• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    catalyst regeneration zone divided into sectors for regenerative catalytic units. The present invention relates to a combustion zone of a regenerative catalytic unit for the continuous regeneration of the catalyst, that combustion zone having an annular shape and being divided into at least two combustion stages, each stage being divided into one. number n of substantially equal radial sectors, the catalyst gravitatively flowing from a sector of the first combustion stage to the sector vertically of the second combustion stage by means of lowering legs, and the circulation of the combustion gas being such that The flue gas travels successively through all sectors of the first combustion stage in any order, then all sectors of the second combustion stage in any order.
    公开号:BR112012023915B1
    申请号:R112012023915-5
    申请日:2011-02-18
    公开日:2019-02-26
    发明作者:Eric Sanchez；Frédéric Bazer-Bachi；Beatrice Fischer
    申请人:IFP Energies Nouvelles；
    IPC主号:
    专利说明:

    Descriptive Report of the Invention Patent for the PROCESS OF REGENERATION OF A COOKED CATALYST WHICH CIRCULES IN MOBILE LAYER AND APPLICATION OF THE PROCESS.
    FIELD OF THE INVENTION [001] The present invention relates to the domain of the units that appeal to the mobile layer technology, technology that is found, for example, in the catalytic refining units of gasolines, in the structural isomerization units, in the units of metastasis or in certain oligocracking or dehydrogenation units. This technology is characterized by the fact that this catalytic layer follows a slow gravitational movement, while the load to be treated crosses the layer in a transversal or radial way. For this, the charge is usually introduced at the periphery of the catalytic layer in gravity flow, and the reaction effluents are collected in a central collector. Circulation from the center to the periphery of the catalytic layer is also considerable.
    [002] In catalytic refining units, the regeneration zone of the coking catalyst is also used, according to the mobile layer technology. This regeneration zone comprises several stages, combustion, oxychlorination, calcination and reduction of the catalyst which are described in the patents FR2641712, FR2761910 and FR2922786, for example.
    [003] The present invention relates more particularly to an arrangement of the combustion zone that is part of the regeneration zone, that combustion zone being divided into radial sectors, each sector being crossed by the combustion gas, according to a specific path.
    [004] The advantages of this new configuration in relation to the previous technique are a better control in temperature of this zone of
    Petition 870180056795, of 06/29/2018, p. 7/30
    2/15 combustion and an optimized consumption of oxidizing gas. The present invention also entails a simplification of the combustion zone internals in relation to the prior art.
    EXAMINATION OF THE PREVIOUS TECHNIQUE [005] In the so-called regenerative units, such as, for example, the catalytic refining of gasolines, the regeneration of the coking catalyst, after passing through the reaction zone, is carried out continuously.
    [006] This is the case, for example, with high severity catalytic refining. In this type of unit, the catalyst is continuously extracted from the reactor (s), purified from the hydrogen it contains and sent to a regeneration zone in which the coke is burned in a controlled manner to restore the activity of the catalyst. Other operations are carried out in the regeneration zone, such as oxychlorination, calcination and reduction of the catalyst, but the present invention relates particularly to the combustion zone.
    [007] In this combustion zone, it is advisable to avoid overheating the catalyst so as not to deteriorate its catalytic performance and avoid the formation of a hot spot, which requires working with oxygen very diluted by inert gases (nitrogen and carbon dioxide, for example) .
    [008] For this purpose, it is customary to recycle the oxygen-depleted combustion gases to serve as a diluent, injecting a small amount of air, so that the oxygen content is sufficiently low, to limit the exotherm of the combustion reaction.
    [009] It is known to the technician to carry out combustion in two stages, a first stage at a low temperature and with an oxidant defect to burn most of the coke in a controlled manner with an important, but nevertheless limited, temperature increase. second stage at the highest temperature and ex
    Petition 870180056795, of 06/29/2018, p. 8/30
    3/15 combustion process to end combustion, but accompanied by a relatively small temperature rise due to the small amount of coke that remains to burn.
    [0010] In the prior art, coke combustion is generally carried out in two narrow thickness radial layers arranged in a crown, in which the catalyst circulates from top to bottom at low speed by gravity flow, the flue gas circulating horizontally through the radial layer , most often from the outside of the layer to the inside.
    [0011] The stretched gases from the different regeneration zones are recovered and treated so that they can be recycled again in the regeneration zone. Indeed, according to the prior art, it is known to dilute oxygen by nitrogen. Now nitrogen is a very expensive gas. For example, for a refining unit of 40 tonnes of catalyst, if regeneration gases were not reused, it would be necessary to use approximately 6000 to 10,000 Nm3 / h of nitrogen.
    [0012] By recycling the regeneration gases, the consumption of fresh nitrogen drops to approximately 80 Nm3 / h. In addition, the regeneration gas circuit comprises various costly equipment such as the recycling compressor, dryer, electric oven and exchanger. Any reduction in nitrogen flow therefore has a very considerable impact on the investment costs and the operating costs of the catalyst regeneration circuit.
    [0013] One of the objectives of the present invention is to optimize the use of inert gas flow and thus reduce the size of the equipment for the same amount of regenerated catalyst, using a new type regeneration zone.
    [0014] The closest prior art is the patent application published under FR 2 934 963 A1, which describes a zone
    Petition 870180056795, of 06/29/2018, p. 9/30
    4/15 combustion, comprising at least one annular coke combustion zone, this zone being divided into radial sectors, each stage comprising N radial sectors.
    [0015] In the aforementioned order, combustion is generated by the notion of molar composition with a constant oxygen content at the entrance of each sector. This results in a variation in the amount of coke burned from one sector to another in the same stage and, therefore, a possible inhomogeneity of combustion quality in the different sectors.
    [0016] According to the present invention, it is the molar flow of oxygen that is kept constant over all sectors of a stage, so that the amount of coke burned is the same over all sectors of a stage. The improvement of the combustion homogeneity over all sectors, which constitute a stage, then guarantees optimized catalytic performances, necessary to obtain the high octane indexes researched, for example, in the regenerative refining units.
    BRIEF DESCRIPTION OF THE FIGURES [0017] Figure 1 represents a schematic sectional view of a combustion zone, according to the invention with more than 2 sectors per stage and showing the combustion gas circuit.
    [0018] Figure 2 represents a schematic view in top view of the combustion zone, according to the invention, which allows to distinguish 4 sectors per stage.
    BRIEF DESCRIPTION OF THE INVENTION [0019] The present invention describes a process for regenerating a coking catalyst at the end of a reaction zone, the catalyst circulating in the regenerating zone in the mobile layer state. Movable layer means a gravitational circulation mode of the catalyst, the gas allowing the regeneration of that catalyst
    Petition 870180056795, of 06/29/2018, p. 10/30
    5/15 in the regeneration zone that circulates in a direction substantially perpendicular to that of the flow of the catalyst.
    [0020] The present invention consists more precisely in a process of regeneration of the coking catalyst at the exit of the reaction zone that comprises at least one combustion zone of the coke deposited on the catalyst.
    [0021] The regeneration process, according to the present invention, can be applied to so-called regenerative units, in which the coking catalyst during the reaction must be regenerated continuously. The catalyst regeneration process generally consists of an oxychlorination step, calcination followed by a catalyst reduction step. The regenerated catalyst is reintroduced into the reaction zone. The steps located downstream of the combustion step are not part of the present invention, which is perfectly compatible with any embodiment of those steps downstream. [0022] The present invention, therefore, refers to the combustion stage of the regeneration zone, named after the combustion zone.
    [0023] The combustion zone, according to the present invention, is a zone with two stages, in which the catalyst circulates in a mobile layer, that is, in gravity flow, and in which the oxidizing gas passes through the catalyst layer, in a radially, preferably from the outer periphery of the layer to its inner periphery. The catalyst layer has an annular shape and is divided into a number of radial sectors.
    [0024] For the understanding of the gas circulation circuit, the sectors of the first stage of combustion are numbered from 1 to N, and the sectors of the second stage are numbered from T to Ν '.
    [0025] A sector i of the first stage and sector i 'of the second stage are approximately vertical to each other, and the number
    Petition 870180056795, of 06/29/2018, p. 11/30
    6/15 sectors of the first stage and equal to the number of sectors of the second stage. Sectors i and i ', vertically from each other, are said corresponding sectors.
    [0026] The flue gas circulation consists of going through all sectors of the first stage in any order, then all sectors of the second stage in any order. For example, in a configuration where each stage is divided into 4 sectors, a possible circulation circuit according to the present invention is circuit 1, 2, 3, 4, T, 2 ', 3', 4 '.
    [0027] Another possible circuit is circuit 1, 2, 3, 4, 4 ', 3', 2 ', T, according to the shape, by which the transition of the combustion gas between the two combustion stages is ensured .
    [0028] One can also consider a type 1, 3, 4, 2, 2 ', 4', 3 ', T circuit. In reality, any circuit, covering the sectors of the first stage in any order, then the sectors the second stage in any order also remains within the scope of the present invention.
    [0029] Another important feature of the present invention that distinguishes it from the prior art is the fact that each combustion stage works with a constant molar flow of oxygen. More precisely, each sector of a specific combustion stage receives an oxidizing gas at the entrance, just as the molar flow of oxygen is always the same.
    [0030] Thus, the flow of coke burned in each sector of the same stage is the same. The homogeneity of the thermal gradient in the different sectors of the same combustion stage then guarantees the quality of the catalyst regeneration.
    [0031] As the flow rate of oxidant gas evolves from one sector to the next, this means that the oxygen content is not constant from one sector to the next one stage. This remains true for
    Petition 870180056795, of 06/29/2018, p. 12/30
    7/15 sectors of the second combustion stage.
    [0032] At the level of the first combustion stage, the amount of oxygen introduced over each sector corresponds to the combustion of an amount of coke between 50% and 90% of the total coke deposited on the catalyst, and preferably between 60% and 80 %, and at the second stage level, the amount of oxygen introduced corresponds to the total combustion of the residual coke. [0033] In practice the oxidizing gas is introduced over all sectors of the second stage in excess, this excess can be quantified by an excess of oxygen at the exit of the sector between 0.1% and 0.5% and, preferably, included between 0.2% and 0.4% oxygen.
    [0034] Preferably, the number of combustion stages is two, and the number of sectors per stage is between 2 and 8, and preferably between 2 and 4.
    [0035] Cooling gas supplies are made at the entrance of each sector in order to maintain the inlet temperature within certain limits, generally 460 to 480 ° C for the first stage sectors, and 470 ° C to 490 ° C for the second stage sectors.
    [0036] This cooling gas is generally the oxidizing gas trapped at the compressor outlet of the recycling circuit, therefore, before it passes through the series of heat exchangers and / or furnaces, forming part of the traditional circuit for type units regenerative refining. Cooling gas supplies are generally made by means of specific lines that lead to the lines that allow to connect the output of one sector to the entrance of the neighboring sector. In the same line, the cooling gas is mixed with a flow of combustion gas, in order to allow the supply of combustion between the different sectors of the same stage. Oxidizing gas can, in general, contain between 4% and 21% of oxygen. Petition 870180056795, dated 06/29/2018, p. 13/30
    8/15 not.
    [0037] A variant of the combustion zone, according to the present invention, consists of no longer cooling the combustion gas by means of cooling gas supplies, but using heat exchangers, thus allowing to significantly reduce the total combustion gas flow required for regeneration of the catalyst.
    [0038] Another variant of the process is to simplify the combustion gas distribution circuit, adopting an alternate configuration between the different sectors.
    [0039] Alternate configuration is defined as a configuration, in which the combustion gas circulates from the outside to the inside over a specific sector, and then circulates from the inside to the outside over the next sector, and so on. It is called the next sector of a specific sector, the geometrically neighboring sector that is covered by the oxidizing gas.
    DETAILED DESCRIPTION OF THE INVENTION [0040] The present invention can be described as a combustion zone for regenerative units, for example, for regenerative refining or structural isomerization, in which the flow of the catalyst takes place in a mobile layer (ie in flow) gravity), from a first stage to a second stage, each stage being divided into a number of radial sectors, and the circulation of the combustion gas in a circuit characterized by the fact that the combustion gas passes successively through all sectors of the first stage , then successively all sectors of the second stage.
    [0041] In the case of a regenerative refining unit or any other processes, requiring continuous catalyst regeneration, the catalyst regeneration zone comprises in addition to the combustion zone that allows combustion of the deposit coke
    Petition 870180056795, of 06/29/2018, p. 14/30
    9/15 on the catalyst, from other areas in which oxychlorination, calcination and reduction of the catalyst take place. These other zones will not be described in this text, as they remain, according to their configuration in the prior art.
    [0042] Figure 1 shows the structure of the regeneration zone, according to the invention.
    [0043] The catalyst circuit in sector 4 will be described below, and that of the oxidant gas in sector 1.
    [0044] The numbering of the sectors of the first combustion stage is: 1, 2, 3, 4.
    [0045] The numbering of the sectors of the second stage, compared to those of the first combustion stage is: T, 2 ', 3' and 4 '. These sectors are separated by a wall (9). The sectors that are vertical to each other, such as 1 and T, 2 and 2 ', 3 and 3', 4 and 4 'are said corresponding sectors.
    [0046] The catalyst is introduced in the upper compartment (I) by the leg (5) and circulates in the compartment (I) of sector 4 in gravity flow, then it passes through the leg (5 ') to be introduced in the lower compartment (I ') of sector 3'. He leaves sector 4 'by the descent line (5).
    [0047] The fuel gas is introduced in compartment (I) through the peripheral conduit (E) communicating with sector 1, a box (6) forcing the gas to circulate towards the outer crown of that zone. The gas passes radially through the catalytic layer (I), from the outer periphery towards the inner periphery of the catalytic layer and is found in the annular space (II).
    [0048] This annular space (II) allows the combustion gas to be sent via line (7) to the sector entrance, following the same annular space, be it sector 2 that appears in figure 2. It is called sector following a determined sector the geometrically neighboring sector
    Petition 870180056795, of 06/29/2018, p. 15/30
    10/15 that is followed by the combustion gas, according to the direction of travel of that combustion gas.
    [0049] The gas circuit in sector 2 is the same as that described for sector 1.
    [0050] From the exit of sector 2 the oxidizing gas passes to the entrance of sector 3, after the exit of sector 3 the oxidizing gas passes to the entrance of sector 4.
    [0051] From the exit of sector 4, the combustion gas is introduced at the entrance of sector 4 'belonging to the second stage of combustion disposed below that sector 4.
    [0052] The oxidizing gas continues its circuit in the second stage of combustion: exit from sector 4 'towards the entrance of sector 3'; exit from sector 3 'towards the entrance of sector 2'; exit from sector 2 'towards the entrance of sector T, and exit from sector T towards the outside through the conduit (S).
    [0053] The introductions of the mixture of cooling gas / supply of combustion gas are made by the lines (8) that are connected to the lines (7).
    [0054] The oxidizing gas leaves the last sector of the second stage of combustion through the evacuation duct (S).
    [0055] The present invention can therefore be defined as a process of regenerating a coking catalyst that circulates in a mobile layer, that catalyst being coking outside the reaction zone.
    [0056] The regeneration process, according to the invention, comprises at least one combustion zone of the coke deposited on the catalyst, that combustion zone having an annular shape and being divided into at least two combustion stages, each stage of combustion. combustion being divided into a number N of radially equal sectors.
    Petition 870180056795, of 06/29/2018, p. 16/30
    11/15 [0057] The catalyst drains gravitationally from a sector of the first combustion stage to the sector located vertically in the second combustion stage by means of lowering legs, and the circulation of the flue gas circulation gas is such that the flue gas passes successively through all sectors of the first combustion stage in any order, then all sectors of the second combustion stage in any order.
    [0058] The molar flow of combustion gas has a first value for all sectors of the first stage, this first value allowing the combustion of an amount of coke between 50% and 90% of the total coke deposited on the catalyst, preferably between 60 and 80%.
    [0059] The molar flow rate of oxidant has the same second value, different from the previous one, for all sectors of the second combustion stage, this second value allowing the total combustion of residual coke with an excess of oxygen in the oxidant gas between 0, 1 and 0.5% oxygen, preferably between 0.2 and 0.4% oxygen.
    [0060] The inlet temperature of all sectors of the first combustion stage is generally between 460 and 490 ° C, and the inlet temperature of all sectors of the second combustion stage is generally between 470 and 510 ° C.
    [0061] The number of sectors in each combustion stage is generally between 2 and 8, and preferably between 2 and 4.
    [0062] According to a first variant of the present invention, the number of sectors being 4 in each combustion stage, and numbering 1, 2, 3, 4 the sectors of the first stage and T, 2 ', 3', 4 'the corresponding sectors of the second stage, the oxidant gas follows
    Petition 870180056795, of 06/29/2018, p. 17/30
    12/15 circuit 1, 2, 3, 4, 4 ', 3', 2 ', Τ.
    [0063] According to a second variant of the present invention, the number of sectors being 2 at each combustion stage, and numbering 1, 2 the sectors of the first stage and T, 2 'the corresponding sectors of the second stage, the gas oxidizer follows circuit 1, 2, 2 ', T.
    [0064] According to a third variant of the present invention, the oxidizing gas travels through each sector going from the outer periphery to the inner periphery of each of the sectors.
    [0065] According to a variant, the oxidant gas travels through each sector, going from the internal periphery towards the external periphery of each sector.
    [0066] Finally, according to another variant, the oxidizing gas circulates from the external periphery towards the internal periphery over a specific sector, and from the internal periphery towards the external periphery over the neighboring sector of the sector considered.
    [0067] In general, the oxidizing gas is air that has an oxygen content between 4% and 21%.
    [0068] The cooling of the oxidizing gas at the entrance of each sector can in a variant of the present invention be carried out by means of a set of exchangers.
    [0069] The catalyst regeneration process, according to the present invention, can be applied to all units that use a catalyst that needs continuous regeneration and in which the catalyst flows in a mobile layer. The following units can be cited as examples: regenerative refining of gasolines, structural isomerization, metastasis, oligocracking, dehydrogenation.
    COMPARATIVE EXAMPLE [0070] The following example compares the configuration, according to
    Petition 870180056795, of 06/29/2018, p. 18/30
    13/15 the prior art represented by the application published under number FR 2 934 963 A1, with the configuration, according to the present invention. [0071] The regeneration zone is divided into 2 stages, each stage comprising 4 sectors noted with 1,2,3,4 for the first stage and T, 2 ', 3', 4 'for the second stage.
    [0072] Two types of oxidant gas circulation are compared:
    1, T, 2, 2 ', 3, 3', 4, 4 ', according to the geometric configuration of the prior art
    1, 2, 3, 4, 4 ', 3', 2 ', T, according to the invention.
    The conditions common to both configurations are as follows:
    -120 kg.h ' 1 of coke to be burned (be 1800 kg.h' 1 of coking catalyst);
    - 2 combustion stages;
    - 4 sectors per stage;
    - average inlet temperature for sectors 1 to 4 of the first combustion stage (475 ° C):
    - average inlet temperature for sectors 1 to 4 of the second combustion stage (480 ° C).
    [0073] According to the prior art, the management of combustion gas flow rates is carried out, maintaining a constant oxygen content at the entrance of each section, which causes disparities, relatively important in the amount of coke burned and, therefore, in the outlet temperatures of the sectors of the same stage.
    [0074] In accordance with the present invention, the management of combustion gas flows is carried out, keeping the oxygen flow constant at a certain value over all sectors of the first stage, then at a different value over all stages of the second stage, either:
    - molar flow of oxygen that arrives over sectors 1 to 4 of the first combustion stage adjusted to burn 2/3 of coPetition 870180056795, dated 06/29/2018, p. 19/30
    14/15 that;
    - molar flow of oxygen that arrives over sectors T at 4 'of the second combustion stage adjusted to burn the remaining coke, with an excess of 30% in relation to the amount of stoichiometric oxygen.
    [0075] It appears in table 1 below, according to the invention, that the outlet temperatures of the sectors of the first stage are situated in the range of 530 to 521 ° C and in the range of 506 to 501 ° C for the sectors of the second stage. While, according to the prior art (see table 2), the dispersion of outlet temperatures in each sector is much more pronounced.
    [0076] It is also noted that, according to the invention, the percentage of coke burned is quite constant over all sectors of the same stage (66.6% in the first stage and 100% in the second stage), whereas it is very different from one sector to another, according to the previous technique.
    Table 1 (according to the invention)
    Stage 1 / Sectors 1 2 3 4 Coke conversion (%) 66.6 66.6 66.6 66.6 Flow (t.h ' 1 ) 7.4 8.7 10.0 11.3 % mol O2 0.80 0.68 0.59 0.52 Tempered (° C) 470 473 475 477 Output (° C) 530 529 525 521 Stage 2 / Sectors T 2' 3 ' 4 ' Coke conversion (%) 100 100 100 100 Flow (t.h ' 1 ) 12.6 13.6 14.6 15.6 % mol O2 0.55 0.51 0.47 0.44 Tempered (° C) 480 480 480 480 Output (° C) 506 504 502 50T
    Petition 870180056795, of 06/29/2018, p. 20/30
    15/15
    Table 2 (according to the prior art)
    Stage 1 / Sectors 1 2 3 4 Coke conversion (%) 66.6 87.6 100 100 Flow (t.h ' 1 ) 7.4 9.7 11.4 12.7 % mol O2 0.8 0.8 0.8 0.8 Tempered (° C) 475 475 475 475 Output (° C) 536 522 516 51 Stage 2 / Sectors T 2' 3 ' 4 ' Coke conversion (%) 100 100 100 100 Flow (t.h ' 1 ) 8.6 10.9 12.6 13.9 % mol O2 0.55 0.55 0.55 0.55 Tempered (° C) 480 480 480 480 Output (° C) 518 491 480 480
    Petition 870180056795, of 06/29/2018, p. 21/30
    权利要求:
    Claims (6)
    [1]
    1. Process of regeneration of a coking catalyst that circulates in a mobile layer, characterized by the fact that it comprises at least one combustion zone of the coke deposited on the catalyst, that combustion zone having an annular shape and being divided into at least two stages combustion, each stage being divided into a number N of radial sectors, where N is in the range of 2 to 4, roughly equal, the catalyst flowing gravitatively from a sector of the first combustion stage (I) to the sector located in the vertical of the second stage of combustion (I ') by means of lowering legs (5.5'), θ the circulation of the flue gas being substantially perpendicular to that of the catalyst, and such that the flue gas passes successively through all sectors of the first combustion stage (I), then all sectors of the second combustion stage (I ') in the following order, where the number of sectors is 4 at each stage of the co-zone mbustão, and numbering 1, 2, 3, 4 the sectors of the first stage and T, 2 ', 3', 4 'the sectors facing the second stage, the oxidant gas follows circuit 1, 2, 3, 4 , 4 ', 3', 2 ', T, or where the number of sectors is 2 in each stage of the combustion zone, and numbering 1, 2 the sectors of the first stage and T, 2' the sectors facing each other of the second stage, the oxidant gas follows circuit 1, 2, 2 ', T, the molar oxidant flow having the same first value for all sectors of the first stage (I), that first value allowing the combustion of a quantity of coke in the range of 50% to 90% of the total coke deposited on the catalyst, and a second value, distinct from the previous one, for all sectors of the second combustion stage (I '), this second value allowing combustion
    Petition 870180153238, of 11/21/2018, p. 5/10
    [2]
    2/2 total residual coke with an excess of oxygen in the oxidant gas in the range of 0.1% to 0.5%, the inlet temperature of all sectors of the first stage of the combustion zone (I) being in the range of 460 to 490Ό, and the inlet temperature of all sectors of the second stage of the combustion zone (I ') being in the range of 470 to 510Ό.
    2. Process of regeneration of a coking catalyst, according to claim 1, characterized by the fact that the combustion of coke in the first stage of the combustion zone (I) is in the range of 60 to 80% of the total coke deposited on the catalyst, and the excess of oxygen in the oxidant gas in the second stage of the combustion zone (I ') is in the range of 0.2 to 0.4%.
    [3]
    3. Process of regeneration of a coking catalyst, according to claim 1 or 2, characterized by the fact that the combustion gas circulates from the outside to the inside over a determined sector of the combustion zone (l, l ') and from the inside abroad on the neighboring sector of the sector considered.
    [4]
    4. Process for the regeneration of a coking catalyst according to any one of claims 1 to 3, characterized by the fact that the oxidant gas is air that has an oxygen content in the range of 4 to 21%.
    [5]
    5. Process for the regeneration of a coking catalyst according to any one of claims 1 to 4, characterized by the fact that the combustion gas is cooled at the entrance of each sector of the combustion zone (l, l ') by a changers.
    [6]
    6. Application of the regeneration process of a coking catalyst, as defined in claim 1, characterized by the fact that it is related to the following processes: regenerative refining, structural isomerization, metastasis, oligocracking, dehydrogenation.
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    同族专利:
    公开号 | 公开日
    WO2011117478A1|2011-09-29|
    FR2957821B1|2014-08-29|
    FR2957821A1|2011-09-30|
    BR112012023915A2|2016-08-02|
    KR20130007631A|2013-01-18|
    ES2587759T3|2016-10-26|
    EP2550102A1|2013-01-30|
    US8901025B2|2014-12-02|
    EP2550102B1|2016-05-04|
    CN102869447B|2015-09-02|
    KR101844613B1|2018-04-02|
    CN102869447A|2013-01-09|
    US20130072376A1|2013-03-21|
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    法律状态:
    2018-04-03| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2018-08-28| B06A| Notification to applicant to reply to the report for non-patentability or inadequacy of the application according art. 36 industrial patent law|
    2019-01-29| B09A| Decision: intention to grant|
    2019-02-26| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 18/02/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1001161A|FR2957821B1|2010-03-24|2010-03-24|NEW AREA OF CATALYST REGENERATION DIVIDED IN SECTORS FOR REGENERATIVE CATALYTIC UNITS|
    FR1001161|2010-03-24|
    PCT/FR2011/000103|WO2011117478A1|2010-03-24|2011-02-18|Catalyst regeneration zone split into sectors for regenerative catalytic units|
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