CN1258558A - Radial gas-solid reactor - Google Patents
Radial gas-solid reactor Download PDFInfo
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- CN1258558A CN1258558A CN 99104594 CN99104594A CN1258558A CN 1258558 A CN1258558 A CN 1258558A CN 99104594 CN99104594 CN 99104594 CN 99104594 A CN99104594 A CN 99104594A CN 1258558 A CN1258558 A CN 1258558A
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Abstract
The present invention relates to one radial gas-solid reactor used in moving bed and fixed bed for petroleum processing and aims at solving the problem of inhomogeneous distribution of gas phase reactant in cactalyst bed. The present invention has a reactant entrance on the side of reactor casing and at the height of half the vertical height of outer net in the catalytic reaction area, and a baffle plate between the outer net and the reactant entrance to prevent the reactant from scouring the outer net of catalyst bed directly. The present invention has small static pressure drop of gas phase reactant in distribution channel and homogeneous distribution of gas phase reactant in catalyst bed.
Description
The present invention relates to a kind of fixed bed or moving bed gas-solid reaction equipment, relate in particular to a kind of fixed bed or gas and solid radial reactor for moving-bed that is used for petroleum refining process.
Gas-solid radial reactor is a kind of reactor efficiently, and its application in petroleum refining process is very extensive, generally adopts two kinds of forms of fixed bed and moving bed.But existing fixed bed and moving bed radial reactor, vapor-phase reactant generally enter the reactant distribution passage from the bed top and distribute, and then radially enter beds.In this process, exist vapor-phase reactant and distribute uneven problem.
A kind of moving bed radial reactor of the said firm has been introduced by UOP in a U.S. Pat 4141690 of its application.This reactor, vapor-phase reactant enters reactor from the reactant entrance on reactor top, flows into downwards then and distributes passage.In distributing passage, vapor-phase reactant radially sees through beds along the different axial heights of beds, reacts with catalyst.Product enters center cavity, discharges from reacting product outlet.
In above process, the pressure drop of gas (vapor-phase reactant and gas-phase reaction product) from reactant entrance to reacting product outlet is called total reactor pressure falls, and the pressure drop that gas produces in distributing passage and center cavity is called differential static pressure.When vapor-phase reactant radially sees through beds, be called vapor-phase reactant distributed uniform degree along the ratio of the minimum of a value of the flow on the unit lateral area of the different axial heights of beds and maximum.Obviously, vapor-phase reactant distributed uniform degree is big more, and then vapor-phase reactant is radially even more through beds along the different axial heights of beds, and the utilization rate of catalyst is high more.Relevant studies show that, differential static pressure proportion in overall presure drop is more little, and then vapor-phase reactant distributed uniform degree is high more.U.S. Pat 4141690 described reactors, for the reactor of high throughput, its ratio of height to diameter is bigger, vapor-phase reactant enters before the beds and to distribute in the passage and product goes out bed to enter the differential static pressure that is produced in center cavity after the perforate central tube bigger in annular, thereby the distributed uniform degree of vapor-phase reactant is reduced.
Also there is similar problem in existing fixed bed gas-solid radial reactor.
Obviously, the distributed uniform degree that improve vapor-phase reactant has only two approach: the first improves total reactor pressure falls, and it is two for reducing differential static pressure.The former can only implement under the condition that allows, in order to avoid increase operating cost.The present invention by reducing the differential static pressure of vapor-phase reactant in distributing passage, improves the distributed uniform degree of vapor-phase reactant from the second approach.
The object of the present invention is to provide little, the gas-solid radial reactor that can uniform distribution in beds of the differential static pressure of a kind of vapor-phase reactant in distributing passage.
For achieving the above object, the technical solution used in the present invention is: a kind of gas-solid radial reactor that is used for petroleum refining process, comprise the catalytic reaction zone in a cylindrical shell and the housing, housing is provided with reactant entrance, reacting product outlet, catalyst inlet, the catalyst discharge port, catalytic reaction zone comprises with the housing coaxial arrangement, Intranet that is arranged in order from inside to outside and outer net, it is characterized in that: reactant entrance is positioned at the side of housing, the vertical height at reactant entrance center is positioned at the middle part of outer net axial height, is provided with baffle plate between reactant entrance and the outer net.
By technical solution of the present invention as can be seen, the present invention improves existing gas-solid radial reactor, the inlet of vapor-phase reactant is opened in the reactor enclosure body side surface, and made the middle part that is centered close to the outer net axial height of reactant entrance.Reactant enters the distribution passage between outer net and the housing from the middle part, enter after distributing and see through beds, reacts with catalyst.For preventing that vapor-phase reactant from directly washing away the beds outer net, at outer net and reactant entrance place one baffle plate is set, this also helps the distribution of vapor-phase reactant.Compared with prior art, the distance of the vapor-phase reactant of gas-solid radial reactor of the present invention from reactant entrance to beds outer net each point more becomes average, reduced the distance that vapor-phase reactant is advanced in distributing passage, thereby reduced the differential static pressure of vapor-phase reactant in distributing passage, improved the distributed uniform degree of vapor-phase reactant in beds.Vapor-phase reactant distributes evenly more in beds, and the reaction task that the catalyst in the beds is born is just average more, thereby can effectively utilize catalyst to greatest extent.
For for the fixed bed reactors of green coke reaction, the uniformity that vapor-phase reactant distributes in beds is high more, and coke distributes just evenly more on beds, thereby can prolong operation cycle.
The present invention can be widely used in the gas-solid reaction process in the PETROLEUM PROCESSING, is particularly useful for the naphtha catalytic reforming process.
The present invention is further detailed explanation below in conjunction with drawings and Examples.Accompanying drawing is only drawn for explanation the present invention, does not limit the present invention.
Fig. 1 is the structural representation that advances next-out moving bed radial reactor in a kind of of the present invention.
Fig. 2 is that the A-A of Fig. 1 is to cutaway view.
Fig. 3 is the structural representation that advances upper outlet type moving bed radial reactor in a kind of of the present invention.
Fig. 4 is the structural representation that advances next-out fixed bed radial reactor in a kind of of the present invention.
Fig. 5 is the structural representation that advances upper outlet type fixed bed radial reactor in a kind of of the present invention.
In of the present invention a kind of moving bed radial reactor shown in Figure 1, vapor-phase reactant enters reactor from the middle part, and the gas-phase reaction product is discharged from reactor lower part.
Reactor shown in Figure 1 comprises a cylindrical shell 1.Housing 1 top is catalyst buffering area 15, and the bottom is a catalytic reaction zone 20.Catalyst buffering area 15 is made of upper body 1 and the buffering area base plate 13 that is positioned at its underpart.Buffering area housing 1 top is provided with catalyst inlet 4.This figure is the situation that a catalyst inlet 4 is set, and certainly, can be provided with a plurality of as required.The central authorities of catalytic reaction zone 20 are provided with and housing cylindrical shape Intranet 71 coaxial arrangement, that be arranged in order from inside to outside and outer net 6.The pressure drop of crossing beds for conditioned reaction thing air communication is at the tube having holes 8 of the inside of Intranet 7 lining one with Intranet 7 coaxial arrangement.The center of tube having holes 8 is a center cavity 18.It is that pre-existing reactors is used always that tube having holes 8 is set.Certainly, when the beds pressure drop reaches enough big, also can not establish tube having holes 8.Form the reactant distribution passage 16 of annular between housing 1 and the outer net 6.The top of tube having holes 8, Intranet 7 and outer net 6 is provided with upper sealing panel 9, and the bottom is provided with bed base plate 10, and bed base plate 10 is bearing in the bottom of housing 1.Buffering area base plate 13 is provided with uniform catalyst transport 14, enters the top of annular region between Intranet 7 and the outer net 6 through upper sealing panel 9.The bed base plate 10 of tube having holes 8 bottoms is provided with gas-phase reaction product outlet 3, is stretched out by the bottom of housing 1.Reacting product outlet 3 can be provided with a plurality of, and this figure has only illustrated 1 the situation that is provided with.Bed base plate 10 between Intranet 7 and the outer net 6 is provided with catalyst discharge port 5.Reactant entrance 2 is positioned at the side of reaction zone housing 1, and the vertical height at its center is positioned at the middle part of outer net 6 axial heights.Reactant entrance 2 preferably faces the mid point (being 50% point of outer net 6 axial heights) of outer net 6 axial heights, certainly according to circumstances, can also move up or down vertically respectively from the height of outer net 6 mid points, but the distance that moves up or down preferably respectively is 20% of outer net 6 axial heights.Be provided with baffle plate 11 between reactant entrance 2 and the outer net 6, directly wash away beds outer net 6 to prevent reactant flow.The direction that baffle plate 11 can also change reactant flow simultaneously is set, helps vapor-phase reactant and enter distribution passage 16 with circumferencial direction vertically.Baffle plate 11 is watt shape cylinder shapes among Fig. 1, is fixed in (referring to Fig. 1 and Fig. 2) on the housing 1 by 4 steady arms 12.As for the size of baffle plate 11 areas and and housing 1 between distance, then be that the increase with the reactor for treatment amount increases.In general, baffle plate 11 areas are 1.1～10 times of reactant entrance 2 cross-sectional areas, are generally 4 times; Baffle plate 11 is 1/10～1/2 of reactant entrance 2 diameters apart from the distance of housing 1, is generally 1/4.Fig. 1, shown in Figure 2 watt of shape cylinder shape baffle plate 11 are not unique form of baffle plate 11 of the present invention, for example adopt circular flat board can yet.Baffle plate 11 fixedly be not limited to said method, can also baffle plate 11 be fixed on the housing 1 with other part and method commonly used.
The working condition of reactor shown in Figure 1 is such:
Catalyst enters the catalyst buffering area 15 of reactor from catalyst inlet 4, again by the annular region of catalyst buffering area 15 between catalyst transport uniform on the buffering area base plate 13 14 inflow Intranets 7 and outer net 6, move down vertically, and discharge by the catalyst discharge port 5 of bottom, form the beds 17 (seeing Fig. 1, Fig. 2) that moves.
Vapor-phase reactant enters reactor from reactant entrance 2, after baffle plate 11 changes direction, enter vapor-phase reactant with circumferencial direction vertically and distribute passage 16, radially see through beds 17 after the distribution, contact with the catalyst that axially moves down at this, react.The gas-phase reaction product converges at center cavity 18, discharges from reactor lower part through reacting product outlet 3.Upper sealing panel 9 can prevent that vapor-phase reactant from directly entering center cavity 18 from reactant distribution passage 16.
In the of the present invention another kind of moving bed radial reactor shown in Figure 3, vapor-phase reactant enters reactor from the middle part, and the gas-phase reaction product is discharged from reactor top.Only be with the difference of reactor shown in Figure 1: the reacting product outlet 3 of reactor shown in Figure 3 is positioned at the top of housing 1.Be provided with a product conduit 19 between reacting product outlet 3 and the center cavity 18, one end of this conduit is communicated with center cavity 18 through upper sealing panel 9, an other end links to each other with the reacting product outlet 3 on housing top, and the gas-phase reaction product of center cavity 18 is upwards discharged through reacting product outlet 3 through product conduit 19.
Figure 4 shows that a kind of fixed bed radial reactor of the present invention.Vapor-phase reactant enters reactor from the reactor middle part, and the gas-phase reaction product is discharged from reactor lower part.Compare with moving bed radial reactor shown in Figure 1, fixed bed reactors are not provided with the catalyst buffering area, and catalyst inlet 4 is used for loading catalyst before going into operation.This reactor comprises a cylindrical shell 1, and housing 1 top is provided with catalyst inlet 4, and the bottom is provided with reacting product outlet 3 and catalyst discharge port 5.In the housing 1 is catalytic reaction zone 20, and the layout of baffle plate 11 and moving bed radial reactor shown in Figure 1 are identical between the layout of tube having holes 8 wherein, Intranet 7, outer net 6 and reactant entrance 2 and reactant entrance 2 and the outer net 6.
The working condition of reactor shown in Figure 4 is such:
Before going into operation with catalyst from catalyst inlet 4 pack into Intranet 7 in the housing 1 and the annular region between the outer net 6, form fixed beds layer 17.Catalyst in the operating process in the beds 17 does not move.Vapor-phase reactant enters reactor from reactant entrance 2, after baffle plate 11 changes direction, enters gas distribution channel 16 with circumferencial direction vertically, radially sees through fixed beds layer 17 after the distribution, contacts with catalyst at this, reacts.The gas-phase reaction product converges at center cavity 18, discharges from reactor lower part through reacting product outlet 3.
Fig. 5 is the structural representation of another fixed bed radial reactor of the present invention.Vapor-phase reactant enters reactor from the middle part, and the gas-phase reaction product is discharged from reactor top.The difference of Fig. 5 and fixed bed reactors shown in Figure 4 only is: the reacting product outlet 3 of reactor shown in Figure 5 is positioned at the top of housing 1, be provided with a product conduit 19 between reacting product outlet 3 and the center cavity 18, one end of this conduit is communicated with center cavity 18 through upper sealing panel 9, an other end links to each other with the reacting product outlet 3 on housing top, and the gas-phase reaction product in the center cavity 18 is upwards discharged through reacting product outlet 3 through product conduit 19.
Claims (6)
1, a kind of gas-solid radial reactor that is used for petroleum refining process, comprise the catalytic reaction zone (20) in a cylindrical shell (1) and the housing (1), housing (1) is provided with reactant entrance (2), reacting product outlet (3), catalyst inlet (4), catalyst discharge port (5), catalytic reaction zone (20) comprises with housing (1) coaxial arrangement, Intranet that is arranged in order from inside to outside (7) and outer net (6), it is characterized in that: reactant entrance (2) is positioned at the side of housing (1), the vertical height at reactant entrance (2) center is positioned at the middle part of outer net (6) axial height, is provided with baffle plate (11) between reactant entrance (2) and the outer net (6).
2, radial reactor according to claim 1 is characterized in that: the inside of Intranet (7) is provided with the tube having holes (8) with Intranet (7) coaxial arrangement.
3, radial reactor according to claim 1 and 2 is characterized in that: 50% of being positioned at outer net (6) axial height of the vertical height at reactant entrance (2) center is the scope of the outer net height 40% of mid point.
4, radial reactor according to claim 1 and 2 is characterized in that: baffle plate (11) is a watt shape cylinder shape, and its convex surface points to housing (1).
5, radial reactor according to claim 1 and 2 is characterized in that: baffle plate (11) is for circular dull and stereotyped.
6, radial reactor according to claim 1 and 2 is characterized in that: be provided with steady arm (12) between baffle plate (11) and the housing (1), steady arm (12) is fixed in baffle plate on the housing (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99104594A CN1100599C (en) | 1999-05-10 | 1999-05-10 | Radial gas-solid reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99104594A CN1100599C (en) | 1999-05-10 | 1999-05-10 | Radial gas-solid reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1258558A true CN1258558A (en) | 2000-07-05 |
| CN1100599C CN1100599C (en) | 2003-02-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN99104594A Expired - Lifetime CN1100599C (en) | 1999-05-10 | 1999-05-10 | Radial gas-solid reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101658799B (en) * | 2009-09-14 | 2011-06-29 | 洛阳瑞泽石化工程有限公司 | Continuous catalyst regeneration method and device thereof |
| CN103846061A (en) * | 2013-10-22 | 2014-06-11 | 洛阳智达石化工程有限公司 | Novel multi-bed radial fixed bed reactor |
| CN103805234B (en) * | 2012-11-07 | 2015-09-02 | 中国石油化工股份有限公司 | A kind of radial-flow type residual hydrocracking reactor |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101172922B (en) * | 2006-11-02 | 2010-05-12 | 中国石油化工股份有限公司 | Method for producing propylene with C_4 alkene catalytic pyrolysis |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4141690A (en) * | 1977-08-05 | 1979-02-27 | Uop Inc. | Catalytic reaction chamber for gravity-flowing catalyst particles |
| CN2131600Y (en) * | 1992-06-18 | 1993-05-05 | 中国石油化工总公司 | Low-resistance flow distributor of reactor of ridially fixed bed |
-
1999
- 1999-05-10 CN CN99104594A patent/CN1100599C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101658799B (en) * | 2009-09-14 | 2011-06-29 | 洛阳瑞泽石化工程有限公司 | Continuous catalyst regeneration method and device thereof |
| CN103805234B (en) * | 2012-11-07 | 2015-09-02 | 中国石油化工股份有限公司 | A kind of radial-flow type residual hydrocracking reactor |
| CN103846061A (en) * | 2013-10-22 | 2014-06-11 | 洛阳智达石化工程有限公司 | Novel multi-bed radial fixed bed reactor |
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| Publication number | Publication date |
|---|---|
| CN1100599C (en) | 2003-02-05 |
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Owner name: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORAT Free format text: FORMER NAME: CHINA PETROCHEMICAL CORPORATION |
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| CP01 | Change in the name or title of a patent holder |
Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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Granted publication date: 20030205 |