Cross flow gas-liquid catalytic reaction systems
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IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C10G-045/00
C10G-045/72
C10G-065/12
B01J-008/04
B01J-008/00
B01J-008/02
C10G-045/10
C10G-047/14
C10G-049/00
출원번호
US-0926413
(2013-06-25)
등록번호
US-9416324
(2016-08-16)
발명자
/ 주소
Korsten, Hans G.
출원인 / 주소
EXXONMOBIL RESEARCH AND ENGINEERING COMPANY
대리인 / 주소
Carter, Larry E.
인용정보
피인용 횟수 :
0인용 특허 :
10
초록▼
A gas-liquid catalyzed reaction is performed by introducing at least a portion of the reactive gas into the catalyst as a cross-flow or radial-flow stream. Introducing at least a portion of the reactive gas as a radial flow stream allows the reactive gas to travel through the catalyst bed along a sh
A gas-liquid catalyzed reaction is performed by introducing at least a portion of the reactive gas into the catalyst as a cross-flow or radial-flow stream. Introducing at least a portion of the reactive gas as a radial flow stream allows the reactive gas to travel through the catalyst bed along a shorter path length. This reduces the pressure drop for the radial flow portion of the gas. The reactive gas can be introduced into the catalyst bed at various heights relative to the height of the catalyst bed.
대표청구항▼
1. A method for performing a catalyzed gas-liquid reaction, comprising: providing a first catalyst bed in a reactor, the reactor including an inner conduit that occupies a portion of the volume of the first catalyst bed and an outer gap between the first catalyst bed and a wall of the reactor, where
1. A method for performing a catalyzed gas-liquid reaction, comprising: providing a first catalyst bed in a reactor, the reactor including an inner conduit that occupies a portion of the volume of the first catalyst bed and an outer gap between the first catalyst bed and a wall of the reactor, wherein the reactor further comprises a reactor effluent outlet which is fluidly connected to the first catalyst bed;exposing a downward axial flow of a hydrocarbon feedstock to a first catalyst located in the first catalyst bed in the presence of a reactive gas under effective processing conditions to produce a first liquid reaction effluent; anddelivering at least a portion of the reactive gas flow into the first catalyst bed via the inner conduit as a radial flow and at least a portion of the reactive gas flows directly into the catalyst bed in a co-current manner with the feedstock, thereby contacting the hydrocarbon feedstock and the first catalyst in the first catalyst bed under first effective processing conditions;wherein at least about 50 vol % of the reactive gas flow exits the first catalyst bed by passing into the outer gap, and at least 50 vol % of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 2. The method of claim 1, wherein the first effective processing conditions comprise effective hydroprocessing conditions and the reactive gas comprises hydrogen. 3. The method of claim 1, wherein passing at least about 50 vol % of the reactive gas flow into the outer gap comprises passing the at least about 50 vol % of the reactive gas flow through a gas/liquid selective membrane structure that separates the first catalyst in the first catalyst bed from the outer gap. 4. The method of claim 3, wherein the gas/liquid selective membrane structure is comprised of a gas permeable ceramic membrane. 5. The method of claim 3, wherein the gas/liquid selective membrane structure is comprised of a gas permeable metal membrane. 6. The method of claim 1, wherein at least about 25 vol % of the reactive gas is delivered into the first catalyst bed as a radial gas flow. 7. The method of claim 1, wherein the at least a portion of the reactive gas flow is delivered into the first catalyst bed at a plurality of heights relative to a height of the first catalyst bed. 8. The method of claim 1, wherein substantially all of the reactive gas flow is delivered into the first catalyst bed as a radial gas flow. 9. The method of claim 1, wherein at least 90 vol % of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 10. The method of claim 9, wherein substantially all of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 11. The method of claim 1, wherein the reactor is cylindrical and the axial flow is in a direction parallel with the central axis of the cylinder and the radial flow is in any direction that is perpendicular to the central axis. 12. The method of claim 1, wherein exposing a hydrocarbon feedstock to a first catalyst under first effective processing conditions comprises exposing the hydrocarbon feedstock to a hydrotreating catalyst under effective hydrotreating conditions, the hydrotreating catalyst comprising at least one Group VI metal and at least one Group VIII metal optionally on a support, the effective hydrotreating conditions including a temperature of about 200° C. to about 450° C.; a pressure of about 250 psig (1.8 MPa) to about 5000 psig (34.6 MPa); a Liquid Hourly Space Velocity (LHSV) of about 0.05 to about 10 h−1; and a hydrogen treat rate of about 200 scf/B (35.6 m3/m3) to about 10,000 scf/B (1781 m3/m3). 13. The method of claim 1, wherein exposing a hydrocarbon feedstock to a first catalyst under first effective processing conditions comprises exposing the hydrocarbon feedstock to a hydrocracking catalyst under effective hydrocracking conditions, the hydrocracking catalyst comprising at least one Group VI metal and at least one Group VIII metal on an acidic support, the effective hydrocracking conditions comprising a temperature of about 550° F. (288° C.) to about 840° F. (449° C.), hydrogen partial pressures of from about 250 psig to about 5000 psig (1.8 MPag to 34.6 MPag), liquid hourly space velocities of from 0.05 h−1 to 10 h−1, and hydrogen treat gas rates of from 35.6 m3/m3 to 1781 m3/m3 (200 SCF/B to 10,000 SCF/B). 14. The method of claim 1, wherein exposing a hydrocarbon feedstock to a first catalyst under first effective processing conditions comprises exposing the hydrocarbon feedstock to a dewaxing catalyst under effective catalytic dewaxing conditions, including a temperature of about 200° C. to about 450° C., a hydrogen partial pressure of about 1.8 to about 34.6 mPa (250 to 5000 psi), a liquid hourly space velocity of from about 0.2 hr−1 to about 10 hr−1, and a hydrogen circulation rate of from about 35.6 to about 1781 m3/m3 (200 to 10,000 scf/B). 15. The method of claim 1, further comprising: providing a second catalyst bed in the reactor, the second catalyst bed being at least partially supported by the inner conduit; andexposing an axial flow of at least a portion of the first liquid reaction effluent to a second catalyst located in the second catalyst bed in the presence of the reactive gas under second effective processing conditions to produce a second liquid reaction effluent,delivering at least a portion of the reactive gas flow into the second catalyst bed via the inner conduit as a radial flow, thereby contacting the second liquid reaction effluent and the second catalyst in the second catalyst bed under second effective processing conditions,wherein at least about 50 vol % of the reactive gas flow delivered to the second catalyst bed exits the second catalyst bed by passing into the outer gap, and at least 50 vol % of the second liquid reaction effluent exits the reactor via the reactor effluent outlet, wherein the at least 50 vol % of the first liquid reaction effluent is a component of the at least 50 vol % of the second liquid reaction effluent that exits the reactor via the reactor effluent outlet. 16. The method of claim 15, wherein at least a portion of the reactive gas flow delivered to the second catalyst bed is delivered as a radial gas flow. 17. The method of claim 16, wherein at least about 50% of the reactive gas flow delivered to the second catalyst bed exits the second catalyst bed by passing into an outer gap through a gas/liquid selective membrane structure that separates second catalyst in the second catalyst bed from the outer gap. 18. The method of claim 17, wherein the gas/liquid selective membrane structure is comprised of a gas permeable ceramic membrane. 19. The method of claim 17, wherein the gas/liquid selective membrane structure is comprised of a gas permeable metal membrane. 20. The method of claim 15, wherein the second catalyst is a hydrotreating catalyst and the first catalyst is a hydrocracking catalyst or a dewaxing catalyst. 21. The method of claim 15, wherein at least 90 vol % of the second liquid reaction effluent exits the reactor via the reactor effluent outlet. 22. The method of claim 21, wherein substantially all of the second liquid reaction effluent exits the reactor via the reactor effluent outlet. 23. The method of claim 15, wherein passing at least about 50 vol % of the reactive gas flow into the inner conduit comprises passing the at least about 50 vol % of the reactive gas flow through a gas/liquid selective membrane structure that separates the first catalyst in the first catalyst bed from the inner conduit. 24. The method of claim 23, wherein the gas/liquid selective membrane is a gas permeable ceramic membrane. 25. The method of claim 23, wherein the gas/liquid selective membrane is a gas permeable metal membrane. 26. The method of claim 15, wherein at least 90 vol % of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 27. The method of claim 26, wherein substantially all of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 28. A method for performing a catalyzed gas-liquid reaction, comprising: providing a first catalyst bed in a reactor, the reactor including an inner conduit that occupies a portion of the volume of the catalyst bed and an outer gap between the first catalyst bed and a wall of the reactor, wherein the reactor further comprises a reactor effluent outlet which is fluidly connected to the first catalyst bed;exposing an axial flow of a hydrocarbon feedstock to a first catalyst located in the first catalyst bed under first effective processing conditions to produce a first liquid reaction effluent; anddelivering at least a portion of a reactive gas flow into the first catalyst bed via the outer gap as a radial flow and at least a portion of the reactive gas flows directly into the catalyst bed in a co-current manner with the feedstock, thereby contacting for the hydrocarbon feedstock and the first catalyst in the first catalyst bed under first effective processing conditions;wherein at least about 50 vol % of the reactive gas flow exits the first catalyst bed by passing into the inner conduit, and at least 50 vol % of the first liquid reaction effluent exits the reactor via the reactor effluent outlet. 29. The method of claim 28, wherein the first effective processing conditions comprise effective hydroprocessing conditions and the reactive gas comprises hydrogen. 30. The method of claim 28, wherein the reactive gas comprises at least about 80 mol % hydrogen. 31. The method of claim 28, wherein at least about 25 vol % of the reactive gas flow is delivered into the first catalyst bed as a radial gas flow.
Unmuth Eugene E. (Naperville IL) Mahoney John A. (Glen Ellyn IL) Bertolacini Ralph J. (Naperville IL), Process for the manufacture of lubricating oils.
Smolarek James ; Leavitt Frederick Wells ; Nowobilski Jeffert John ; Bergsten Victor Emmanuel ; Fassbaugh John Harry, Radial bed vaccum/pressure swing adsorber vessel.
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