Process for the treatment of heavy oils using light hydrocarbon components as a diluent
IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C10G-065/12
출원번호
US-0502357
(2009-07-14)
등록번호
US-9260671
(2016-02-16)
발명자
/ 주소
Shafi, Raheel
Hamad, Esam Z.
Kressmann, Stephane Cyrille
Alzaid, Ali Hussain
출원인 / 주소
SAUDI ARABIAN OIL COMPANY
대리인 / 주소
Bracewell & Giuliani LLP
인용정보
피인용 횟수 :
0인용 특허 :
61
초록▼
The present invention relates to a process for the treatment of heavy oils using a catalytic hydrotreating process. More specifically, the invention relates to the presence of light hydrocarbon components in conjunction with the heavy oils for improved treatment of the heavy oils utilizing moderate
The present invention relates to a process for the treatment of heavy oils using a catalytic hydrotreating process. More specifically, the invention relates to the presence of light hydrocarbon components in conjunction with the heavy oils for improved treatment of the heavy oils utilizing moderate temperature and pressure.
대표청구항▼
1. A process for upgrading of heavy oils comprising the steps of: feeding a heavy oil feed stream to a hydrodemetalization reaction vessel, the hydrodemetalization reaction vessel containing a hydrodemetalization catalyst, the hydrodemetalization catalyst being operable to remove a substantial quant
1. A process for upgrading of heavy oils comprising the steps of: feeding a heavy oil feed stream to a hydrodemetalization reaction vessel, the hydrodemetalization reaction vessel containing a hydrodemetalization catalyst, the hydrodemetalization catalyst being operable to remove a substantial quantity of metal compounds from the heavy oil feed stream;feeding a hydrogen source to the hydrodemetalization reaction vessel, the hydrogen source having a hydrogen pressure in the range of 50 to 150 bar; andfeeding a light hydrocarbon diluent to the hydrodemetalization reaction vessel, the light hydrocarbon diluent being substantially in liquid phase,wherein the feeding of the heavy oil feed stream and the hydrogen source and the light hydrocarbon diluent to the hydrodemetalization reaction vessel defines a feed rate, the feed rate further defining a total liquid hourly space velocity within a predetermined liquid hourly space velocity range of 0.1 hr−1 to 5 hr−1 such that a combined effluent stream is produced and removed from the hydrodemetalization reaction vessel;the process further comprising;feeding the combined effluent stream to a hydrodesulfurization reaction vessel, the hydrodesulfurization reaction vessel containing a hydrodesulfurization catalyst operable to remove a substantial amount of sulfur from the combined effluent such that a hydrodesulfurization catalyst effluent is produced;feeding the hydrodesulfurization catalyst effluent to a hydroconversion reaction vessel, the hydroconversion reaction vessel containing a hydroconversion catalyst, the hydroconversion catalyst being operable to convert the hydrodesulfurization catalyst effluent to a hydroconverted product, the hydroconverted product having, an increased API gravity as compared to the heavy oil feed stream;feeding the hydroconverted product to a separation unit, the separation unit operable to separate the hydroconverted product into a process gas component stream and a liquid product;feeding the liquid product to a flash vessel to separate a light hydrocarbon fraction and a final liquid product, the final liquid product having a reduced sulfur content, reduced metal content and increased API gravity in comparison to the heavy oil feed stream;recycling at least a portion of the light hydrocarbon fraction to the hydrodemetalization reaction vessel; andcombining the recycled light hydrocarbon fraction with a fresh light hydrocarbon diluent to form the light hydrocarbon diluent and to thereby recycle the light hydrocarbon diluent to the hydrodemetalization reaction vessel to reduce coke formation. 2. The process of claim 1, further comprising the step of: recycling at least a portion of the process gas component stream to the hydrodemetalization reaction vessel. 3. The process of claim 1 wherein the separation unit is operable to remove sulfur components from the hydroconverted product. 4. The process of claim 1 wherein the sulphur removed, from the heavy feed oil stream in the hydrodesulfurization reaction vessel is at least 30 wt % of sulphur found in the heavy oil feed stream. 5. The process of claim 1 wherein the light hydrocarbon diluent is a mixture of hydrocarbons derived from crude oil and defining a final boiling point,the heavy oil feed stream further defines an initial boiling point, andthe final boiling point of the light hydrocarbon diluent does not exceed the initial boiling point of the heavy oil feed stream. 6. The process of claim 1 wherein at least a portion of the light hydrocarbon fraction is added to the heavy oil feed stream. 7. The process of claim 1 wherein the light hydrocarbon diluent is present at a ratio of at least 5 wt % compared to the heavy oil feed stream. 8. The process of claim 1 wherein the light hydrocarbon diluent comprises light hydrocarbons selected from the group consisting of C15-C25 alkyl hydrocarbons. 9. The process of claim 1 wherein the light hydrocarbon diluent comprises less than about 30 wt % aromatics and has a final boiling point less than about 335° C. 10. The process of claim 1 wherein a ratio of the light hydrocarbon diluent to heavy crude oil in the heavy oil feed stream, while the process is at steady state, is 10 wt %, and a circulation rate of the light hydrocarbon diluent is between 5 wt % to 20 wt % of a feed of the fresh light hydrocarbon diluent for reduced crudes. 11. The process of claim 1, wherein an average deactivation rate of hydroprocessing catalysts for the production of reduced sulfur crude oil is 1° C. per month. 12. A process for upgrading of heavy oils to increase diesel comprising the steps of: feeding a heavy oil feed stream to a hydrodemetalization reaction vessel, the hydrodemetalization reaction vessel containing a hydrodemetalization catalyst, the hydrodemetalization catalyst being operable to remove a substantial quantity of metal compounds from the heavy oil feed stream;feeding a hydrogen source to the hydrodemetalization reaction vessel, the hydrogen source having a hydrogen pressure in the range of 50 to 150 bar; andfeeding a light hydrocarbon diluent to the hydrodemetalization reaction vesselwherein the feeding of the heavy oil feed stream and the hydrogen source and the light hydrocarbon diluent to the hydrodemetalization reaction vessel defines a feed rate, the feed rate further defining a total liquid hourly space velocity within a predetermined liquid hourly space velocity range of 0.1 hr−1 to 5 hr−1 that a combined, effluent stream is produced and removed from the hydrodemetalization reaction vessel;the method further comprising:feeding the combined effluent stream to a hydrodesulfurization reaction vessel, the hydrodesulfurization reaction vessel containing a hydrodesulfurization catalyst operable to remove a substantial amount of sulfur from the combined effluent such that a hydrodesulfurization catalyst effluent is produced;feeding the hydrodesulfurization catalyst effluent to a separation unit, the separation unit operable to separate the hydrodesulfurization catalyst effluent into a process gas component stream and a liquid product;recycling at least a portion of the gas component stream to the hydrodemetalization reaction vessel;feeding the liquid product to a flash vessel to separate a light hydrocarbon fraction and a final liquid product, the final liquid product having a higher diesel content as compared to the heavy oil feed stream;recycling at least a portion of the light hydrocarbon fraction to the hydrodemetalization reaction vessel; andcombining the recycled light hydrocarbon fraction with a fresh light hydrocarbon diluent to form the light hydrocarbon diluent and to thereby recycle the light hydrocarbon diluent to the hydrodemetalization reaction vessel to reduce coke formation.
연구과제 타임라인
LOADING...
LOADING...
LOADING...
LOADING...
LOADING...
이 특허에 인용된 특허 (61)
Van Zijll Langhout Wouter C. (The Hague NLX) Pegels Abraham A. (The Hague NLX) Wijffels Joannes B. (The Hague NLX), Apparatus for the hydrogenation of heavy hydrocarbon oils.
Morales Alfredo L. (San Antonio de Los Altos VEX) Galiasso Roberto (San Antonio de Los Altos VEX) Carrasquel Angel R. (Los Teques VEX) Salazar Jose A. (Los Teques VEX), Catalyst for removing sulfur and metal contaminants from heavy crudes and residues.
Morales Alfredo L. (San Antonio de Los Altos VEX) Galiasso Roberto (San Antonio de Los Altos VEX) Carrasquel Angel R. (Los Teques VEX) Salazar Jose A. (Los Teques VEX), Catalyst for removing sulfur and metal contaminants from heavy crudes and residues.
de Agudelo M. M. Ramirez (Los Teques VEX) Galarraga C. E. (Los Teques VEX), Catalyst for the simultaneous hydrodemetallization and hydroconversion of heavy hydrocarbon feedstocks.
Bearden ; Jr. Roby (Baton Rouge LA) Aldridge Clyde L. (Baton Rouge LA) Pine Lloyd A. (Baton Rouge LA), Catalysts and hydrocarbon treating processes utilizing the same.
Morimoto ; Tatsuo ; Nakamura ; Munekazu ; Inooka ; Masayoshi ; Yawata ; Teizaburo, Catalysts for hydrodemetallization of hydrocarbons containing metallic compounds as impurities and process for hydro-tr.
Duddy John E. ; Abrams Lawrence M. ; Hildebrandt Steven J., Catalytic multi-stage hydrodesulfurization of metals-containing petroleum residua with cascading of rejuvenated catalyst.
Baird ; Jr. William C. (Baton Rouge LA) Bearden ; Jr. Roby (Baton Rouge LA), Combined desulfurization and hydroconversion with alkali metal hydroxides.
Hinojos Antonio R. (Bartlesville OK) Bone ; Jr. Bertram T. (Bartlesville OK), Control of a hydrofining process for hydrocarbon-containing feed streams which process employs a hydrodemetallization re.
Heck Roland H. (Pennington NJ) Reischman Tom (Lambertville NJ) Teitman Gerald J. (Vienna VA) Viscontini Salvatore T. M. (Northampton PA), Delayed coking with refinery caustic.
Baird ; Jr. William C. (Baton Rouge LA) Beardon ; Jr. Roby (Baton Rouge LA), Desulfurization and hydroconversion of residua with sodium hydride and hydrogen.
Bonnell William S. (Mount Lebanon PA) Christman Robert D. (Pittsburgh PA) Lasher Jordan S. (Pittsburgh PA) Paraskos John A. (Pittsburgh PA) Yanik Stephen J. (Valencia PA), Hydrodesulfurization apparatus with upstaged reactor zones.
Frayer ; James Albert ; Lese ; Henri K. ; McKinney ; Joel Drexler ; Met zer ; Kirk J. ; Paraskos ; John Angelo, Hydrodesulfurization process employing a guard reactor.
Bonnell William S. (Pittsburgh Mt. Lebanon PA) Christman Robert D. (Pittsburgh Pittsburgh PA) Lasher Jordan S. (Pittsburgh Pittsburgh PA) Paraskos John A. (Pittsburgh PA) Yanik Stephen J. (Valencia P, Hydrodesulfurization process with upstaged reactor zones.
Sato Goro (Kitakyushu JPX) Higashi Hidehiro (Kitakyushu JPX) Shirono Katsuhiro (Kitakyushu JPX) Eto Yoshio (Kitakyushu JPX), Hydrotreating process for heavy hydrocarbon oils.
Renard Pierre (Saint Nom La Breteche FRX), Hydrotreatment method for a petroleum residue or heavy oil with a view to refining them and converting them to lighter f.
Stangeland Bruce E. (Berkeley CA) Kramer David C. (San Anselmo CA) Smith David S. (Baton Rouge LA) McCall James T. (Baton Rouge LA) Scheuerman Georgieanna L. (Moraga CA) Bachtel Robert W. (El Cerrito, Method and apparatus for an on-stream particle replacement system for countercurrent contact of a gas and liquid feed st.
Morel Frederic,FRX ; Duplan Jean-Luc,FRX ; Billon Alain,FRX ; Kressmann Stephane,FRX, Process for converting heavy petroleum fractions that comprise a distillation stage, ebullated-bed hydroconversion stages of the vacuum distillate, and a vacuum residue and a catalytic cracking stage.
Frederic Morel FR; Stephane Kressmann FR; Jean-Luc Duplan FR, Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step.
Morel, Frederic; Kressmann, Stephane; Colyar, James, Process for converting petroleum fractions, comprising an ebullated bed hydroconversion step, a separation step, a hydrodesulphurization step and a cracking step.
Beaton William I. (Wheaton IL) Hensley Albert L. (Munster IN) Evans April J. (Naperville IL), Process for demetallation and desulfurization of heavy hydrocarbons.
Baird ; Jr. ; William Chalmers ; Bearden ; Jr. ; Roby ; Bollinger ; Jr. ; Ralph Louis, Process for desulfurization of residua with sodamide-hydrogen and regeneration of sodamide.
Baird ; Jr. William Chalmers (Baton Rouge LA) Bearden ; Jr. Roby (Baton Rouge LA) Bollinger ; Jr. Ralph Louis (Baton Rouge LA), Process for desulfurization of residua with sodamide-hydrogen and regeneration of sodamide.
Billon Alain,FRX ; Morel Frederic,FRX ; Kressmann Stephane,FRX ; Kim Sun Dong,KRX ; Ha Sung Ki,KRX ; Heor Haen,KRX, Process for hydrotreatment of a heavy hydrocarbon fraction using permutable reactors and introduction of a middle distillate.
Galiasso Roberto E. (San Antonio de Los Altos VEX) Arias Beatriz R. (Caracas VEX) Caprioli Lino (Caracas VEX) Garcia Juan (San Antonio de Los Altos VEX) Kum Humberto (Los Teques VEX), Process for the conversion of heavy hydrocarbon feedstocks characterized by high molecular weight, low reactivity and hi.
Lindsay David A. (Orange CA) Smith Michael C. (Costa Mesa CA) Albertson Walter (Brea CA) Schwedock Marvin J. (Costa Mesa CA), Temperature controlled catalytic demetallization of hydrocarbons.
Myers John W. (Bartlesville OK) Parrott Stephen L. (Bartlesville OK) Sughrue Edward L. (Bartlesville OK), Two-stage hydrotreating of a mixture of resid and light cycle oil.
Reynolds, Bruce E.; Lam, Fred W.; Chabot, Julie; Antezana, Fernando J.; Bachtel, Robert; Gibson, Kirk R.; Threlkel, Richard; Leung, Pak C., Upflow reactor system with layered catalyst bed for hydrotreating heavy feedstocks.
※ AI-Helper는 부적절한 답변을 할 수 있습니다.