• 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:
    The present invention discloses an inclined-bed reactor for implementing small amounts of catalyst, inclined gravity flow of the catalyst and transverse flow of the load, consisting of parallel outer and inner conical walls inclined at an angle alpha relative to vertically, the cone pointing up or down. The catalyst is introduced into the distribution zone by introduction legs (8) and collected at the outlet of the reaction zone by drainage legs (9), the assembly constituted by the conical walls and the legs (8, 9) being enclosed in a ferrule (5) comprising a hemispherical upper portion, a cylindrical central portion, and a hemispherical lower portion. The charge is admitted inside the ferrule (5) by an intake manifold (6) located at the top of the upper hemispherical part, and the reaction effluents are discharged through a lower pipe (7) located at the lower part. of the lower hemisphere. Application of the reactor to regenerative reforming.
    公开号:FR3033265A1
    申请号:FR1551821
    申请日:2015-03-04
    公开日:2016-09-09
    发明作者:Joana Fernandes；Julien Gornay；Alexandre Pagot；Fabian Lambert；Pierre-Yves Martin；Christophe Pierre；Francois Sala
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The invention relates to a novel inclined bed reactor technology with gravity flow of catalyst and cross flow of the load. It applies more particularly to the catalytic reforming of gasoline with continuous regeneration of the catalyst. The invention makes it possible to use very small quantities of catalyst and thus to control residence times of low value, a particularity that can not be achieved with current technologies. The present reactor makes it possible to achieve PPHs greater than 50 h -1 (ratio of the feed rate to the mass of catalyst), or even greater than 100 h -1.
    [0002] In the context of reactions with high endo or exothermicity, such as gasoline reforming reactions, the reactor according to the invention makes it possible to limit the incidence of this thermicity on the temperature profile inside the reaction zone. Given the impact of the temperature variation within the reactor on the catalytic activity, this is an essential effect on the performance of the unit.
    [0003] The present technology can be considered as an extension of the technology of radial beds used in regenerative reforming. EXAMINATION OF THE PRIOR ART In the prior art relating to radial bed reactors, mention may be made of US Pat. No. 6,221,320, which summarizes conventional technologies. According to the state of the art, the catalytic bed in a radial bed reactor is delimited by two grids, an internal grid and an external grid. More precisely, there are generally: - an internal grid which delimits the central collector of the gaseous effluents, - an external grid which delimits the supply volume of the charge in the gaseous state.
    [0004] The process fluid arrives through the external volume defined between the outer shell and the outer gate. It then passes through the catalytic bed substantially horizontally and perpendicular to the flow of catalyst which is gravitational, that is to say substantially vertical from top to bottom and obtained under the sole effect of the weight of the catalyst bed. The process fluid in radial flow and gravitational flow catalyst are separated by the internal grid which generally has a cylindrical shape with the same substantially vertical axis as the external grid. The cylinder, or more generally the substantially cylindrical shape, defined by the internal grid serves as a central collector to evacuate the gaseous effluents from the reaction zone between the outer gate and the inner gate and therefore of substantially annular shape.
    [0005] 3033265 2 The constraints related to radial bed technology are numerous. In particular, the gas velocities at the crossing of the catalytic bed are limited in order to: - avoid cavitation at the inlet of the bed, - avoid the blockage of the catalyst at its outlet against the internal grid, - reduce the pressure losses depending on the speed and thickness of the bed. For reasons of uniform distribution over the entire height of the catalytic bed, a perforated grid designed to create the pressure drop can be added to the central collector. Finally, for construction reasons, it is often necessary to leave sufficient space between the internal grid and the external grid. Finally, when all the constraints are combined, the minimum volume of catalyst that can be enclosed in the annular zone can not fall below a certain minimum value. In general, according to the prior art, the maximum PPHs are of the order of 20 h -1, whereas the reactor according to the present invention makes it possible to reach PPHs greater than 50 h -1, or even greater than 100 h -1.
    [0006] SUMMARY DESCRIPTION OF THE FIGURES FIG. 1a is a schematic view of a reactor according to the invention with central introduction of the catalyst and lateral evacuation. The angle of the bed with respect to the horizontal is greater than the angle of repose of the catalyst (minimum angle allowing a gravitational flow of the catalyst particles). FIG. 1b shows a schematic view of a reactor according to the invention with another angle of inclination of the catalytic zone and a catalytic bed defined by two concentric cones to control its thickness. FIG. 1c represents another variant of the reactor according to the invention with peripheral introduction of the catalyst and central evacuation. The catalytic bed is also delimited by two concentric cones in order to control its thickness. FIG. 2a shows an exploded view of the reactor according to the invention in the variant of FIG. 1c, which makes it possible to visualize the peripheral introduction legs (8) of the catalyst and the central collection leg (9).
    [0007] FIG. 2b shows the same exploded view as that of FIG. 2a, the reactor being provided with its outer shell (5) which allows the introduction of the reaction gas through the inlet pipe (6) and the recovery of the effluents by the outlet pipe (7). The crossing of the catalytic layer (3) is only along the inclined portion.
    [0008] SUMMARY OF THE INVENTION The present invention can be defined as a gravity flow reactor inclined by the catalyst and having a transverse flow of the feedstock. The term inclined gravitational flow of the catalyst means that it does not flow vertically as in the reactors of the prior art, but at a certain angle of inclination, the only constraint on this angle being that it is greater than the angle called "slope" angle below which a flow of the solid is impossible. By transverse flow of the feed means that the feed passes through the catalytic layer in a direction substantially perpendicular to that of the flow of the catalyst. Said reactor consists of an outer conical wall (1) and an inner conical wall (2), the two walls being substantially parallel to one another, that is to say that the distance separating the two walls and defining the The thickness of the inclined catalytic zone (3) does not vary by more than 1 cm between the upper part and the lower part of said catalytic zone. The tip of the cone formed by the outer and inner walls can be directed upwards or downwards. The inclined catalytic zone (3) is generally preceded by a catalyst distribution zone (4) which is a vertical cylindrical zone of height H between 200 and 1500 mm, preferably between 350 and 700 mm, the catalyst being introduced into said distribution zone (4) by one or more introduction legs (8) and collected at the outlet of the reaction zone (4) by one or more evacuation legs (9). A reactor having the inclined catalytic zone (3) and into which the catalyst is introduced by an introduction leg and collected by a plurality of evacuation legs, as shown in FIGS. 1a and 1b, fits perfectly into the frame of the present invention. The following description is made on a reactor as shown in Figure 1 c. The assembly consisting of the outer conical walls (1) and inner (2), the introduction legs (8), and the evacuation leg or legs (9) being enclosed in a shell (5) comprising an upper part hemispherical (10), a cylindrical central portion (11) and a hemispherical lower portion (12). The charge is admitted inside the shell (5) by an intake manifold (6) located generally at the top of the upper hemispherical part (10), and the reaction effluents are discharged through a lower pipe (7) located generally at the lower portion of the lower hemispherical portion (12).
    [0009] In general, the distance separating the outer (1) and inner (2) conical walls is between 50 and 200 mm, and preferably between 50 and 150 mm. In general, in the context of the present invention, the angle of inclination α of the reaction zone (3) is between 0 ° (excluded) and 70 °, and preferably between 10 ° and 50 °, this angle alpha is spotted in relation to the vertical. In general, in the context of the present invention, the ratio of height to diameter is between 1 and 30, preferably between 1 and 10, and even more preferably between 1 and 5, the height being defined as the sum of the heights. of the distribution zone (4) and the inclined catalytic zone (3), and the diameter as that of the distribution zone (4). The present invention also relates to a process for the catalytic reforming of a gasoline type cut using the previously described reactor. According to this method: the load enters the shell (5) by means of the inlet pipe (6) situated approximately at the top of the upper hemispherical part (10) of the shell (5), the load passes through the catalytic zone sloping (3), and the effluents resulting from the catalytic reaction are collected in the outlet pipe (7) situated approximately at the center of the lower hemispherical portion (12) of the ferrule (5), the catalyst is admitted into the zone vertical distribution (4) by the introduction leg (s) (8), flows through the inclined catalytic zone (3) and is then evacuated by the central outlet leg (s) (9).
    [0010] The process for catalytic reforming of a gasoline type cut according to the invention has a PPH (ratio of the mass flow rate of feed over the weight of catalyst) generally greater than 50 h -1, and preferably greater than 100 h -1. The catalytic reforming process of a gasoline type cut according to the invention can treat fillers having a paraffin content of up to 70% by weight.
    [0011] Finally, the catalytic reforming process of a gasoline type cut according to the invention can even treat an entirely paraffinic filler. The inclined gravity flow reactor according to the present invention is preferably incorporated in a catalytic reforming unit at the head of the series of 3 or 4 reactors constituting said unit. The operating conditions of a regenerative reforming unit of gasolines are typically: an inlet temperature of each reactor of between 480 and 550 ° C., a pressure of each reactor of between 0.9 and 0.5 MPa (1 MPa = 106 Pa). This operating pressure generally decreases as the succession of reactors is monitored from the overhead reactor to the last reactor. DETAILED DESCRIPTION OF THE INVENTION The present invention describes a type of inclined catalytic bed reactor, intended to implement a small amount of catalyst, of the order of one tonne, and which may advantageously constitute the first reactor of the series. in a gasoline catalytic reforming unit which comprises according to the prior art three to four reactors placed in series. More specifically, the reactor according to the present invention is a gravity flow reactor inclined catalyst and transverse flow of the load.
    [0012] Sloped gravitational flow of the catalyst is understood to mean a flow taking place according to the force of gravity and at a certain alpha angle between 0 and 70 ° (this angle alpha is marked with respect to the vertical). The reactor according to the present invention comprises an outer conical wall (1) and an inner conical wall (2), the two walls being substantially parallel to each other.
    [0013] By substantially parallel, it is meant that the distance "e" (according to FIG. 2a) separating the two walls and defining the thickness of the catalytic layer (3) does not vary by more than 1 cm between the upper part and the lower part of the reactor. The tip of the cone formed by the outer (1) and inner (2) walls can be directed upwards or downwards.
    [0014] Preferably, when the tip is pointing downwards (corresponding to FIG. 1c), a plurality of introduction legs (8) and a catalyst discharge leg (9) are used. Likewise, when the tip of the cone formed by the outer (1) and inner (2) walls is directed upwards (corresponding to FIGS. 1a and 1b), an insertion leg (8) is preferably used. ) of the catalyst and a plurality of evacuation legs (9).
    [0015] The following description is made according to the configuration of a catalytic zone (3) with conical walls directed downwards (according to Figure 1c, detailed in Figures 2a and 2b). The inclined catalytic zone (3) is generally preceded by a catalyst distribution zone (4) which is a vertical zone of height H between 200 and 1500 mm, preferably between 350 and 700 mm. This distribution zone allows the catalyst introduced by the introduction legs (8) to be distributed uniformly before entering the inclined reaction zone (3). These introduction legs (8) have a diameter generally between 2 and 4 inches (or between 5.0 cm and 10.2 cm).
    [0016] The inclined catalytic zone (3) terminates in a catalyst outlet pipe (9) which is also called a central drainage leg (9), the diameter of which is generally between 2 and 6 inches (ie between 5 and 0 cm and 7.7 cm). In some cases, there may be several escape legs (9) approximately evenly distributed in a circle. In the following for simplification, we speak of the case of a single evacuation leg (9).
    [0017] In the introduction legs (8), the catalyst distribution zone (4), the inclined catalytic zone (3) and the central discharge leg (9), the flow of the catalyst is always great. The assembly formed by the introduction legs (8), the catalyst introduction zone (4), the inclined catalytic zone (3) and the central discharge leg (9) is enclosed in a ferrule (5). ) having a hemispherical upper portion (10), a cylindrical central portion (11), and a hemispherical lower portion (12). The charge is introduced at the top of the upper hemispherical portion through the inlet manifold (6). The feed passes through the inclined catalytic zone (3) over the entire inclined portion and the reaction effluents are collected by the outlet pipe (7) located in the lower hemispherical portion of the ferrule (5). The thickness of the inclined catalytic zone (3) is between 50 and 200 mm, and preferably between 50 mm and 150 mm. The angle of inclination alpha of the inclined catalytic zone (3) is between 0 and 70 °, and preferably between 10 and 50 °.
    [0018] Among the possible arrangements of the reactor according to the invention can be a central introduction of the catalyst and a peripheral evacuation as shown in Figures 1a and 1b. The invariant element of these different provisions is the existence of the inclined catalytic zone (3).
    [0019] This means that an arrangement of the reactor as shown in FIG. 1a or 1b in which the catalyst is admitted by an upper insertion leg (8) and collected by a plurality of lower collection legs (9). is perfectly within the scope of the present invention.
    [0020] The distribution zone of the catalyst (4) has a height H which depends on the number of introduction legs (8), the angle of flow of the catalyst and the diameter of the ferrule. This height is generally between 200 and 1500 mm, preferably between 350 and 700 mm. Advantageously, the reactor according to the present invention can be used as the overhead reactor in a catalytic reforming process of a gasoline type cut using a series of three or four radial bed reactors. In this case, the flow of the charge and of the catalyst can be described as follows: the charge enters the shell (1) by means of the inlet pipe (6) situated approximately at the top of the hemispherical part upper (10) ferrule (5), - the load passes through the inclined catalytic zone (3), and the effluents resulting from the catalytic reaction are collected in the outlet pipe (7) located approximately in the center of the hemispherical portion lower (12) of the shell (5), 20 - the catalyst is admitted into the vertical distribution zone (4) by the introduction legs (8), flows by gravitational way through the inclined catalytic zone (3) then is evacuated by the central exit leg or legs (9). This catalyst is generally in the form of a spherical ball whose diameter is between 1 and 4 mm, preferably between 1.5 and 2 mm.
    [0021] In a process for the catalytic reforming of a petrol type fraction using the reactor according to the present invention, the PPH (ratio of the feed rate to the weight of catalyst) is greater than 50 h -1, preferably greater than 100 h -1. 1. In a catalytic reforming process of a gasoline type cut using the reactor according to the present invention, the filler can have a paraffin content of up to 70% by weight, and even be a fully paraffinic filler. EXAMPLES The following examples make it possible to illustrate the design of a reactor according to the invention intended to be placed at the head of a regenerative reforming unit treating a feed which is a gasoline cut of flow rate 150 t / h of feedstock. . The term "petrol cut" is usually understood to mean a petroleum fraction with an initial boiling point of about 40 ° C. and a final point of about 220 ° C. Any petroleum fraction that fell within these limits may be perfectly suitable as regenerative reforming feedstock. . 5 - Example 1 represents a reference case not in accordance with the invention, - Example 2 illustrates the performance of a unit provided with a head reactor according to the invention with the same operating conditions and the same total amount of catalyst as in Example 1. - Example 3 illustrates the performance of a unit having the same characteristics as that of Example 2, but treating a more severe load. Example 1 is according to the prior art. In this example, a hydrocarbon feedstock is treated in four reaction zones (or reactors) arranged in series. The distribution of the catalyst in the reactors is as follows: 10% / 20% / 30% / 40% by weight based on the total weight of catalyst. The order in which the reactors follow each other corresponds to the flow of the effluents. The total amount of catalyst is 75 tons. The overall PPH is 2 h-1. Table 1 gives the composition of the hydrocarbon feedstock: initial boiling point 100 ° C, boiling point 170 ° C: Composition Paraffins 50 feed (wt / wt) olefins 0 naphthenes 35 aromatics RON 48.4 Flow rate (t / h) 150 Table 1 The catalyst used in the reactors comprises a chlorinated alumina support, platinum and is promoted with tin. The catalyst particles are spherical with an average diameter of 1.8 mm. The charge heated to 520 ° C. is thus treated successively in the four reactors with an intermediate heating of the effluent at 520 ° C. before it is introduced into the next reaction zone.
    [0022] The operating conditions in the four reaction zones are given in Table 2 below. These conditions were chosen to produce a reformate recovered at the outlet of the fourth reactor whose RON (Research Octane Number according to the English terminology) is equal to 103.5.
    [0023] Reactor 1 Reactor 2 Reactor 3 Reactor 4 Temperature 520 520 520 520 reactor inlet (° C) Pressure (MPa) 0.69 0.65 0.60 0.55 PPH (h-1) 20.0 10.0 6.7 Molar ratio 2.5 H2 / charge (mol / mol) Table 2 Example 2 is according to the invention. The hydrocarbon feed is treated in five reactors arranged in series with a distribution of the following catalyst: 2% / 10% / 20% / 30% / 38% by weight relative to the total weight of catalyst. The small reactor according to the present invention is placed at the head. It is reactor 1 which contains 2% of the total catalyst mass of the unit. The total amount of catalyst is still 75 tons to treat a hydrocarbon feed rate of 150 t / h (overall PPH = 2 h -1). As in Example 1, the feed and effluent from a reaction zone are heated to 520 ° C before entering the reaction zone.
    [0024] The operating conditions in the reaction zones of the reactors are grouped in the following Table 3: Reactor 1 Reactor 2 Reactor 3 Reactor 4 Reactor 5 Temperature 520 520 520 520 520 at the inlet of the reactor (° C) Pressure 0.74 0 , 69 0.65 0.60 0.55 (MPa) PPH (1-1-1) 100.0 20.0 10.0 6.7 5.26 Molar ratio H2 / charge (mol / mol) 2.5 Table 3 The sizing of the first reactor is carried out according to Figures 2a and 2b with the geometric characteristics described in Table 4 below. PPH (h-1) 100 Catalyst volume (m3) 1.74 Alpha cone angle (/ vertical) (°) 20 Thickness of catalyst bed (mm) 150 Ferrule diameter (m) 2.43 Catalyst distribution zone height ( H) (m) 0.5 Total catalyst height HT (m) 3.4 Total reactor height (m) 5.2 Pressure drop of annular reaction zones (Pa) 600 Table 4 Using the small head reactor according to the invention, the temperature drop is limited in the first reaction zone, but also in the other zones 2, 3, 4 and 5. Indeed, the very strong endothermicity related to the first reactions is more easily controlled by the use of a very small amount of catalyst.
    [0025] Because the activity of the catalyst is a function of the average temperature in the catalyst bed, by limiting the temperature drop within the reactor, the yield of aromatics compounds is improved, as shown in Table 5 below. . EXAMPLE 1 Example 2 (not in accordance with the invention) (according to the invention) Overall PPH (h -1) 2 2 PPH (h-1) overhead reactor 100 Yield in reformate (C5 +) 91.2 90, 4 (`) / 0 wt.) Yield of aromatics 74.6 75.8 (`) / 0 wt) RON of reformate 103.5 104.7 5 Table 5 This increase in temperature in the catalytic beds greatly affects the activity of the catalyst. catalyst. For the same amount of catalyst as illustrated below, the gain in aromatic production allows an improvement in RON of 1.2 points.
    [0026] Example 3 illustrates the contribution of the invention to the load severity. A load is all the more severe as its paraffin content is high. According to the approach of the prior art, it is necessary to increase the amount of catalyst or the reactor inlet temperature to maintain the RON of the reformate.
    [0027] Example 3 treats a filler described in Table 6 below, much more severe load than that of Example 1, since very clearly paraffinic. Composition Paraffins Charge (°) / 0 wt.) Olefins 0 Naphthenes 22 Aromatic 15 RON 40.1 Flow rate (t / h) 150 Table 6 3033265 12 Under the same operating conditions as those described in Tables 3 and 4, the RON of Reformat is maintained at 103.5 despite a 13% wt increase in the amount of paraffins in the feed, as shown in Table 7 below. PNA corresponds to the percentage of paraffins (P), naphthenes (N) and aromatics (A).
    [0028] EXAMPLE 1 Example 3 (not in accordance with the invention) (according to the invention) PNA of the feed (`) / 0 wt) 50/35/15 63/22/15 overall PPH (1-1-1) 2 PPH (h-1) of the reactor reactor 100 RON reformat 103.5 103.5 Table 7 The reactor according to the present invention placed at the head of the series of reactors of a catalytic gasoline reforming unit allows therefore to extend the treatment of gasoline cuts to very paraffinic cuts, which is a very important improvement in a context marked by the drastic limitation of the aromatic content in the species.
    权利要求:
    Claims (12)
    [0001]
    CLAIMS1) Reactor inclined gravity flow of the catalyst and transverse flow of the load, said reactor consisting of an outer conical wall (1) and an inner conical wall (2), substantially parallel to each other, the two conical walls being inclined at an angle alpha to the vertical, the tip of the cone being upward or downwardly directed, and the catalyst being introduced into the distribution zone (4) by one or more insertion legs ( 8) and collected at the outlet of the reaction zone (4) by one or more discharge legs (9), the assembly consisting of the outer (1) and inner (2) conical walls, the introduction legs (8). ), and the exhaust legs (9) being enclosed in a shell (5) comprising a hemispherical upper part (10), a cylindrical central part (11), and a hemispherical lower part (12), and the load being admitted at the int the ferrule (5) through an intake manifold (6) at the top of the upper hemispherical portion (10), and the reaction effluents being discharged through a lower manifold (7) at the bottom of the hemispherical portion. lower (12).
    [0002]
    2) inclined gravity flow reactor according to claim 1, wherein the distance between the outer conical walls (1) and inner (2) is between 50 and 200 mm, and preferably between 50 and 150 mm.
    [0003]
    3) inclined gravity flow reactor according to claim 1, wherein the alpha angle of inclination of the reaction zone (3) is between 0 ° (excluded) and 70 °, and preferably between 10 ° and 50 ° ( this alpha angle is marked relative to the vertical).
    [0004]
    4) inclined gravity flow reactor according to claim 1, wherein the ratio height to diameter is between 1 and 30, preferably between 1 and 10, and more preferably between 1 and 5, the height being defined as the sum of the heights of the distribution zone (4) and the inclined catalytic zone (3), and the diameter as that of the distribution zone (4).
    [0005]
    5) inclined gravity flow reactor according to claim 1, wherein the distance separating the two conical walls defining the thickness of the inclined catalytic zone (3) does not vary by more than 1 cm between the upper part and the lower part of said catalytic zone. 3033265 14
    [0006]
    6) inclined gravity flow reactor according to claim 1, wherein the distribution zone of the catalyst (4) is a vertical cylindrical zone of height H between 200 and 1500 mm, preferably between 350 and 700 mm. 5
    [0007]
    7) Catalytic reforming process of a gasoline type cut using the reactor according to one of claims 1 to 6, wherein: the load enters the shell (1) by means of the inlet pipe (6) located Approximately at the top of the upper hemispherical portion of the shell (5), the load passes through the inclined catalytic zone (3), and the effluents resulting from the catalytic reaction are collected in the outlet pipe (7) situated approximately in the center of the lower hemispherical part of the ferrule (5), the catalyst is admitted into the vertical distribution zone (4) by the insertion legs (8), flows through the inclined catalytic zone (3) by gravity and then is evacuated by the central exit leg or legs (9). 20
    [0008]
    8) Catalytic reforming process of a petrol type cut according to claim 7, wherein the PPH (ratio of the feed rate to the weight of catalyst) is greater than 50 h -1, preferably greater than 100 h -1.
    [0009]
    9) A method of catalytic reforming of a gasoline type cut according to claims 7 and 8, wherein the filler has a paraffin content of up to 70% by weight.
    [0010]
    10) Catalytic reforming process of a petrol type cut according to claims 7 and 8, wherein the charge is entirely paraffinic. 30
    [0011]
    11) Catalytic reforming process of a gasoline type cut according to claim 7, wherein the reactor of claim 1 is placed at the head of the series of reactors constituting said method. 35
    [0012]
    12) Catalytic reforming process of a petrol cut according to claim 7, wherein the operating conditions are: - inlet temperature of each reactor between 480 and 550 ° C, - pressure of each reactor between 0.9 and 0.5 MPa (1 MPa = 106 Pa).
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    FR3033265B1|2015-03-04|2017-03-24|Ifp Energies Now|INCLINE BED REACTOR TO IMPLEMENT LOW CATALYST QUANTITIES|FR3033265B1|2015-03-04|2017-03-24|Ifp Energies Now|INCLINE BED REACTOR TO IMPLEMENT LOW CATALYST QUANTITIES|
    CN109569443B|2017-09-28|2021-09-10|中国石化工程建设有限公司|Moving radial bed reactor|
    FR3081167B1|2018-05-17|2020-06-12|IFP Energies Nouvelles|DEVICE FOR LIMITING VORTEX AND SOLID DEPOSITS|
    法律状态:
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    2021-12-10| ST| Notification of lapse|Effective date: 20211105 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1551821A|FR3033265B1|2015-03-04|2015-03-04|INCLINE BED REACTOR TO IMPLEMENT LOW CATALYST QUANTITIES|FR1551821A| FR3033265B1|2015-03-04|2015-03-04|INCLINE BED REACTOR TO IMPLEMENT LOW CATALYST QUANTITIES|
    RU2017130316A| RU2690288C2|2015-03-04|2016-03-02|Reactor with inclined layer, which enables to use small amount of catalyst|
    US15/555,260| US10618022B2|2015-03-04|2016-03-02|Inclined bed reactor permitting a small quantity of catalyst to be employed|
    PCT/EP2016/054428| WO2016139247A1|2015-03-04|2016-03-02|Inclined-bed reactor allowing the use of a small quantity of catalyst|
    BR112017015912-0A| BR112017015912B1|2015-03-04|2016-03-02|SLOPE GRAVITANT FLOW REACTOR AND CATALYTIC REFORM PROCESS OF A PETROL TYPE CUTTING|
    EP16707742.9A| EP3265223B1|2015-03-04|2016-03-02|Inclined-bed reactor allowing the use of a small quantity of catalyst|
    CN201680013591.3A| CN107405592B|2015-03-04|2016-03-02|Inclined bed reactor allowing the use of small amounts of catalyst|
    TW105106777A| TW201703853A|2015-03-04|2016-03-04|Inclined bed reactor permitting a small quantity of catalyst to be employed|
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