CN1454970A - Continuous catalytic reforming reactor - Google Patents
Continuous catalytic reforming reactor Download PDFInfo
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Abstract
The present invention discloses a continuous catalytic reforming moving bed radial reactor. Said reactor adopts a circular container with catalytic bed as reaction equipment, the reactant inlet is positioned in the upper end of said reaction equipment, and its outlet is positioned in lower end of said reaction equipment, said catalytic bed is formed from external porous wall and internal porous wall cylinder in which the catalyst is filled. Said catalyst can be continuously flowed from top to bottom by means of gravity, at the same time the reaction material can be centrifugally flowed from centre toward exterior in the reaction equipment, and can be concurrently flowed from top to bottom in the distributary channel and collecting channel. Said invention is a Z-type centrifugal radial moving bed reactor, and its structure is simple and catalyst utilization rate is high.
Description
Technical field
The present invention relates to a kind of mesolow or non-pressurized gas and solid phase catalyzing moving bed radial reactor of being applicable to, particularly a kind of catalysis moving bed radial reactor that is applicable to the hydro carbons catalytic reforming.
Background technology
In the existing catalystic reforming method for hydrocarbons, generally adopt gas-solid phase shift movable bed radial catalystic reactor.Described gas-solid phase shift movable bed radial reactor generally is the outer hull that is made of reactor top end socket, cylindrical side wall and bottom bulkhead, in described reactor, have one by porous tube outside cylindrical and cylindrical in the annular space that constitutes of porous tube, promptly form columnar beds behind the catalyzer of packing into.Porous tube can stop granules of catalyst to enter the internal space of interior porous tube in cylindrical, and it can be used as gas-distributing pipe simultaneously, plays the effect of divider, and vapor-phase reactant is assigned to described beds as far as possible equably.Described cylindrical outer porous tube can stop granules of catalyst to enter space outerpace between outer porous tube and the housing, and it can be used as effuser, collecting reaction product.Otherwise outer porous tube can be used as gas-distributing pipe, and interior porous tube is as effuser.In gas-solid phase shift movable bed radial reactor, solid catalyst moves axially along reactor by gravity, and vapor-phase reactant, reacts under a solid catalyst condition that material exists radially or near radially by beds along reactor.U.S. Pat 3,706,536 disclose the first-generation CONTINUOUS REFORMER technology of UOP (Praxair Technology, Inc), and 3 or 4 reactors are overlapping in the reforming process; Chinese patent CN1042559A discloses the continuous reformer technology of Inst Francais Du Petrole (Compaynie Francaise des Petroles), and reactive system generally adopts 3 or 4 reactors to be arranged in juxtaposition.In the above-mentioned technology, all being full of catalyzer in each reactor also moves down by gravity, feed the educt flow radial flow in the reactor chamber, pass annular catalyst (entad flowing) from outer ring space, enter the pipe core space, connect the bottom opening outflow of pipe core then from reactor, form the enterprising Z type radial inflow flow pattern that goes out down.
And in improved method thereafter, Chinese patent CN85103262B and U.S. Pat 4,567,023 discloses second and third CONTINUOUS REFORMER technology of UOP in generation, and the entrance and exit end of educt flow is all in the upper end of reactor, reaction mass from outer ring space radially ecto-entad flow and pass annular catalyst, being radial inflow flows, enter the pipe core space, the top drilling that connects pipe core from reactor flows out then, forms the Π type radial inflow flow pattern that goes out on enterprising.Analyze above-mentioned two kinds of technologies, because it all is that radial inflow is flowed that reactor used structure causes the flow pattern of reaction mass, to reactor radially, the diameter of general outer shroud is about a times of pipe core diameter, so entad flowing of ecto-entad will be about the radially flow velocity of reaction mass also will double; In addition, according to reaction characteristics, catforming process generates hydrogen simultaneously, entire reaction belongs to the reaction that volume increases, and that is to say, reaction mass is at radial flow during through catalytic bed, volume constantly increases, and the cumulative volume increase of reactant flow is nearly 2.5 times in whole catforming process.As everyone knows, in above-mentioned reactor, the direction that flow and the particle of reactant move is vertical, reaction mass flows the particle in the bed is produced a power of pointing to effuser wall direction, therefore increased the friction resistance of catalyzer and wall place in the bed, blocked particle moving down along wall.If the reaction mass radial velocity is enough big, the friction resistance that produces will be enough to support the weight of whole bed, make particle stop to move down, or particle is axially moved down near the effuser grid distributor of center to stop closing at least, this moment, bed was known as because mobile produce " adherent " of reaction mass.Like this, catalyzer will be fixed on formation dead band in the bed and cause coking and deactivation, and the catalyzer in the dead band can not in time shift out bed and go regeneration behind inactivation, cause reaction to worsen.When the reaction mass radial velocity continues to increase, between gas-distributing pipe wall and granular layer, also can form " cavity ", along with the increase of airshed, the thickness of cavity enlarges gradually, makes particle stop to move down.Because the formation of cavity makes air-flow distribution vertically become inhomogeneous,, make the reactor can not normal running until forming short circuit.Hence one can see that, for avoiding the appearance of " adherent " phenomenon, it is crucial reducing the radially flow velocity that points to effuser, for this reason, moving-burden bed reactor often is designed to thin bed radial reactor, the diameter difference of the inside and outside wall of catalytic bed is within reason big, to reduce the radially variation of flow velocity as far as possible, has taked relatively harsher uniform fluid distribution measure simultaneously.Above-mentioned two kinds of technologies all pass through to reduce pipe core percentage of open area, increase pressure drop with control reactant flow axially uniform in reactor.
Chinese patent CN1258558A disclosed method is that the reaction mass inlet is opened the side in reactor shell, the vertical height at reactant entrance center is positioned at the middle part of catalytic reaction zone axial height, reactant ecto-entad radial flow is crossed catalytic bed, enter the center effuser, flow out from reactor bottom then, be difficult to control reactant flow uniform distribution vertically like this, also easily produce " adherent " phenomenon.Cut apart catalytic bed by the method that midfeather is set among the Chinese patent CN1127159A in beds, scheming to reduce the possibility of the adherent generation of catalyzer, but this method does not solve the adherent root problem of catalyzer, causes the structure of reactor complexity on the contrary.U.S. Pat 3,882,015 disclosed method and U.S. Pat 3,706,536 disclosed technology differences, educt flow enters pipe core from the reactor central tube bottom, and by annular catalyst radial inflow annular space, flow out by reactor top and the joining outlet of annular space then, form the centrifugal flow pattern of Z type that goes out on advancing down; The flow direction of this technology reaction mass is opposite with the flow direction of granules of catalyst, can blocked catalysts evenly move downwards.
To sum up patent is described, all kinds of catalysis moving bed radial reactors have adopted the reaction mass ecto-entad along radial direction mobile mode entad mostly, radial gas presents acceleration tendency, reforming reaction is the process that increases volume in addition again, therefore, for avoiding " adherent ", brought very big restriction and difficulty for the moving bed radial DESIGN OF REACTOR.Simultaneously, entad the flowing of existing patented technology ecto-entad will be because the inlet feed thermosteresis of flow manifold outside will cause that inevitably the axial temperature of catalytic bed bed is poor.
Summary of the invention
The technical issues that need to address of the present invention are:
(1) reduces radially flow velocity of educt flow, thereby avoid the appearance of catalyzer " adherent " phenomenon;
(2) reduce the thermosteresis of reaction mass in flow manifold, make the axial temperature of catalytic bed bed more even.
The present invention solves the problems of the technologies described above with this by a kind of centrifugal continuous catalytic reforming reactor is provided, and overcomes the defective that exists in the prior art simultaneously.In addition, centrifugal continuous catalytic reforming reactor of the present invention has simple in structure and loads and unloads catalyzer characteristics easily.
Inventive concept
Design of the present invention is such:
(1) the mobile employing reaction mass of reaction mass is shunted through reactor central tube, uniform distribution radially enters annular catalyst vertically, space afflux between annular catalyst and reactor wall flows out, be the centrifugal flow shape, the flow velocity of the reaction mass of volume increase is radially reduced gradually, thereby guarantee that reacting material outlet wall flow velocity is lower, the possibility of having avoided catalyzer " adherent " to take place.
(2) reaction mass is made radially centrifugal flow from inside to outside, and the import reaction mass does not have thermosteresis in the flow manifold of center, has guaranteed the even of the interior axial temperature of reactor.
(3) reaction mass is done from inside to outside, and import and outlet lay respectively at the top and bottom of reactor, makes reaction mass make in the same way relative mobile in flow manifold and afflux runner, is the enterprising Z type flow pattern that goes out down.Effuser adopts porous tube as wall, and (or using grid) opened wide on the bed top of catalyzer fully, and be not only simple in structure, and the loading and unloading catalyzer is very convenient.
(4) reaction mass is done from inside to outside, the enterprising Z type flow pattern that goes out down, and effuser adopts porous tube as wall, and the bed top of catalyzer also can seal fully, and reaction mass is made pure radial flow, helps reaction mass uniform distribution vertically.According to above-mentioned design, the present invention proposes following technical scheme:
The said continuous catalytic reforming reactor of the present invention comprises:
Catalytic bed in one cylindrical vessel and the container, on the wall of this cylindrical vessel, be provided with reacting material inlet, reacting product outlet, catalyst addition tube and catalyzer discharge tube, it is characterized in that: described reacting material inlet places the top of cylindrical vessel, and described reacting product outlet places the cylindrical vessel bottom.
In cylindrical vessel, comprise with the coaxial setting of cylindrical vessel, the contour not perforate of upper portion side wall of arranging according to this from inside to outside, inner core and the perforate height porous wall urceolus identical or different that the bottom is porous wall with inner core, described inner core is connected with placing cylindrical vessel top reacting material inlet, constitutes the reaction mass flow manifold; Form catalytic bed between inner core and the porous wall urceolus; Constitute reaction product material afflux runner between porous wall urceolus and the cylindrical vessel sidewall, it is connected with the reacting product outlet that places the cylindrical vessel bottom.
Description of drawings Fig. 1 centrifugal catalysis moving bed radial structure of reactor synoptic diagram of the present invention is wherein: the 1-reacting material inlet; The 2-catalyst addition tube; 3-reaction mass flow manifold;
4-reaction product material afflux runner; The 5-catalytic bed; The 6-inner core;
7-porous wall urceolus; The 8-cylindrical vessel; 9-catalyzer discharge tube;
10-is catalytic bed radially; 11-catalyst sealing district; 12-catalyzer back up pad;
The 13-reacting product outlet.Fig. 2 is close to the perforated plate construction synoptic diagram wherein for reactor cross-section structural representation Fig. 3 bilayer among Fig. 1: 14-distribution hole; 15-porous slab; The 16-multihole lamina.Fig. 4 is double-deck to make somebody a mere figurehead the perforated plate construction synoptic diagram wherein: 14-distribution hole; 15-porous slab: 16-multihole lamina; The 17-support bar.Fig. 5 cell structure synoptic diagram is wherein: the 18-grizzly bar.Fig. 6 is that A-A makes up the arranged side by side and overlapping combination synoptic diagram of synoptic diagram Fig. 9 reactor combination synoptic diagram overlapping and arranged side by side Figure 10 reactor side by side to the overlapping combination synoptic diagram of synoptic diagram Fig. 7 reactor Fig. 8 reactor among Fig. 5
The present invention is further illustrated below in conjunction with accompanying drawing, and institute's accompanying drawing of painting just helps to understand the present invention, and it does not limit protection scope of the present invention:
By Fig. 1 and Fig. 2 as seen, the said centrifugal continuous catalytic reforming reactor of the present invention comprises:
In cylindrical shape container 8, comprise with the 8 coaxial settings of cylindrical shape container, the top of arranging according to this from inside to outside Not perforate of sidewall, bottom are interior tube 6 and the porous wall urceolus 7 of porous wall, interior tube 6 with place cylindrical shape container 8 Top reacting material inlet 1 is connected, and consists of reaction mass flow manifold 3; Interior tube 6 top sidewalls are provided with one section The catalyst sealing district 11 of not perforate, catalyst sealing district are radially bed district 10, catalyst sealing district 11 below 11 Radially catalytic bed 10 forms catalytic beds 5, catalytic bed 5 with place respectively cylindrical shape container 8 upper and lowers Catalyst addition tube 2 and catalyst discharging pipe 9 are connected, and catalytic bed 5 is supported by catalyst gripper shoe 12; Porous wall urceolus 7 is connected with the reacting product outlet 13 that places cylindrical shape container 8 bottoms, with the cylindrical shape container Consist of product material collection stream runner 4 between 8 sidewalls; Cross-sectional area and the reaction of product material collection stream runner 4 The ratio of the cross-sectional area of material flow manifold 3 is advisable with 1～5.
Described interior tube 6 equates that with the height H of porous wall urceolus 7 height of its opening area can be consistent or inconsistent, and when the height of opening area was inconsistent, the height of interior 6 opening areas was Hi, the height of the opening area of porous wall urceolus 7 is H, the height in catalyst sealing district 11 is Δ Hi, radially the height of catalytic bed 10 is Hi, the height Δ H in catalyst sealing district 11iFor catalytic bed 10 radially radially 0.5～5 times of thickness be advisable. Catalytic bed 5 tops are opened wide fully, simplified structure of reactor, made things convenient for the loading and unloading of catalyst; When the perforate district When the height in territory was consistent, the height of interior tube 6 and porous wall urceolus 7 opening areas was Hi, the height Δ H in catalyst sealing district 11iFor catalytic bed 10 radially radially 0.2～2 times of thickness be advisable, be fully close above catalytic bed 5 Seal, be conducive to the Radial Flow of reaction mass.
Embodiment
The described reactor of Fig. 1 is work like this:
Hydrogen hydrocarbon molar ratio is 1～3 in the raw material, and temperature of reaction is that 420～580 ℃, reaction pressure are 0.2～0.8Mpa, and weight space velocity is 0.5～2.5 hour
-1At reactor internal reaction material shown in Figure 1 is such mobile: reaction mass enters the flow manifold 3 that porous wall inner core 6 constitutes by reacting material inlet 1, react by the 14 radial inflow catalytic beds 10 of the distribution hole on the porous wall inner core 6, and then reaction product enters reaction product afflux runner 4 by the distribution hole 14 on the porous outer wall 7 from inside to outside, flows out through reacting product outlet 13.After granules of catalyst autocatalysis agent filling tube 2 flows into catalytic beds, do moving vertically from top to bottom, then, flow out catalytic bed by the catalyzer discharge tube 9 of bottom.
The reaction response device that the present invention proposes compared with prior art has the following advantages:
1. reduce the radial velocity of the outer gas collection barrel of the flow direction of reaction mass significantly, optimized the radially streamline distribution in the catalyst zone, avoided the generation of catalyzer " adherent " phenomenon;
2. reaction mass centrifugal flow from inside to outside, owing to do not have thermosteresis at the center flow manifold, it is even more to help in the reactor axial temperature;
3. optimized the streamline distribution in the catalyst sealing district, the ratio of effectively regulating axial flow and radial flow had both been avoided channel or stagnant area in the catalyst sealing district, can effectively reduce the height in catalyst sealing district again, had improved the utilization ratio of catalyzer;
4. the control pressure drop of interior porous wall reaction mass sparger generally only accounts for 15～50% of catalytic bed pressure drop, when realizing lower control pressure drop, has guaranteed reaction mass uniform distribution vertically;
5. unenclosed construction is adopted at the catalytic bed top, makes structure of reactor simple, helps the loading and unloading of catalyzer;
6. adopt best fluid distribution technology, guarantee reaction mass uniform distribution vertically, help evenly moving down of catalyzer, improved the utilising efficiency of catalyzer.
In addition, for satisfying the needs of different catalytic reforming process, a plurality of reactors of the present invention can be used in combination.Fig. 7～Figure 10 provides the synoptic diagram of several various combination modes.Wherein Fig. 7 is the signal with the overlapping combination of 4 reactors of the present invention; Fig. 8 is 4 reactors of the present invention synoptic diagram of combination side by side; Fig. 9 is the synoptic diagram that the reactor of the present invention of 1 reactor of the present invention and 3 overlapping combinations makes up side by side; Figure 10 is the synoptic diagram that the reactor of the present invention of 2 groups of 2 overlapping combinations makes up side by side.
Claims (10)
1, a kind of continuous catalytic reforming reactor, comprise catalytic bed (5) in a cylindrical vessel (8) and the container, on the wall of this cylindrical vessel (8), be provided with reacting material inlet (1), reacting product outlet (13), catalyst addition tube (2) and catalyzer discharge tube (9), it is characterized in that: described reacting material inlet (1) places the top of cylindrical vessel (8), and reacting product outlet (13) places cylindrical vessel (8) bottom; In cylindrical vessel (8), comprise with the coaxial setting of cylindrical vessel (8), arrange contour from inside to outside according to this, not perforate of upper portion side wall, the bottom is the inner core (6) and the perforate height porous wall urceolus (7) identical or different with inner core (6) of porous wall, inner core (6) is connected with placing cylindrical vessel (8) top reacting material inlet (1), constitute reaction mass flow manifold (3), form catalytic bed (5) between inner core (6) and the porous wall urceolus (7), constitute reaction product material afflux runner (4) between porous wall urceolus (7) and cylindrical vessel (8) sidewall, it is connected with the reacting product outlet (13) that places cylindrical vessel (8) bottom;
Wherein: catalytic bed (5) comprising: by inner core (6) not perforate of upper portion side wall section Δ H
iCatalyst sealing district (11) and inner core (6) lower sides perforate section H with porous wall urceolus (7) formation
iWith the radially catalytic bed (10) that porous wall urceolus (7) is formed, catalytic bed (5) is connected with catalyst addition tube (2) that places cylindrical vessel (8) upper and lower respectively and catalyzer discharge tube (9).
2, reactor as claimed in claim 1 is characterized in that, inner core (6) is highly different with porous wall urceolus (7) perforate, inner core (6) not perforate of upper portion side wall section Δ H
iFor the 0.5-5 of catalytic bed (10) radial thickness radially doubly.
3, reactor as claimed in claim 1 is characterized in that, inner core (6) is highly identical with porous wall urceolus (7) perforate, inner core (6) not perforate of upper portion side wall section Δ H
iFor the 0.2-3 of catalytic bed (10) radial thickness radially doubly.
As claim 2 or 3 described reactors, it is characterized in that 4, the ratio of the cross-sectional area of the cross-sectional area of reaction product material afflux runner (4) and reaction mass flow manifold (3) is 1～5.
5, reactor as claimed in claim 4, it is characterized in that, porous wall urceolus (7) is close to multihole lamina (16) by porous slab (15), or by the structure of making somebody a mere figurehead with support bar (17) between porous slab (15) and the multihole lamina (16), wherein the percentage of open area of multihole lamina (16) is 30～50%, and porous slab (15) percentage of open area is 20～40%.
6, reactor as claimed in claim 4 is characterized in that, porous wall urceolus (7) is a cell structure, and the porosity of grid is 40～60%.
7, reactor as claimed in claim 4, it is characterized in that, the porous wall structure of inner core (6) is for to be close to multihole lamina (16) by porous slab (15), or by built on stilts in the middle of porous slab (15) and the multihole lamina (16) with support bar (17), or be close to structure by the bilayer that porous slab (15) and grid are formed, wherein porous slab (15) percentage of open area is 0.5%～10%, and multihole lamina (16) percentage of open area is 30～50%, and the voidage of grid is 40～60%.
8, a kind of catalysis moving bed radial reactor is characterized in that, with at least two overlapping combinations of reactor as claimed in claim 1.
9, a kind of catalysis moving bed radial reactor is characterized in that, at least two reactors as claimed in claim 1 are made up side by side.
10. a catalysis moving bed radial reactor is characterized in that, with at least three reactor as claimed in claim 1 combinations arranged side by side and overlapping.
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| CN 03116945 CN1290602C (en) | 2003-05-16 | 2003-05-16 | Continuous catalytic reforming reactor |
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| EP2246320A1 (en) | 2009-04-29 | 2010-11-03 | Bayer MaterialScience AG | Process for the preparation of aromatic amines |
| CN102010759A (en) * | 2010-12-14 | 2011-04-13 | 大连理工大学 | Method and device for producing hydrogen-rich gases by catalyzing and gasifying solid fuels |
| CN102258962A (en) * | 2011-05-24 | 2011-11-30 | 徐志刚 | Gas solid phase catalytic reactor |
| CN102875469A (en) * | 2011-07-14 | 2013-01-16 | 中国石油化工股份有限公司 | Method for preparing caprolactam through adopting radial moving bed reactor |
| 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 |
| 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 |
| CN104650960A (en) * | 2013-11-19 | 2015-05-27 | 中国石油天然气股份有限公司 | Catalytic reforming process |
| TWI510285B (en) * | 2009-07-29 | 2015-12-01 | IFP Energies Nouvelles | Device for distributing feed and recovering effluents in a radial bed catalytic reactor and process using the same |
| CN105621357A (en) * | 2014-10-27 | 2016-06-01 | 中国石油化工股份有限公司 | Methane-reforming and hydrogen-production method |
| CN108854862A (en) * | 2017-05-11 | 2018-11-23 | 中国石化工程建设有限公司 | A kind of particulate matter bed supportive grid and radial flow reactors |
| CN108854857A (en) * | 2017-05-11 | 2018-11-23 | 中国石化工程建设有限公司 | A kind of flow-guiding type supportive grid and flowing bed reactor for reactor catalyst 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 |
| CN113509894A (en) * | 2021-07-22 | 2021-10-19 | 中冶赛迪工程技术股份有限公司 | Moving bed gas-solid radial reactor |
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| EP2246320A1 (en) | 2009-04-29 | 2010-11-03 | Bayer MaterialScience AG | Process for the preparation of aromatic amines |
| DE102009019436A1 (en) | 2009-04-29 | 2010-11-04 | Bayer Materialscience Ag | Process for the preparation of aromatic amines |
| TWI510285B (en) * | 2009-07-29 | 2015-12-01 | IFP Energies Nouvelles | Device for distributing feed and recovering effluents in a radial bed catalytic reactor and process using the same |
| CN102010759A (en) * | 2010-12-14 | 2011-04-13 | 大连理工大学 | Method and device for producing hydrogen-rich gases by catalyzing and gasifying solid fuels |
| CN102258962A (en) * | 2011-05-24 | 2011-11-30 | 徐志刚 | Gas solid phase catalytic reactor |
| CN102258962B (en) * | 2011-05-24 | 2013-07-31 | 徐志刚 | Gas solid phase catalytic reactor |
| CN102875469A (en) * | 2011-07-14 | 2013-01-16 | 中国石油化工股份有限公司 | Method for preparing caprolactam through adopting radial moving bed reactor |
| 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 |
| 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 |
| 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 |
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| CN105621357A (en) * | 2014-10-27 | 2016-06-01 | 中国石油化工股份有限公司 | Methane-reforming and hydrogen-production method |
| CN108854862A (en) * | 2017-05-11 | 2018-11-23 | 中国石化工程建设有限公司 | A kind of particulate matter bed supportive grid and radial flow reactors |
| CN108854857A (en) * | 2017-05-11 | 2018-11-23 | 中国石化工程建设有限公司 | A kind of flow-guiding type supportive grid and flowing bed reactor for reactor catalyst bed |
| CN108854857B (en) * | 2017-05-11 | 2021-05-18 | 中国石化工程建设有限公司 | Flow guide type support grid for reactor catalyst bed layer and fluidized bed reactor |
| CN108854862B (en) * | 2017-05-11 | 2021-05-18 | 中国石化工程建设有限公司 | Particulate matter bed layer support grid and radial flow reactor |
| 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 |
| CN113509894A (en) * | 2021-07-22 | 2021-10-19 | 中冶赛迪工程技术股份有限公司 | Moving bed gas-solid radial reactor |
| CN113828251A (en) * | 2021-09-18 | 2021-12-24 | 中国化学工程第六建设有限公司 | Continuous catalytic reforming reaction device |
| CN113828251B (en) * | 2021-09-18 | 2023-05-05 | 中国化学工程第六建设有限公司 | Continuous catalytic reforming reaction device |
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