WO2016091489A1 - Reacteur a lit radial permettant de mettre en œuvre de faible quantite de catalyseur - Google Patents
Reacteur a lit radial permettant de mettre en œuvre de faible quantite de catalyseur Download PDFInfo
- Publication number
- WO2016091489A1 WO2016091489A1 PCT/EP2015/075738 EP2015075738W WO2016091489A1 WO 2016091489 A1 WO2016091489 A1 WO 2016091489A1 EP 2015075738 W EP2015075738 W EP 2015075738W WO 2016091489 A1 WO2016091489 A1 WO 2016091489A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- module
- catalyst
- reactor
- ferrule
- modules
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/10—Catalytic reforming with moving catalysts
- C10G35/12—Catalytic reforming with moving catalysts according to the "moving-bed" method
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
- B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
- B01J23/626—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with tin
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/06—Catalytic reforming characterised by the catalyst used
- C10G35/085—Catalytic reforming characterised by the catalyst used containing platinum group metals or compounds thereof
- C10G35/09—Bimetallic catalysts in which at least one of the metals is a platinum group metal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Definitions
- the invention relates to the radial bed reactor technology with gravity circulation of catalyst and transverse 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 implement very small amounts of catalyst according to a radial bed technology, a feature which is not possible 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).
- the catalytic bed in a radial bed reactor is delimited by two grids, an internal grid and an external grid. More specifically, we generally distinguish:
- the process fluid in radial flow and gravitational flow catalyst are separated by the internal grid which generally has a cylindrical shape of the same substantially vertical axis as the external grid.
- the cylinder 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.
- US 4,441 1,870 discloses a reactor containing a plurality of reaction chambers, each of these chambers having an annular zone for the catalyst and the feed being distributed in the different reaction zones so as to achieve a uniform flow of reactants in the reaction zone. the different areas. This document does not provide any information on the geometric characteristics of said reaction zones.
- Figure 1a shows an exploded view of the shell (1) of the reactor according to the invention, but not containing a module (M), so as to clearly view the floor (13) which supports said modules.
- FIG. 1b is an exploded view of the reactor according to the invention in which we can see the modules (M) and their connection with the upper part of the ferrule (1), as well as the inlet legs of the catalyst (10) and the extraction legs (1 1).
- FIG. 2a shows a section of the reactor in a view from above making it possible to see the modules (M), the catalytic zone of each module (4) and the external (2) and internal grids (3) defining said catalytic zone.
- FIG. 2b shows a section of the reactor in side view making it possible to visualize the inlet of the charge (8) and the outlet of the effluents (12) as well as the volume (9) of distribution of the charge on all the modules (M) and the lower volume (7) for collecting the effluents from each module (M).
- FIG. 2c represents a module (M) in side view and makes it possible to clearly understand the corresponding entity within the reactor.
- the present invention describes a type of radial bed reactor, intended to implement a small amount of catalyst of the order of one tonne and which may advantageously be the first reactor of the series in a catalytic reforming unit of the gasolines which comprises according to the prior art, three to four reactors placed in series.
- This reactor can be called modular in the sense that it consists of a set of identical modules operating in parallel and enclosed in a single ferrule.
- the reactor according to the present invention is a reactor with a radial flow of the charge and with a gravity flow of the catalyst consisting of a set of substantially identical modules (M) enclosed in a single shell (1), having means for introduction of the catalyst (10) located in the upper part, and means for discharging said catalyst (1 1) located in the lower part (7), and means for introducing the load by an upper central tube (8) and means for discharging the effluents through a lower central pipe (12), each module having a cylinder defined by a substantially vertical outer wall (2) and a substantially vertical inner wall (5), the combination of the two walls defining an annular zone (4) containing the catalyst, and the outer (2) and inner (5) walls of each module being permeable to the gas charge and the gas effluents, and being generally constituted said modules being positioned vertically in a generally symmetrical manner with respect to the center of the ferrule (1), and the effluent outlets of each module being made by the central collector (3) of each module which communicates with the lower part
- modules within the ferrule (1) there may be mentioned alignments of said modules according to several concentric circles. In general, whatever the particular arrangement of the modules within the shell, they are distributed approximately symmetrically with respect to the center of the shell (1).
- the modules (M) are distributed regularly inside the shell in a circle.
- the reactor according to the present invention has a number of modules between 3 and 12, and very preferably between 5 and 10.
- the reactor according to the present invention has, for each module (M), a height-to-diameter ratio of between 3 and 30, and very preferably of between 7 and 11.
- this reactor can be used as the head reactor in a catalytic reforming process of a gasoline type cut using a series of three or four radial bed reactors.
- the flow of the feedstock and the catalyst can be described as follows:
- the charge enters the shell (1) by means of the inlet pipe (8) located in the upper part of the reactor and then occupies the internal volume (9) from which it enters the inside of each module (M ) by passing through the outer gate of said module (2),
- the catalyst is admitted into each module via an intake manifold (10) and flows in the annular zone (4) of each module in a gravitational manner and is then discharged from the module via an outlet pipe (1 1).
- the PPH ratio of the feed rate to the weight of catalyst
- the filler can have a paraffin content of up to 70% by weight, and even be an entirely paraffinic filler.
- the invention essentially consists in producing a set of radial "modules" of small sizes allowing higher PPHs to be achieved than in traditional reactors, all of these modules being enclosed in a single shell.
- FIG. 1a represents the reactor in exploded view and without module, so as to clearly visualize the outer shell (1) and of FIG. 1b which represents the reactor in an exploded view containing the modules.
- FIGS. 2a and 2b show a reactor viewed from above (FIG. 2a) and from the side (FIG. 2b).
- the load enters the shell (1) by means of the tubing (8) located in the upper part.
- the charge then occupies the internal volume (9) from which it enters the interior of each module through the outer gate of said module (2).
- the charge passes through the catalytic bed contained in the annular zone (4) of each module and the effluents resulting from the catalytic reaction are collected in the central collector (3) of each module.
- the effluents of each module are grouped in the lower volume (7) of the ferrule (1).
- the internal volume (9) and the lower volume (7) are separated by a floor (13) which is sealed between the two volumes and which also supports the modules (M).
- the catalyst is admitted into each module through an intake manifold (10). It flows by gravity into the annular zone (4) of each module, then is evacuated from the module by an outlet pipe (1 1). There is at least one intake manifold (10) and one outlet manifold (1 1) per module.
- the modules have the shape of cylinders delimited by a substantially vertical outer wall (2) and a substantially vertical inner wall (5), all of the two walls defining an annular zone (4) containing the catalyst.
- the outer (2) and inner (5) walls of each module are permeable to the feedstock and the gas effluents, and generally consist of Johnson gate or other equivalent means.
- These modules are positioned in a single shell (1) which serves as a volume for the supply of process gas through the upper part (6) and the evacuation of effluents.
- the effluents from each catalytic zone are then collected in a common volume (7) located at the lower part of the ferrule (1).
- the modules make it possible to produce catalytic beds with very small thicknesses, which considerably reduces the pressure drop constraints.
- the height to diameter ratio of each module is generally between 3 and 30, preferably between 7 and 11.
- the PPH (ratio of the feed rate to the weight of catalyst) is generally greater than 50 h -1, preferably greater than 100 h -1.
- the centers of each module are advantageously positioned along a circle, as shown by way of example in FIG. 2a for a reactor containing 6 identical modules.
- the number of modules is generally between 3 and 12, preferably between 5 and 10.
- the central collectors (3) of each module communicate with the same volume (7) located at the lower part of the shell (1) which allows the evacuation of the effluent through the outlet pipe (12).
- tie rods (6) for holding the modules (M) placed on the plate (13).
- This plate (13) is sealed to prevent mixing of the load contained in the upper volume (9) with the effluent collected in the lower volume (7).
- Said plate (13) is supported by pillars and reinforcing beams to support the weight of the modules (filled with catalyst).
- Each module (M) has a fixing plate to the plate (13), this fixing can be performed by any means known to those skilled in the art.
- the reactor also makes it possible to inspect visually through a manhole, the reactor once assembled, especially for external grids, and internal grids, at least in part.
- the paralleling of several modules also makes it possible to consider condemning one in case of failure, while continuing to operate the system on the remaining modules.
- the proposed system thus allows the achievement of high PPH objectives to optimize the reaction performance of the process, while providing a realistic mechanical concept, flexible, flexible and easy maintenance.
- Example 1 represents the reference case not in accordance with the invention
- Example 2 represents the performance of a unit according to the invention provided with a head reactor 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 dealing with a more severe load.
- Example 1 a hydrocarbon feed is treated in four reaction zones arranged in series in four reactors.
- the distribution of the catalyst in the reactors is as follows: 10% / 20% / 30% / 40% by weight relative to the total weight of catalyst.
- the total amount of catalyst is 75 tons.
- Table 1 gives the composition of the hydrocarbon feedstock:
- the catalyst used in the reactors comprises a chlorinated alumina support, platinum and is promoted with tin.
- the charge heated to 514 ° C. is thus treated successively in the four reactors with an intermediate heating of the effluent at 514 ° C. before being introduced into the next reaction zone.
- Example 2 corresponds to Example 1 except that 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 with respect to total weight of catalyst.
- the small reactor according to the present invention is placed at the head. It is the reactor 1.
- the total amount of catalyst is 75 tonnes to treat a hydrocarbon feed rate of 150 t / h.
- Example 1 the feed and effluent from one reaction zone are heated to 514 ° C before entering the next reaction zone.
- the dimensioning of the first reactor is carried out according to FIGS. 1 and 2 with the geometrical characteristics described in Table 4.
- Example 3 illustrates the contribution of the invention from the point of view of the severity of charge. A load is all the more severe as its paraffin content is high. With an identical approach to the previous state, it is necessary to increase the amount of catalyst or the reactor inlet temperature to maintain the RON of the reformate. Example 3 is intended to treat a filler as described in Table 6, much more severe load than that of Example 1.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BR112017009987-0A BR112017009987B1 (pt) | 2014-12-08 | 2015-11-04 | Reator com escoamento radial da carga e com escoamento gravitante do catalisador e processo de reforma catalítica de uma mistura de tipo gasolina |
US15/533,660 US10323194B2 (en) | 2014-12-08 | 2015-11-04 | Radial bed reactor allowing the use of a small quantity of catalyst |
CN201580066793.XA CN107427804B (zh) | 2014-12-08 | 2015-11-04 | 允许使用少量催化剂的径向床反应器 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1462077A FR3029429B1 (fr) | 2014-12-08 | 2014-12-08 | Reacteur a lit radial permettant de mettre en œuvre de faible quantite de catalyseur |
FR1462077 | 2014-12-08 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2016091489A1 true WO2016091489A1 (fr) | 2016-06-16 |
Family
ID=52589577
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2015/075738 WO2016091489A1 (fr) | 2014-12-08 | 2015-11-04 | Reacteur a lit radial permettant de mettre en œuvre de faible quantite de catalyseur |
Country Status (6)
Country | Link |
---|---|
US (1) | US10323194B2 (fr) |
CN (1) | CN107427804B (fr) |
BR (1) | BR112017009987B1 (fr) |
FR (1) | FR3029429B1 (fr) |
TW (1) | TW201627061A (fr) |
WO (1) | WO2016091489A1 (fr) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10478794B1 (en) * | 2019-02-26 | 2019-11-19 | Chevron Phillips Chemical Company Lp | Bi-modal radial flow reactor |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4411870A (en) | 1981-12-28 | 1983-10-25 | Uop Inc. | Reactor system |
US6221320B1 (en) | 1990-10-03 | 2001-04-24 | Nagaoka International Corporation | Device and method for holding catalyst in a radial flow reactor |
FR2922124A1 (fr) * | 2007-10-10 | 2009-04-17 | Inst Francais Du Petrole | Reacteur en lit fixe a couches minces pour le traitement chimique de solide catalytique finement divise |
FR2948580A1 (fr) * | 2009-07-29 | 2011-02-04 | Inst Francais Du Petrole | Dispositif de distribution de la charge et de recuperation des effluents dans un reacteur catalytique a lit radial |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6059961A (en) * | 1998-04-27 | 2000-05-09 | Uop Llc | Method to alleviate thermal cycles in moving bed radial flow reactor |
US8101133B2 (en) * | 2010-02-25 | 2012-01-24 | Praxair Technology, Inc. | Radial flow reactor |
US8313561B2 (en) * | 2010-10-05 | 2012-11-20 | Praxair Technology, Inc. | Radial bed vessels having uniform flow distribution |
-
2014
- 2014-12-08 FR FR1462077A patent/FR3029429B1/fr active Active
-
2015
- 2015-11-04 WO PCT/EP2015/075738 patent/WO2016091489A1/fr active Application Filing
- 2015-11-04 BR BR112017009987-0A patent/BR112017009987B1/pt active IP Right Grant
- 2015-11-04 CN CN201580066793.XA patent/CN107427804B/zh active Active
- 2015-11-04 US US15/533,660 patent/US10323194B2/en active Active
- 2015-12-04 TW TW104140829A patent/TW201627061A/zh unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4411870A (en) | 1981-12-28 | 1983-10-25 | Uop Inc. | Reactor system |
US6221320B1 (en) | 1990-10-03 | 2001-04-24 | Nagaoka International Corporation | Device and method for holding catalyst in a radial flow reactor |
FR2922124A1 (fr) * | 2007-10-10 | 2009-04-17 | Inst Francais Du Petrole | Reacteur en lit fixe a couches minces pour le traitement chimique de solide catalytique finement divise |
FR2948580A1 (fr) * | 2009-07-29 | 2011-02-04 | Inst Francais Du Petrole | Dispositif de distribution de la charge et de recuperation des effluents dans un reacteur catalytique a lit radial |
Also Published As
Publication number | Publication date |
---|---|
BR112017009987A2 (pt) | 2018-01-02 |
FR3029429A1 (fr) | 2016-06-10 |
TW201627061A (zh) | 2016-08-01 |
FR3029429B1 (fr) | 2018-07-27 |
US10323194B2 (en) | 2019-06-18 |
BR112017009987B1 (pt) | 2021-06-01 |
CN107427804A (zh) | 2017-12-01 |
CN107427804B (zh) | 2020-12-01 |
US20170313950A1 (en) | 2017-11-02 |
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