CN1333084A - Gas and solid radial reactor for moving-bed - Google Patents
Gas and solid radial reactor for moving-bed Download PDFInfo
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- CN1333084A CN1333084A CN 01128724 CN01128724A CN1333084A CN 1333084 A CN1333084 A CN 1333084A CN 01128724 CN01128724 CN 01128724 CN 01128724 A CN01128724 A CN 01128724A CN 1333084 A CN1333084 A CN 1333084A
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- skirt
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- catalyst
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- 239000007787 solid Substances 0.000 title claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 83
- 210000001364 upper extremity Anatomy 0.000 claims description 9
- 239000000376 reactant Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 3
- 229930195733 hydrocarbon Natural products 0.000 abstract description 3
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 3
- 239000003208 petroleum Substances 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- 239000008187 granular material Substances 0.000 description 15
- 239000012808 vapor phase Substances 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 238000001833 catalytic reforming Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000001788 irregular Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000000994 depressogenic effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000005504 petroleum refining Methods 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 229910000679 solder Inorganic materials 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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Abstract
The present invention discloses a gas-solid radial reactor of moving bed for chemical industry and petroleum processing industry, and is characterized by that the lower portion of inner not of said reactor is equipped with a skirt, and the external surface of said skirt is inclined from top to bottom along the direction from inner net toward outer net, its upper edge is connected with inner net, and its lower edge is connected with internal surface of closure head of the bottom, and the radial position of the lower edge is positioned in internal side of radial position of catalyst outlet pipe, and the external surface of said skirt is generally made into circular truncated cone side face or frustum side face. Said invention can effectively reduce or eliminate flow dead zone of catalyst in the reactor, at the same time the structure of said skirt is simple, and easy to implement. It is specially applicable to hydrocarbon conversion reaction and catforming reaction.
Description
(1) technical field
The present invention relates to a kind of gas and solid radial reactor for moving-bed, relate in particular to the gas and solid radial reactor for moving-bed that is used for the petroleum refining catalytic reforming reaction.
(2) background technology
In gas and solid radial reactor for moving-bed, vapor-phase reactant reacts under a solid catalyst condition that material exists.Described catalyst moves axially along reactor, vapor-phase reactant along reactor radially or near radially passing through beds.Traditional gas and solid radial reactor for moving-bed generally is the outside wall (housing) that is made of reactor top end socket, cylindrical side wall and bottom bulkhead, one annular space by cylindrical outer net (or one group of fan-shaped bucket gas distributor that has aperture along the outside wall axially-aligned of reactor) and cylindrical Intranet formation is arranged in described reactor, promptly form columnar beds behind the catalyst of packing into.Described reactor bottom end socket inner surface is the end of beds.Described cylindrical Intranet can stop catalyst granules to enter the inner space of Intranet, and it can be used as discharge, collecting reaction product simultaneously.Described cylindrical outer net can stop catalyst granules to enter space outerpace between outer net and the housing, and it can be used as gas distributor simultaneously, and vapor-phase reactant is assigned to described beds as far as possible equably.Flow through cylindrical outer net, beds and cylindrical Intranet of this vapor-phase reactant comes together in the gas flow pattern of discharge, be called outer advance in go out formula; Otherwise,, then be called the formula of withing too many people coming in and going out if gas flow direction is opposite with the above-mentioned gas flow direction.Reactor also is provided with vapor-phase reactant inlet and reacting product outlet.For outward advance in go out for the formula reactor, they communicate with above-mentioned gas distributor (being outer net) and discharge respectively; For the formula reactor of withing too many people coming in and going out, reactor inlet communicates with above-mentioned discharge, and reactor outlet communicates with gas distributor (being outer net).Be provided with many catalyst ingress pipes in reactor head and catalyst imported beds between Intranet and the outer net, be provided with many catalyst discharge pipes in the beds bottom catalyst is discharged.
If through all discharging after the mean residence time, this is optimal to catalyst granules in reactor.But catalyst granules passes through after the mean residence time in above-mentioned traditional reactor, always there is the part catalyst not discharge on time, shifts to an earlier date or postponement, even have the small part catalyst to rest on reactor always, can not discharge forever, form catalyst and move the dead band.The existence that above-mentioned catalyst moves the dead band is disadvantageous to reaction; Particularly for hydrocarbon conversion reaction (for example catalytic reforming reaction), especially unfavorable.Because produce coke in the course of reaction, these coke can make catalyst lose activity gradually, are invalid to reacting.More disadvantageously, above-mentioned catalyst moves the dead band and As time goes on also can grow up gradually, moves thereby further influence catalyst, until causing improper parking, shortens the device on-stream time.
Certainly, if change the structure and the shape of reactor bottom end socket, the angle with horizontal plane is enough big everywhere to make the enough smooth and inner surface of its inner surface, so that catalyst granules stops on the surface, so also can reduce or eliminate the catalyst dead band of flowing within it.But this can make the axial height of reactor increase greatly; Particularly for the bigger reactor of diameter, especially true.
A patent application of Compagnie Francise des Petroles (publication number CN 1137942A) describes a kind of reactor that catalyst granules is discharged from reactor bottom that helps in detail.Its basic point of departure is, for above-mentioned outer advance in go out for the radial reactor of formula, reactor bottom catalyst outlet is as far as possible near central tube (Intranet), extend one group of pleat of forming by continuous rise and depressed part branch from outlet to bed lateral surface (outer net), for the catalyst of bed bottom provides more the contact-making surface of " suddenly ", thereby reduce or the mobile dead band of elimination reactor bottom catalyst.But the pleat structure of being made up of described continuous rise and depressed part branch in this reactor is too complicated, and the engineering construction difficulty is big.
(3) summary of the invention
Technical problem to be solved by this invention is: reduce the above-mentioned structural complexity that helps the parts that catalyst granules discharges from reactor bottom, and the big problem of engineering construction difficulty that produces because of its complex structure.
For addressing the above problem, the technical solution used in the present invention is: a kind of gas and solid radial reactor for moving-bed, comprise a housing, housing is by cylinder side wall, top end socket and bottom bulkhead are formed, be provided with in the housing along housing shaft to Intranet and the outer net arranged successively from inside to outside, form annular space between Intranet and the outer net, housing is provided with reactant entrance, reacting product outlet, the top end socket is provided with the catalyst ingress pipe, bottom bulkhead is provided with the catalyst discharge pipe, the catalyst ingress pipe links to each other with annular space respectively with the catalyst discharge pipe, the catalyst discharge pipe forms opening on the inner surface of bottom bulkhead, it is characterized in that: the bottom in Intranet is provided with skirt, the outer surface of skirt is from top to bottom along being tilted by the direction of Intranet to outer net, its upper limb links to each other with Intranet, and lower edge links to each other with the inner surface of bottom bulkhead, and the radial position of lower edge is positioned at the inboard of the radial position of described catalyst discharge pipe.
Adopt the present invention, have following beneficial effect:, help catalyst granules along the downward landing of the inclined surface of skirt owing to increased skirt in the bottom of cylindrical Intranet.Skirt generally constitutes (for example frustum cone side or frustum side) by simple face, makes the relatively simple for structure of skirt itself, thereby is easy to manufacture and assemble.In addition, the upper limb of skirt and lower edge are easy to be processed into suitable shape, can link with Intranet and bottom bulkhead respectively at an easy rate.Adopt the present invention, can reduce or eliminate the catalytic amount of catalyst discharge pipe radial position not move on the interior bottom bulkhead inner surface.In addition, in terms of existing technologies, catalyst discharge pipe of the present invention moves to outer net in radial position, can reduce or eliminate the catalytic amount that does not move on the catalyst discharge pipe radial position bottom bulkhead inner surface in addition.Therefore, behind the increase skirt, can eliminate the flow dead of catalyst basically fully.
In a word, the present invention adopts simple skirt structure can eliminate the flow dead of catalyst in reactor, and easy to implement on engineering.
The present invention is further detailed explanation below in conjunction with drawings and Examples.
(4) description of drawings
Fig. 1 is the axial cutaway view that has the gas and solid radial reactor for moving-bed of frustum cone side skirt.
Fig. 2 is the bottom plan view (being that A-A is to cutaway view) of reactor shown in Figure 1.
Fig. 3 is the bottom plan view that has the reactor of toroidal catalyst discharge pipe.
Fig. 4 is the bottom plan view that has the reactor of frustum side skirt.
Fig. 5 is the schematic perspective view of frustum cone side skirt.
Fig. 6 is the schematic perspective view of a kind of frustum side skirt.
Fig. 7 is the schematic perspective view of another frustum side skirt.
(5) specific embodiment
Gas and solid radial reactor for moving-bed as depicted in figs. 1 and 2 comprises a housing, and housing is by circle Cylindrical sidewall 11, top end socket 10 and bottom bulkhead 12 form. Be provided with in the housing along housing shaft to by Interior Intranet 14 and the outer net 13 of outwards arranging successively forms annular space between Intranet 14 and the outer net 13 16, annular space 16 is packed into and is namely formed the cylinder catalyst bed behind the catalyst. Housing top end socket 10 Be provided with reactant entrance 1, bottom bulkhead 12 is provided with reacting product outlet 3. In reactor head The compartment of terrain is provided with many (more than one) catalyst ingress pipes 2 on the top end socket 10, is used for catalysis Agent imports annular space 16. The compartment of terrain is provided with many (more than one) sections for round on the bottom bulkhead 12 The catalyst discharge pipe 4 of shape is used for catalyst is derived from annular space 16. Every catalyst is discharged Pipe 4 is the conglobate opening 5 of shape (referring to Fig. 2) on the inner surface of bottom bulkhead 12 respectively.
The bottom of Intranet 14 is provided with skirt 15, and its outer surface is frustum cone side, referring to Fig. 5 stereogram. The outer surface of skirt 15 is from top to bottom along tilted its upper limb 7 and Intranet 14 by the direction of Intranet to outer net Link to each other, lower edge 8 links to each other with the inner surface of bottom bulkhead 12. Upper limb 7 can be adopted with the binding of Intranet 14 Use welding manner, but should weld grinding is smooth; Lower edge 8 can with the binding of bottom bulkhead 12 inner surfaces With methods such as employing spot welding. The radial position of lower edge 8 is positioned at the radial position of above-mentioned catalyst discharge pipe 4 The inboard (that is be positioned at the circular open 5 of catalyst discharge pipe 4 on bottom bulkhead 12 inner surfaces The inboard is referring to Fig. 2), and with the radial distance of catalyst discharge pipe 4 should be as best one can little. Skirt 15 Upper limb 7 should be connected with the bottom of cylindrical Intranet 14 as far as possible smoothly, with what reduce catalyst moving Adverse effect. If the following Intranet in upper limb 7 and Intranet 14 junctions is aperture area not, then skirt 15 Lower edge 8 and the inner surface of bottom bulkhead 12 between should leave certain gap so that skirt is inner empty Between gas in 17 can overflow. This gap should less than the diameter of catalyst granules, make catalyst granules Can not enter skirt inner space 17. In the specification of the present invention, described " radial position ", " distance radially From " all refer to projected position and projector distance on the reactor shell diametric(al).
The outer surface of skirt 15 can also adopt the frustum side. Each face of frustum side is roughly the plane Trapezoidal, its stereogram is referring to Fig. 6, Fig. 7. When adopting frustum side skirt, the upper end of frustum side can Link with Intranet 14 progressively to be transited into concordant rounded upper edge 7 (as shown in Figure 6). Perhaps, cone The upper end of platform side also can not transition, and take advantage of a situation and extend until join with above-mentioned cylindrical Intranet 14, This moment, upper limb 7 was not concordant, as shown in Figure 7. Fig. 4 shows the reaction with frustum side skirt The bottom plan view of device. Reference numeral among Fig. 4 is identical with Fig. 1, Fig. 2.
On the engineering, reactor bottom end socket 12 general sphere or the elliposoidals of adopting. Frustum cone side or frustum The lower edge 8 of side skirt should be processed into the shape suitable with bottom bulkhead 12 curved surfaces, to seal with the bottom 12 link. Obviously, the upper limb of the skirt of frustum cone side or frustum side and lower edge form required form Process all be fairly simple, also be to be easy to realize with the binding of Intranet 14 and bottom bulkhead 12 .
Below only describe the present invention as an example of the skirt of frustum cone side or frustum side example, but this also Do not limit scope of the present invention. The outer surface of skirt 15 can also be by frustum cone side or frustum side To irregular curved surface outwardly or that concave and then form, or combined by the face of other shape Face. Skirt 15 can be integral form, also can be by symmetrical or asymmetric multi-disc parts splicing Form. Skirt 15 can be installed in the reactor with integral way, also can be with skirt 15 at reactor Be divided into polylith outward, in reactor, assemble. Those skilled in the art is as long as carry according to the present invention The thinking of confession arranges skirt that outer surface tilts and is beneficial to catalyst in the bottom of cylindrical Intranet 14 Landing all can reach purpose of the present invention. For the purpose of the present invention, the skirt outer surface adopts frustum cone side to be Best.
The lateral surface of described skirt 15 should be as far as possible smooth, and ensure certain steepness, so that catalysis The agent particle can not be stagnated on the lateral surface of skirt as far as possible. Define below steepness: if described skirt 15 Be frustum cone side, then described round platform base angle angle [alpha] is steepness (referring to Fig. 5); If described skirt 15 Be the frustum side, then the side of described frustum (planar trapezoidal) is steepness with the angle of horizontal plane; If described skirt 15 consists of by other irregular, then the tangent plane of each irregular upper any point with The reckling of the angle of horizontal plane is steepness. The present invention, described steepness is generally spent to 80 30 Between the degree, decide according to the mobile performance of catalyst granules. The mobile performance of catalyst granules is more good, then institute Stating steepness can be more little; And the mobile performance of catalyst granules is more poor, and then required steepness is more big. Guaranteeing catalyst granules under the prerequisite of not stagnating on the lateral surface of skirt 15, described steepness should be use up Amount ground is little; Because increase extraly the effective area that steepness can reduce cylindrical Intranet 14, or do not have Effect ground improves the height of reactor. For the moving-bed reforming catalyst, described steepness general desirable 60 Degree.
The present invention, the radial position of catalyst discharge pipe 4 be generally at the middle part of beds radial position, Or more be partial to cylindrical outer net 13. Referring to Fig. 1 and Fig. 2, the axial line of every catalyst discharge pipe 4 601 are about 0.5t with the radial distance c of cylindrical Intranet 14 in the radial position of bottom bulkhead 12, T is the width of annular space 16, i.e. the external diameter of the internal diameter of cylindrical outer net 13 and cylindrical Intranet 14 Half (thickness that is equivalent to beds) of difference. Obviously, above-mentioned distance too hour, with unfavorable Immobilising on the bottom bulkhead inner surface that reduces or eliminates beyond 4 radial positions of catalyst discharge pipe Catalytic amount. So in possible situation, above-mentioned distance had better not be less than 0.3t. But above-mentioned When distance is too big, can increase the height of skirt, reduce the effective area of cylindrical Intranet 14. So combine Close consideration, above-mentioned distance generally is preferably between 0.4t～0.6t, is preferably 0.5t.
Many catalyst discharge pipes 4 are uniform on the circumferential position around the skirt lower edge. Obviously, catalysis Agent discharge pipe 4 circumferential distance each other is more little, then the circumferencial direction between the two catalyst discharge pipes 4 The catalyst granules of upper stagnation is more few. So increasing the number of catalyst discharge pipe 4 moves reducing catalyst Moving dead band is favourable. Particularly the number when catalyst discharge pipe 4 increases to the limit---catalyst row When going out pipe and being linked to be an annular discharge pipe, the catalyst in the radial position of catalyst discharge pipe 4 flows The dead band will be eliminated fully. Referring to Fig. 3, catalyst discharge pipe 4 for the coaxial section of housing be annular Pipe, its opening 5 on bottom bulkhead 12 is annular, around skirt 15 lower edges 8 continuously Distribute. Two parts gusset 9 solder joint that bottom bulkhead 12 is disconnected by annular opening 5. Annulus The center line 602 of the annular opening 5 of shape catalyst discharge pipe 4 on bottom bulkhead 12 is apart from Intranet 14 Radial distance generally between 0.4t～0.6t, be preferably 0.5t; T is the width of annular space 16.
The present invention is specially adapted to hydrocarbon conversion reaction, is particularly useful for moving of petroleum refining catalytic reforming reaction The movable bed gas-solid radial reactor.
Claims (10)
1, a kind of gas and solid radial reactor for moving-bed, comprise a housing, housing is by cylinder side wall (11), top end socket (10) and bottom bulkhead (12) are formed, be provided with in the housing along housing shaft to Intranet (14) and the outer net (13) arranged successively from inside to outside, form annular space (16) between Intranet (14) and the outer net (13), housing is provided with reactant entrance (1), reacting product outlet (3), top end socket (10) is provided with catalyst ingress pipe (2), bottom bulkhead (12) is provided with catalyst discharge pipe (4), catalyst ingress pipe (2) links to each other with annular space (16) respectively with catalyst discharge pipe (4), catalyst discharge pipe (4) forms opening (5) on the inner surface of bottom bulkhead (12), it is characterized in that: be provided with skirt (15) in the bottom of Intranet (14), the outer surface of skirt (15) is from top to bottom along being tilted by the direction of Intranet (14) to outer net (13), its upper limb (7) links to each other with Intranet (14), lower edge (8) links to each other with the inner surface of bottom bulkhead (12), and the radial position of lower edge (8) is positioned at the inboard of the radial position of described catalyst discharge pipe (4).
2, gas and solid radial reactor for moving-bed according to claim 1 is characterized in that: the outer surface of described skirt (15) is frustum cone side or frustum side.
3, gas and solid radial reactor for moving-bed according to claim 2 is characterized in that: the round platform base angle angle of described frustum cone side or the angle of described frustum side and horizontal plane are 30 to 80 degree.
4, gas and solid radial reactor for moving-bed according to claim 3 is characterized in that: the round platform base angle angle of described frustum cone side or the angle of described frustum side and horizontal plane are 60 degree.
5, according to each described gas and solid radial reactor for moving-bed of claim 1 to 4, it is characterized in that: described catalyst discharge pipe (4) is circular pipe for the above section that the spaced around around the lower edge (8) of skirt (15) distributes.
6, gas and solid radial reactor for moving-bed according to claim 5 is characterized in that: the axial line (601) of every catalyst discharge pipe (4) is 0.4 times to 0.6 times of annular space (16) width apart from the radial distance of Intranet (14).
7, gas and solid radial reactor for moving-bed according to claim 6 is characterized in that: the axial line (601) of every catalyst discharge pipe (4) is 0.5 times of annular space (16) width apart from the radial distance of Intranet (14).
8, according to each described gas and solid radial reactor for moving-bed of claim 1 to 4, it is characterized in that: described catalyst discharge pipe (4) for the coaxial section of housing be the pipe of annular, its opening (5) on bottom bulkhead (12) inner surface is an annular, continuous distributed around the lower edge (8) of skirt (15).
9, gas and solid radial reactor for moving-bed according to claim 8 is characterized in that: the center line (602) of the annular opening (5) of described catalyst discharge pipe (4) on bottom bulkhead (12) inner surface is 0.4 times to 0.6 times of annular space (16) width apart from the radial distance of Intranet (14).
10, gas and solid radial reactor for moving-bed according to claim 9 is characterized in that: the center line (602) of the annular opening (5) of described catalyst discharge pipe (4) on bottom bulkhead (12) inner surface is 0.5 times of annular space (16) width apart from the radial distance of Intranet (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011287241A CN1140331C (en) | 2001-07-14 | 2001-07-14 | Gas and solid radial reactor for moving-bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011287241A CN1140331C (en) | 2001-07-14 | 2001-07-14 | Gas and solid radial reactor for moving-bed |
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| CN1333084A true CN1333084A (en) | 2002-01-30 |
| CN1140331C CN1140331C (en) | 2004-03-03 |
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| CNB011287241A Expired - Lifetime CN1140331C (en) | 2001-07-14 | 2001-07-14 | Gas and solid radial reactor for moving-bed |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2246320A1 (en) | 2009-04-29 | 2010-11-03 | Bayer MaterialScience AG | Process for the preparation of aromatic amines |
| CN102350273A (en) * | 2011-07-13 | 2012-02-15 | 迈瑞尔实验设备（上海）有限公司 | Cold molding apparatus for radial rector of moving bed |
| CN103084122A (en) * | 2011-10-31 | 2013-05-08 | 中国石油化工集团公司 | Radial reactor |
| CN103506054A (en) * | 2012-06-21 | 2014-01-15 | 中国石油化工集团公司 | Continuous reforming reactor material sealing apparatus with material discharge hopper, and method |
| CN103506055A (en) * | 2012-06-21 | 2014-01-15 | 中国石油化工集团公司 | Device and method for sealing reactants of continuous reforming reactor of countercurrent moving bed |
| CN109092213A (en) * | 2017-06-21 | 2018-12-28 | 阿克森斯公司 | The fixed bed or moving-burden bed reactor of the Radial Flow of the pending process stream of tool comprising improved inside |
| CN109651036A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | A method of by preparing low-carbon olefin |
| CN111099720A (en) * | 2018-10-26 | 2020-05-05 | 中国石油化工股份有限公司 | Sewage biological treatment reactor and treatment method thereof |
| CN113663607A (en) * | 2021-09-14 | 2021-11-19 | 中国石油大学(北京) | Downer reactor and method of operating same |
| CN114286853A (en) * | 2019-08-26 | 2022-04-05 | 环球油品有限责任公司 | Device for catalytic reforming of hydrocarbons with flow distributor and method for reforming of hydrocarbons |
| CN114425278A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for producing low-carbon olefin and application |
| WO2023231210A1 (en) * | 2022-05-13 | 2023-12-07 | 中国化学工程第三建设有限公司 | Uop propane dehydrogenation reactor device and maintenance method therefor |
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2001
- 2001-07-14 CN CNB011287241A patent/CN1140331C/en not_active Expired - Lifetime
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009019436A1 (en) | 2009-04-29 | 2010-11-04 | Bayer Materialscience Ag | Process for the preparation of aromatic amines |
| EP2246320A1 (en) | 2009-04-29 | 2010-11-03 | Bayer MaterialScience AG | Process for the preparation of aromatic amines |
| CN102350273A (en) * | 2011-07-13 | 2012-02-15 | 迈瑞尔实验设备（上海）有限公司 | Cold molding apparatus for radial rector of moving bed |
| CN103084122B (en) * | 2011-10-31 | 2016-05-04 | 中国石油化工集团公司 | Radial reactor |
| CN103084122A (en) * | 2011-10-31 | 2013-05-08 | 中国石油化工集团公司 | Radial reactor |
| CN103506054A (en) * | 2012-06-21 | 2014-01-15 | 中国石油化工集团公司 | Continuous reforming reactor material sealing apparatus with material discharge hopper, and method |
| CN103506054B (en) * | 2012-06-21 | 2015-10-28 | 中国石油化工集团公司 | A kind of continuous reforming reactor material sealing device with hopper and method |
| CN103506055A (en) * | 2012-06-21 | 2014-01-15 | 中国石油化工集团公司 | Device and method for sealing reactants of continuous reforming reactor of countercurrent moving bed |
| CN103506055B (en) * | 2012-06-21 | 2015-08-12 | 中国石油化工集团公司 | A kind of counter-flow moving bed continuous reforming reactor reaction mass sealing device and method |
| CN109092213A (en) * | 2017-06-21 | 2018-12-28 | 阿克森斯公司 | The fixed bed or moving-burden bed reactor of the Radial Flow of the pending process stream of tool comprising improved inside |
| CN109651036B (en) * | 2017-10-10 | 2022-03-11 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin from synthesis gas |
| CN109651036A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | A method of by preparing low-carbon olefin |
| CN111099720B (en) * | 2018-10-26 | 2022-05-03 | 中国石油化工股份有限公司 | Sewage biological treatment reactor and treatment method thereof |
| CN111099720A (en) * | 2018-10-26 | 2020-05-05 | 中国石油化工股份有限公司 | Sewage biological treatment reactor and treatment method thereof |
| CN114286853A (en) * | 2019-08-26 | 2022-04-05 | 环球油品有限责任公司 | Device for catalytic reforming of hydrocarbons with flow distributor and method for reforming of hydrocarbons |
| CN114286853B (en) * | 2019-08-26 | 2024-05-31 | 环球油品有限责任公司 | Apparatus for catalytically reforming hydrocarbons with flow distributor and method for reforming hydrocarbons |
| CN114425278A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for producing low-carbon olefin and application |
| CN113663607A (en) * | 2021-09-14 | 2021-11-19 | 中国石油大学(北京) | Downer reactor and method of operating same |
| WO2023231210A1 (en) * | 2022-05-13 | 2023-12-07 | 中国化学工程第三建设有限公司 | Uop propane dehydrogenation reactor device and maintenance method therefor |
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| Publication number | Publication date |
|---|---|
| CN1140331C (en) | 2004-03-03 |
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