Process for the selective hydrogenation and hydrodesulferization of a pyrolysis gasoline feedstock
원문보기
IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C07C-007/163
C10G-045/32
C10G-045/02
C10G-069/06
출원번호
US-0376531
(2010-06-09)
등록번호
US-9260670
(2016-02-16)
국제출원번호
PCT/US2010/037864
(2010-06-09)
§371/§102 date
20120116
(20120116)
국제공개번호
WO2010/144512
(2010-12-16)
발명자
/ 주소
Grenoble, Dane Clark
Himelfarb, Paul Benjerman
Treybig, Michael Norris
Vanderwilp, Brian Scott
출원인 / 주소
Shell Oil Company
인용정보
피인용 횟수 :
1인용 특허 :
8
초록▼
Disclosed is a process for the selective hydrogenation of diolefins and sulfur compounds that are contained in a pyrolysis gasoline feedstream. The process includes utilizing a single hydrotreating reaction stage by introducing the pyrolysis gasoline feedstock that includes a diolefin concentration
Disclosed is a process for the selective hydrogenation of diolefins and sulfur compounds that are contained in a pyrolysis gasoline feedstream. The process includes utilizing a single hydrotreating reaction stage by introducing the pyrolysis gasoline feedstock that includes a diolefin concentration and an organic sulfur concentration into a reactor that is loaded with a high activity hydrotreating catalyst and which is operated under selective hydrogenation conditions. A reactor effluent having a reduced diolefin concentration and a reduced organic sulfur concentration is yielded from the reactor and is separated into a portion that is recycled as a reactor feed. The remaining portion of the reactor effluent is passed downstream for further processing or handling.
대표청구항▼
1. A process for the selective hydrogenation of diolefins and sulphur compounds contained in a pyrolysis gasoline feedstock, comprising a diolefin concentration exceeding 3 wt % and an organic sulfur concentration exceeding 50 ppmw, wherein said process comprises: introducing a hydrocarbon stream th
1. A process for the selective hydrogenation of diolefins and sulphur compounds contained in a pyrolysis gasoline feedstock, comprising a diolefin concentration exceeding 3 wt % and an organic sulfur concentration exceeding 50 ppmw, wherein said process comprises: introducing a hydrocarbon stream that comprises said pyrolysis gasoline feedstock into a reactor that contains a single hydrotreating reaction stage comprising hydrotreating catalyst and operated at selective hydrogenation conditions, wherein said hydrocarbon stream is contacted with said hydrotreating catalyst;yielding from said reactor a reactor effluent comprising a reduced diolefin concentration of less than 10 ppmw, a reduced organic sulfur concentration of less than 3 ppmw, and an aromatics content of at least 90 wt % of a reactor inlet aromatics content;separating said reactor effluent into a portion of said reactor effluent and a remaining portion of said reactor effluent;and introducing as a recycle said portion of said reactor effluent into said reactor wherein the weight ratio of said recycle to said hydrocarbon stream is greater than 1:1. 2. A process as recited in claim 1, wherein said selective hydrogenation conditions include a feed inlet temperature to said reactor that is in the range of from 100° C. to 250° C., a reactor operating pressure in the range of from 10 bara to 100 bara, and a weight hourly space velocity in the range of from 0.2 to 40 hr−1. 3. A process as recited in claim 2, wherein said pyrolysis gasoline feedstock further comprises monoolefins at a concentration in the range of from 1 to 20 wt % and aromatics at a concentration in the range of from 10 wt % to 80 wt %, and wherein said reactor effluent has a reduced monoolefin concentration as measured by a bromine number of less than 1 and aromatics content of at least 95 wt % of said hydrocarbon stream. 4. A process as recited in claim 2, wherein said hydrotreating catalyst comprises molybdenum and either nickel or cobalt supported on alumina. 5. A process as recited in claim 4, wherein said step of separating said reactor effluent includes: separating said reactor effluent into a total reactor effluent portion of said reactor effluent and a total reactor effluent remaining portion of said reactor effluent; andusing said total reactor effluent portion as a total recycle stream of said recycle. 6. A process as recited in claim 4, wherein said step of separating said reactor effluent includes: passing said reactor effluent to a separator for separating said reactor effluent into a liquid fraction and a vapor fraction;passing said liquid fraction to a fractionator for separating said liquid fraction into a light cut and a heavy cut;separating said heavy cut into a heavy cut portion of said heavy cut and a heavy cut remaining portion of said heavy cut; andusing said heavy cut portion of said heavy cut as a heavy cut recycle stream of said recycle. 7. A process as recited in claim 4, wherein said step of separating said reactor effluent includes: passing said reactor effluent to a separator for separating said reactor effluent into a liquid fraction and a vapor fraction;separating said liquid fraction into a liquid fraction portion of said liquid fraction and a liquid fraction remaining portion of said liquid fraction; andusing said liquid fraction portion of said liquid fraction as a first recycle stream of said recycle. 8. A process as recited in claim 7, wherein said step of separating said reactor effluent further includes: passing said liquid fraction remaining portion of said liquid fraction to a fractionater for separating said liquid fraction remaining portion of said liquid fraction into a light cut and a heavy cut;separating said heavy cut into a heavy cut portion of said heavy cut and a heavy cut remaining portion of said heavy cut; andusing said heavy cut portion of said heavy cut as a second recycle stream of said recycle. 9. A process as recited in claim 6, further comprising: introducing said vapor fraction into said reactor along with said hydrocarbon stream and said recycle. 10. A process for the selective hydrogenation of monoolefins, diolefins, and sulfur compounds contained in a pyrolysis gasoline feedstock, wherein said pyrolysis gasoline feedstock having a monoolefins concentration, a diolefins concentration, an aromatics concentration, and an organic sulfur concentration, and wherein said process comprises: introducing a hydrocarbon stream that comprises said pyrolysis gasoline feedstock into a reactor that contains a single hydrotreating reaction stage comprising hydrotreating catalyst and operated under selective hydrogenation conditions, wherein said hydrocarbon stream is contacted with said hydrotreating catalyst;yielding from a reactor outlet of said reactor a reactor effluent having a reduced monoolefin concentration, a reduced diolefin concentration, a reduced organic sulfur concentration, and an aromatics content of at least 90 wt % of a reactor inlet aromatics content; andintroducing as a recycle a portion of said reactor effluent into said reactor wherein the weight ratio of said recycle to said hydrocarbon stream is greater than 1:1. 11. A process as recited in claim 10, wherein said monoolefins concentration is in the range of from 1 to 20 wt %, said diolefins concentration exceeds 3 wt %, said aromatics concentration is in the range of from 10 wt % to 80 wt %, and said organic sulphur concentration exceeds 50 ppmw, and wherein said reduced monoolefin concentration is measured by a bromine number of less than 1, said reduced diolefin concentration is less than 10 ppmw, and said reduced organic sulfur concentration is less than 3 ppmw. 12. A process as recited in claim 11, further comprising: introducing into said reactor with said hydrocarbon stream a portion of said reactor effluent as a recycle at a rate so as to provide a weight ratio recycle-to-hydrocarbon stream that is greater than 1:1. 13. A process as recited in claim 12, wherein said selective hydrogenation conditions include a feed inlet temperature to said reactor that is in the range of from 100° C. to 250° C., a reactor operating pressure in the range of from 10 bara to 100 bara, and a weight hourly space velocity in the range of from 0.2 to 40 hr−1. 14. A process as recited in claim 13, wherein said hydrotreating catalyst comprises molybdenum and either nickel or cobalt supported on alumina.
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이 특허에 인용된 특허 (8)
Gerald Meyer DE; Ekkehard Schwab DE; Michael Hesse DE; Peter Trubenbach DE; Hans-Joachim Muller DE, Catalyst and processes for the selective hydrogenation of unsaturated compounds in hydrocarbon streams.
Rudolf A. Overbeek ; Robert E. Trubac ; Chiung Yuan Huang ; Marino Rota CH; Nelleke van der Puil, Selective hydrogenation process and catalyst therefor.
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