Process for treating a hydrocarbon-containing feed
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IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C10G-047/06
C10G-047/02
C10G-047/24
C10G-047/26
출원번호
US-0010934
(2011-01-21)
등록번호
US-8597497
(2013-12-03)
발명자
/ 주소
Milam, Stanley Nemec
Reynolds, Michael Anthony
Wellington, Scott Lee
출원인 / 주소
Shell Oil Company
인용정보
피인용 횟수 :
0인용 특허 :
5
초록▼
A process for treating a hydrocarbon-containing feedstock is provided in which a hydrocarbon-containing feed comprising at least 20 wt. % of heavy hydrocarbons is mixed with hydrogen and at least one catalyst to produce a hydrocarbon-containing product. The hydrocarbon-containing feedstock, the cata
A process for treating a hydrocarbon-containing feedstock is provided in which a hydrocarbon-containing feed comprising at least 20 wt. % of heavy hydrocarbons is mixed with hydrogen and at least one catalyst to produce a hydrocarbon-containing product. The hydrocarbon-containing feedstock, the catalyst(s), and the hydrogen are provided to a mixing zone and blended in the mixing zone at a temperature of from 375° C. to 500° C. A vapor comprised of hydrocarbons that are vaporizable at the temperature and pressure within the mixing zone is separated from the mixing zone, and, apart from the mixing zone, the vapor is condensed to produce a liquid hydrocarbon-containing product containing at least 85% of the atomic carbon initially present in the hydrocarbon-containing feedstock and containing at most 2 wt. % hydrocarbons having a boiling point of at least 538° C.
대표청구항▼
1. A process for cracking a hydrocarbon-containing feedstock, comprising: providing a hydrocarbon-containing feedstock to a mixing zone, where the hydrocarbon-containing feedstock is selected to contain at least 20 wt. % hydrocarbons having a boiling point of greater than 538° C. as determined in ac
1. A process for cracking a hydrocarbon-containing feedstock, comprising: providing a hydrocarbon-containing feedstock to a mixing zone, where the hydrocarbon-containing feedstock is selected to contain at least 20 wt. % hydrocarbons having a boiling point of greater than 538° C. as determined in accordance with ASTM Method D5307;providing a catalyst to the mixing zone;continuously or intermittently providing hydrogen to the mixing zone and blending the hydrogen, the hydrocarbon-containing feedstock, and the catalyst in the mixing zone at a temperature of from 375° C. to 500° C. and at a total pressure of from 6.9 MPa to 27.5 MPa to produce: a) a vapor comprised of hydrocarbons that are vaporizable at the temperature and the pressure within the mixing zone; andb) a hydrocarbon-depleted feed residuum comprising hydrocarbons that are liquid at the temperature and the pressure within the mixing zone;continuously or intermittently separating at least a portion of the vapor from the mixing zone while retaining at least a portion of the hydrocarbon-depleted feed residuum in the mixing zone;apart from the mixing zone, condensing a liquid hydrocarbon-containing product that contains at least 90% of the atomic carbon initially contained in the hydrocarbon-containing feedstock and that contains less than 2 wt. % hydrocarbons having a boiling point of greater than 538° C. as determined in accordance with ASTM Method D5307 from at least a portion of the vapor separated from the mixing zone. 2. The process of claim 1 wherein the hydrocarbon-containing feedstock is continuously or intermittently provided to the mixing zone. 3. The process of claim 2 wherein the combined volume of the hydrocarbon-depleted feed residuum, the catalyst, and the hydrocarbon-containing feedstock in the mixing zone defines a mixture volume, and wherein the hydrocarbon-containing feedstock is provided to the mixing zone at a flow rate of at least 350 kg/hr per m3 of the mixture volume in the mixing zone. 4. The process of claim 2 wherein: the mixing zone is located in a reactor;the reactor has a reactor volume;the hydrocarbon-containing feedstock and the catalyst initially provided to the mixing zone define an initial mixture volume, where the initial mixture volume is from 5% to 97% of the reactor volume; andwhere the mixture volume of the catalyst, the hydrocarbon-containing feedstock, and the hydrocarbon-depleted feed residuum is maintained at a level of from 10% to 1940% of the initial mixture volume. 5. The process of claim 4 wherein the vapor separated from the mixing zone is separated from the reactor. 6. The process of claim 1 wherein the hydrocarbon-depleted feed residuum is blended with hydrogen and the catalyst in the mixing zone while separating at least a portion of the vapor from the mixing zone. 7. The process of claim 1 wherein the liquid hydrocarbon-containing product condensed from the portion of the vapor separated from the mixing zone contains less than 1 wt. % hydrocarbons having a boiling point of greater than 538° C. as determined in accordance with ASTM Method D5307. 8. The process of claim 1 further comprising the steps of: continuously or intermittently providing hydrogen sulfide to the mixing zone and blending the hydrogen sulfide with the hydrocarbon-containing feedstock, the catalyst, and hydrogen in the mixing zone, wherein hydrogen sulfide is provided to the mixing zone at a mole ratio of hydrogen sulfide to hydrogen of at least 0.5:9.5 up to 1:1, where hydrogen and hydrogen sulfide are provided for mixing such that the combined hydrogen and hydrogen sulfide partial pressures provide at least 60% of the total pressure. 9. The process of claim 1 wherein the hydrocarbon-containing feedstock contains at least 30 wt. % of hydrocarbons having a boiling point of greater than 538° C. as determined in accordance with ASTM Method D5307. 10. The process of claim 1 wherein the hydrocarbon-containing feedstock contains at least 30 wt. % of hydrocarbons that have a boiling point of 538° C. or less as determined in accordance with ASTM Method D5307. 11. The process of claim 2 wherein the hydrocarbon-containing product condensed from the vapor separated from the mixing zone contains at least 40% of the atomic sulfur present in the hydrocarbon-containing feedstock. 12. The process of claim 1 wherein the hydrocarbon-containing product condensed from the vapor separated from the mixing zone contains at least 40% of the atomic nitrogen present in the hydrocarbon-containing feedstock. 13. The process of claim 1 wherein the catalyst provided to mixing zone has an acidity as measured by ammonia chemisorption of at most 200 μmol ammonia per gram of catalyst. 14. The process of claim 13 wherein at least one catalyst provided to the mixing zone and blended with the hydrocarbon-containing feedstock and hydrogen comprises a metal of Columns 6-10 of the Periodic Table or a compound of a metal of Columns 6-10 of the Periodic Table. 15. The process of claim 13 wherein at least one catalyst comprises a metal of Column 6, 14, or 15 of the Periodic Table or a compound of a metal of Column 6, 14, or 15 of the Periodic Table and a metal of Column(s) 3 or 7-15 of the Periodic Table or a compound of a metal of Column(s) 3 or 7-15 of the Periodic Table. 16. The process of claim 1 wherein the catalyst comprises a material comprised of a first metal and a second metal where the first metal comprises a metal selected from the group consisting of Cu, Ni, Co, Fe, Ag, Mn, Zn, Sn, Ru, La, Ce, Pr, Sm, Eu, Yb, Lu, Dy, Pb, Sb, and Bi, where the second metal comprises a metal selected from the group consisting of Mo, W, V, Sn, and Sb, where the second metal is not the same as the first metal, and wherein the material is comprised of at least three linked chain elements, the chain elements comprising a first chain element including the first metal and having a structure according to formula (I) and a second chain element including the second metal and having a structure according to formula (II) where at least one chain element in the material is a first chain element and at least one chain element in the material is a second chain element, where chain elements in the material are linked by bonds between the two sulfur atoms of a chain element and the metal of an adjacent chain element. 17. The process of claim 1 wherein the catalyst is comprised of a material comprised of a first metal and a second metal where the first metal comprises a metal selected from the group consisting of Cu, Ni, Co, Fe, Ag, Mn, Zn, Sn, Ru, La, Ce, Pr, Sm, Eu, Yb, Lu, Dy, Pb, Sb, and Bi where the second metal comprises a metal selected from the group consisting of Mo, W, V, Sn and Sb, where the second metal is not the same as the first metal, and wherein at least a portion of the material of the catalyst has a structure according to a formula selected from the group consisting of formula (III), formula (IV), formula (V), and formula (VI): where M is either the first metal or the second metal, and at least one M is the first metal and at least one M is the second metal; where M is either the first metal or the second metal, at least one M is the first metal and at least one M is the second metal, and X is selected from the group consisting of SO4, PO4, oxalate (C2O4), acetylacetonate, acetate, citrate, tartrate, Cl, Br, I, ClO4, and NO3; where M is either the first metal or the second metal, at least one M is the first metal and at least one M is the second metal, and X is selected from the group consisting of SO4, PO4, oxalate (C2O4), acetylacetonate, acetate, citrate, tartrate, Cl, Br, I, ClO4, and NO3; where M is either the first metal or the second metal, at least one M is the first metal and at least one M is the second metal, and X is selected from the group consisting of SO4, PO4, oxalate (C2O4), acetylacetonate, acetate, citrate, tartrate, Cl, Br, I, ClO4, and NO3. 18. The process of claim 1 wherein at least one catalyst is a solid particulate material having a particle size distribution having a median particle size or a mean particle size of from 50 nm to 1 μm. 19. The process of claim 1 wherein the temperature in the mixing zone is selected and controlled to be at least 430° C. 20. The process of claim 1 wherein the hydrocarbon-containing product contains at most 0.001 wt. % vanadium and at most 0.001 wt. % nickel. 21. The process of claim 1 wherein the hydrocarbon-depleted feed residuum contains less than 0.02 grams of substances insoluble in toluene as determined in accordance with ASTM Method D4072, excluding the catalyst(s), per gram of hydrocarbon-containing feedstock provided to the mixing zone. 22. The process of claim 1 further comprising the steps of: separating a stream containing liquids and solids from the mixing zone;separating solids from the stream containing liquids and solids to produce a liquid stream and a solid material; andproviding the liquid stream to the mixing zone. 23. A process for cracking a hydrocarbon-containing feedstock, comprising: providing a hydrocarbon-containing feedstock to a mixing zone, where the hydrocarbon-containing feedstock is selected to contain at least 20 wt. % residue;providing at least one catalyst to the mixing zone;continuously or intermittently providing hydrogen to the mixing zone and blending the hydrogen, the hydrocarbon-containing feedstock, and the catalyst in the mixing zone at a temperature of from 375° C. to 500° C. and at a pressure of from 3.4 MPa to 27.5 MPa to produce: a) a vapor comprised of hydrocarbons that are vaporizable at the temperature and the pressure within the mixing zone; andb) a hydrocarbon-depleted feed residuum comprising hydrocarbons that are liquid at the temperature and the pressure within the mixing zone;continuously or intermittently separating at least a portion of the vapor from the mixing zone while retaining in the mixing zone at least a portion of the hydrocarbon-depleted feed residuum comprising hydrocarbons that are liquid at the temperature and pressure within the mixing zone;apart from the mixing zone, condensing a liquid hydrocarbon-containing product that contains at least 90% of the atomic carbon initially contained in the hydrocarbon-containing feedstock and that contains less than 2 wt. % hydrocarbons having a boiling point of at least 538° C. as determined in accordance with ASTM Method D5307 from at least a portion of the vapor separated from the mixing zone.
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이 특허에 인용된 특허 (5)
Lopez, Jaime; McKinney, Joel D.; Pasek, Eugene A., Heavy oil hydroprocessing.
Stiefel Edward I. (Bridgewater NJ) Pan Wie-Hin (Fanwood NJ) Chianelli Russell R. (Somerville NJ) Ho Teh C. (Scotch Plains NJ), Hydrotreating using self-promoted molybdenum and tungsten sulfide catalysts formed from bis(tetrathiometallate) precurso.
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