from the reactor's bottom so as to adsorb macromolecules of residue formed during the reaction and carry them out of the reactor.2. The process according to claim 1, wherein said solid powder has a pore diameter no less than 10 nm; and at least 50% of particles have diameters of less than 45 &mgr;m.3. The process according to claim 2, wherein said solid powder has the pore diameter no less than 15 nm; and at least 50% of the particles have diameters of less than 10 &mgr;m.4. The process according to claim 1, wherein an amount of said solid powder added is 0.01-4.0 based on the total weight of the heavy hydrocarbon chargestock fed into the reactor.5. The process according to claim 1, wherein said solid powder comprises a solid catalyst and/or a solid additive.6. The process according to claim 5, wherein said solid catalyst is Co, Mo, Ni, Zn, K, and/or Fe catalyst supported on a carrier such as alumina, silica-alumina, activated carbon, or amorphous aluminum silicate.7. The process according to claim 5, wherein said solid additive is a solid particle that is less active or inert for hydrogenation.8. The process according to claim 7, wherein said solid additive is a brown coal powder, activated carbon, alumina powder, coke product of a coker, and/or coke product of the suspension bed itself.9. The process according to claim 1, wherein said solid powder is carried into the reactor with a hydrocarbon carrier oil.10. The process according to claim 9, wherein said hydrocarbon carrier oil comprises the unconverted oil in the oil formed in the suspension bed, coker gatch, deasphalted oil, and/or poor quality recycle oil.11. The process according to claim 9, wherein additional homogeneous catalyst is fed together with the feeding of the hydrocarbon carrier oil.12. The process according to claim 1, wherein the conditions for the hydrocracking reaction in said reactor are: temperature 300-600° C., mean liquid hourly volume space velocity 0.1-2 h−1, hydrogen/Oil volume ratio 100-2000, pressure 6.0-20 MPa.13. The process according to claim 1, wherein the conditions for the hydrocracking reaction in said reactor are: temperature of 400-500° C., mean liquid hourly volume space velocity of 0.3-1.5 h−1, hydrogen/oil volume ratio of 300-1500, pressure of 8.0-15 MPa.14. The process according to claim 1, wherein said homogeneous catalyst is one or more selected from the group consisting of oil soluble catalysts and water soluble catalysts, the amount of which is 0.01-1.0% based on the total weight of the heavy hydrocarbon chargestock fed into the reactor.15. The process according to claim 1, wherein an amount of said homogeneous catalyst is 0.01-0.1% based on the total weight of said heavy hydrocarbon chargestock fed into the reactor.16. The process according to claim 1, wherein said homogeneous catalyst is a water soluble catalyst.17. The process according to claim 1, wherein reaction temperature is 410-460° C., space velocity is 1.0-1.5 h−1, hydrogen pressure is 8.0-15.0 MPa, hydrogen/oil ratio (v/v) is 800-1200 and an amount of the solid powder is 0.1-1.2% based upon total weight of said heavy hydrocarbon charged stock fed into the reactor.18. The process according to claim 17 wherein a yield of AGO is 29.2-48.8%.19. The process according to claim 17 wherein a yield of VGO is 32.1-44.2%.
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