US20100252482A1 - Reactor and process for endothermic gas phase reactions on a solid catalyst - Google Patents

Reactor and process for endothermic gas phase reactions on a solid catalyst Download PDF

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US20100252482A1
US20100252482A1 US12/746,249 US74624908A US2010252482A1 US 20100252482 A1 US20100252482 A1 US 20100252482A1 US 74624908 A US74624908 A US 74624908A US 2010252482 A1 US2010252482 A1 US 2010252482A1
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reactor
zone
catalytic
exchange
section
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Gilles Ferschneider
Beatrice Fischer
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IFP Energies Nouvelles IFPEN
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    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • B01J8/0423—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
    • B01J8/0438—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds the beds being placed next to each other
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • 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
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    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2208/00017—Controlling the temperature
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    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2208/00504—Controlling the temperature by means of a burner
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    • B01J2208/00707—Fouling
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2208/00814—Details of the particulate material the particulate material being provides in prefilled containers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • 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
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/021—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles comprising a plurality of beds with flow of reactants in parallel
    • B01J2208/022—Plate-type reactors filled with granular catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
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    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/2476—Construction materials
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas

Definitions

  • the present invention relates to a reactor which can recover heat from pressurized combustion gas and use it for reactions.
  • Heavy gasoline cuts principally comprising C 6 to C 10 hydrocarbons deriving from the initial distillation of oil is normally processed to bring their octane number to a high value for use in an automotive vehicle engine.
  • a second unwanted reaction is coking of the catalyst, which reduces the activity of the catalyst and necessitates its periodic regeneration by burning the coke to re-establish its activity. Cracking is greater with increased pressure. Thus, the yields are better at low pressure. However, coking is higher with a lower partial pressure of hydrogen.
  • Old units operated at high pressure (approximately 15 to 30 bars), with a high hydrogen recycle ratio, giving mediocre yields, and could operate for approximately 11 months before the catalyst had to be regenerated.
  • Continuous catalyst regeneration units can regenerate all of a catalyst in a few days, to allow low pressure operation (approximately 3 to 5 bars), and thus increase the yields.
  • the catalyst moves continuously in the reactors, which are thus radial in type, and is sent to a regeneration section in order to be regenerated before being returned to the first reactor.
  • Dehydrogenation reactions are highly endothermic and the reactions stop when the temperature is too low.
  • Current processes generally comprise three or four reactors and as many furnaces in series. Each furnace is followed by a reactor. Because of the high temperatures, the furnace yields are low and it is normal to produce steam to improve the overall yield of the furnace. It is also normal to use that steam to actuate a turbine which drives the recycle compressor and the hydrogen exportation compressor.
  • the invention concerns a reactor for catalytic reforming or for hydrocarbon dehydrogenation, having a cylindrical shape along a vertical axis, an upper head and a lower bottom, comprising at least two annular zones centred on the vertical axis, said two annular zones being a zone termed a catalytic zone and a zone termed the exchange zone.
  • Vertical hermetic panels divide the reactor into sectors, said sectors each comprising at least one exchange section and at least one catalytic section, the ensemble of said exchange sections forming the exchange zone and the ensemble of said catalytic sections forming the catalytic zone.
  • the invention also concerns the process using the reactor of the invention.
  • the present invention In order to heat the reactor, preferably a reforming reactor, the present invention generally employs pressurized combustion gases which means that electricity can be produced for the catalytic reforming unit, and possibly for other units.
  • pressurized combustion gases which means that electricity can be produced for the catalytic reforming unit, and possibly for other units.
  • a single reactor is generally used, with special internal means which mean that the sections for heating by exchange with the combustion gas can be alternated with the adiabatic catalytic sections, with the catalyst being able to move in the reactor under gravity. The overall footprint of the unit, the amount of equipment and the cost of the reaction section are thus reduced.
  • Each reactor is then generally supplied by a dedicated air compressor and a dedicated burner.
  • the invention concerns a reactor for carrying out an endothermic gas phase reaction in the gas phase, having a cylindrical shape along a vertical axis and comprising:
  • At least four annular zones centred on the vertical axis are in succession from the edge towards the centre of the reactor, namely a first zone 201 termed the supply zone, a second zone 202 termed the catalytic zone, a third zone 203 termed the collection zone and a fourth zone 204 termed the exchange zone.
  • the vertical hermetic panels 65 dividing the reactor into sectors are fixed along a central cylindrical zone 205 .
  • the sectors each comprise an exchange section 61 , a catalytic section 62 , a supply section 161 and a collection section 162 , the ensemble of said exchange sections forming the exchange zone 204 , the ensemble of said catalytic sections forming the catalytic zone 202 , the ensemble of said supply sections forming the supply zone 201 and the ensemble of said collection sectors forming the collection zone 203 ,
  • the reactor comprises an upper head and a lower bottom.
  • At least one pipe 163 per section generally passes through the upper head of the reactor to supply the catalytic sections with catalyst and at least one pipe 263 per section passes through the lower bottom of the reactor to evacuate catalyst from the catalytic sections.
  • a supply conduit 17 passing through the upper head of the reactor can supply a sector, denoted the first sector, with reaction mixture
  • an evacuation conduit 18 passing through the upper head of the reactor can evacuate reaction mixture from the last sector of the reactor.
  • a conduit 67 which connects the collection zone of the last sector to the conduit 18 in order to evacuate the reaction mixture is generally present.
  • an inlet conduit 6 passing through the lower bottom of the reactor is connected to conduits 70 leading to tubular chambers 71 .
  • tubular chambers distribute combustion gas by means of tubular plates 69 via the bottom of the reactor into each exchange section.
  • Tubular chambers 72 can collect combustion gas from the top of each exchange section, then conduits 73 provided with expansion bellows 74 can evacuate the combustion gas towards the outlet conduit 7 which passes through the upper head of the reactor.
  • Each exchange section is generally constituted by tubular exchangers or plate exchangers. Each exchange section has either an identical surface area, or the exchange surface area increases from the first to the last exchange section.
  • Each catalytic section is generally formed by two concentric metal screens, preferably of the “Johnson screen” type. All of the catalytic sections generally have the same dimensions or the dimensions of the catalytic sections increase from the first to the last sector.
  • the vertical hermetic panels 65 generally divide the reactor into 3, 4, 6 or 8 sectors, preferably into 4 or 6 sectors.
  • the invention also concerns the process for carrying out a catalytic reforming reaction or hydrocarbon dehydrogenation reaction in a reactor in accordance with the invention.
  • the invention also concerns a process for carrying out an endothermic gas phase catalytic reforming or hydrocarbon dehydrogenation reaction over a solid catalyst in a reactor in accordance with the highly preferred embodiment of the invention, in which the reaction mixture enters the reactor via the conduit 17 then moves from top to bottom in the first exchange section 61 . Said reaction mixture then passes under the first catalytic section 62 between the catalyst down pipes 263 , then passes radially through the first catalytic section 62 , passing from the supply zone 201 to the collection zone 203 of the reactor, passes to the exchange section of the second sector via the conduit 64 . Finally, the reaction mixture moves in succession and in alternating manner in the next exchange sections and the next catalytic sections.
  • the catalyst generally moves from top to bottom at the same speed in all the catalytic sections.
  • the catalyst can move from top to bottom at a speed which increases from the first to the last catalytic section.
  • the invention also concerns the process in which the pressurized combustion gas heats the reaction mixture by indirect heat exchange.
  • the combustion gas supplying the reactor 60 via the conduit 6 derives from heating air at atmospheric pressure moving via line 1 to an air compressor 2 then via the line 3 towards a combustion chamber 4 in which burning a fuel gas moving via 5 can heat the combustion gas to a temperature in the range 600° C. to 800° C., preferably in the range 650° C. to 750° C.
  • the combustion gas supplying the reactor 60 via the conduit 6 derives from heating air at atmospheric pressure moving via the line 1 towards an air compressor 2 then via the line 3 towards a combustion chamber 4 in which burning of a fuel gas moving via the line 5 can heat the combustion air which then passes via an expansion turbine 12 which is on the same shaft as the air compressor and which provides the power necessary for compression;
  • the combustion gas leaving the expansion turbine 12 is at a pressure in the range 0.2 to 0.45 MPa, and at a temperature in the range 600° C. to 800° C., and preferably in the range 650° C. to 750° C.
  • the combustion gas leaving the reactor via the conduit 7 can be reheated in a combustion chamber 8 before being sent to a turbo-expander 10 to produce electricity.
  • FIG. 1 describes one of the ways of providing heat to the reactor. Atmospheric air is supplied via a line 1 to an air compressor 2 . The air is compressed to a pressure close to 4 bars absolute (0.4 MPa) and is then sent via a line 3 to a combustion chamber 4 . A fuel gas is supplied via a line 5 for burning in the combustion chamber 4 . The depleted air which has been heated by combustion at a temperature of close to 700° C. is sent via a line 6 to the reactor 60 .
  • the reaction mixture enters via a line 17 and leaves via a line 18 .
  • the combustion gas cools by exchange with the reaction mixture which is undergoing an endothermic catalytic reforming reaction.
  • the cooled gas is sent via a line 7 to a second combustion chamber 8 where it is reheated by combustion of fuel gas supplied via a line 9 .
  • the hot gas is sent at a temperature close to 750° C. to a turbo-expander 10 which drives an alternator 11 to produce electricity.
  • FIG. 2 describes an alternative manner of supplying heat to the reactor 60 .
  • Atmospheric air is supplied via line 1 to air compressor 2 . Air compressed to a pressure of close to 20 bars is then sent via line 3 to combustion chamber 4 .
  • a fuel gas is supplied via line 5 for burning in the combustion chamber 4 .
  • the depleted air which has been heated by combustion to a temperature of close to 1300° C. is sent to a turbo-expander 12 which drives the air compressor 2 .
  • the gas at the turbine outlet is at about 3 bars and at a temperature of close to 700° C. It is sent via line 6 to reactor 60 .
  • the reaction mixture enters via a line 17 and leaves via a line 18 .
  • the combustion gas cools by exchange with the reaction mixture which is undergoing an endothermic catalytic reforming reaction.
  • the cooled gas is sent via line 7 to a second combustion chamber 8 where it is reheated by combustion of fuel gas supplied via line 9 .
  • the hot gas is sent at a temperature of close to 750° C. to a turbo-expander 10 which drives an alternator 11 to produce electricity.
  • FIG. 3 describes a variation of FIG. 1 in which heat is recovered from hot gases moving via a line 40 at the outlet from the turbine 10 .
  • the exchanger 41 can recover heat either:
  • the effluent gasoline from the exchanger 41 moves via a line 42 .
  • FIG. 4 shows the reaction section of a catalytic reforming section in accordance with the invention.
  • the combustion gas enters the reactor 60 via line 6 and leaves via line 7 .
  • the feed arrives at a feed pump 15 via a line 14 .
  • the feed is sent from the pump outlet via a line 16 to the heat exchanger 19 which is preferably of the Packinox type.
  • the recycle gas which moves via a line 26 is also sent to said exchanger 19 for mixing with the feed moving via the line 16 in the exchanger and heated to a temperature close to 440° C. by exchange with the reaction mixture leaving the reactor 60 via line 18 .
  • the reaction mixture is sent to the reactor 60 via line 17 .
  • the reaction mixture leaving the reactor via line 18 is at about 490° C. and is sent to the top of the heat exchanger 19 where it is cooled to about 100° C.
  • the effluent is sent via the line 20 to a heat exchanger 21 , where it is cooled by heat exchange with air or cooling water.
  • the cooled and partially condensed effluent is sent via a line 22 to a separator tank 23 .
  • the liquid from the tank is withdrawn via a line 28 to a stabilization section.
  • Part of the gas phase from the separator tank 24 principally constituted by hydrogen, is used to constitute a gas recycle, compressed by compressor 25 then moving via line 26 , the remainder being sent to a purification section via a line 27 .
  • FIGS. 5 , 6 , 7 and 8 show different sections of a preferred version of the reactor.
  • FIG. 5 diagrammatically shows the reactor 60 in cross sectional side view.
  • a first zone (visible in FIG. 6 , reference numeral 201 ) termed the supply zone
  • a second zone (visible in FIG. 6 as reference numeral 202 ) termed the catalytic zone
  • a third zone (visible in FIG. 6 as reference numeral 203 ) termed the collection zone
  • a fourth zone (visible in FIG. 6 as reference numeral 204 ) termed the exchange zone.
  • Vertical hermetic panels (visible in FIG. 6 as reference numeral 65 ) are fixed on the cylindrical central zone (visible in FIG. 6 as reference numeral 205 ) and divide the reactor into sectors.
  • Each sector comprises an exchange section 61 and a catalytic section 62 .
  • the ensemble of the exchange sections forms the exchange zone 204 and the ensemble of the catalytic sections forms the catalytic zone 202 .
  • Each sector comprises a supply section 161 and a collection section 162 .
  • the ensemble of supply sections forms the supply zone 201 and the ensemble of collection sections forms the collection zone 203 .
  • combustion gas moves from bottom to top in the reactor.
  • Combustion gas is supplied via the bottom of the reactor via the inlet conduit 6 then is distributed into each exchange section via conduits 70 then via tubular chambers 71 before being distributed via tubular plates 69 into tubes 99 .
  • the combustion gas is collected from the top of the reactor in tubular chambers 72 then sent via conduits 73 provided with expansion bellows 74 to the outlet conduit 7 .
  • the reaction mixture passes through all the sectors in succession.
  • the reaction mixture enters via the conduit 17 and at the collection section of the last sector, it is collected via the conduit (visible in FIG. 6 as reference numeral 67 ) then leaves the reactor via the conduit 18 .
  • reaction mixture comprising hydrogen and hydrocarbons
  • the pressure at the reactor inlet is approximately 4 bars.
  • the reaction mixture enters the exchange zone of the first sector via the inlet 66 (see arrow 101 ). In this first sector, the reaction mixture heats up while dropping (arrow 102 ) as a counter current to the combustion gas and leaves the first exchange section via the outlet 75 .
  • the gas passes below the catalytic section 62 (arrow 103 ) between the catalyst down pipes 263 , rises along the shell and passes through the catalytic section 62 (arrows 104 ).
  • the reaction mixture reacts and cools very rapidly on the catalyst as the naphthenes present in the feed react very rapidly and in a highly endothermic manner.
  • the temperature is generally less than 400° C. at the outlet from the first catalyst section.
  • the reaction mixture is then evacuated from the first section at the top of the reactor and sent to the second section via a conduit (visible in FIG. 6 , numeral 64 ).
  • the reaction mixture is heated up again in the exchange section of the second sector then cooled, reacting in the catalytic section of the second sector.
  • reaction mixture is collected by the conduit (visible in FIG. 6 , reference numeral 67 ) then sent to the outlet conduit 18 .
  • FIG. 6 shows the reactor viewed from the top and in section.
  • Vertical hermetic panels 65 are fixed on the central cylindrical zone 205 and divide the reactor into 8 sectors.
  • the conduits 64 allow passage from one sector to another.
  • the reaction mixture enters the first exchange section via the inlet 66 .
  • the reaction mixture is collected via the conduit 67 .
  • FIG. 7 represents a sector viewed from the centre of the reactor, with the two connected exchange sections 61 in the foreground, the tubular plate 69 and the catalytic section 62 in the background, with the catalyst down pipes 163 and 263 and the closing plates 68 .
  • FIG. 8 shows the same sector viewed from the shell, with the exchange section 61 in the background, the catalytic section 62 in the foreground, the exchange section outlet 75 , the passage 64 from one sector to another and a closing plate 68 .
  • the feed was a 90-170° C. cut with a paraffins content of 60% by volume, a naphthenes content of 25% by volume and an aromatics content of 15% by volume.
  • the pure hydrogen/feed molar ratio was 2.5.
  • the target octane number was 102.
  • the whole catalyst was regenerated continuously in 2.5 days.
  • the reaction mixture arrived at the reactor at 450° C. from the Packinox feed-effluent exchanger. It was heated up by exchange with the hot fumes from the first sector and arrived in the catalyst of the first sector at 486° C. and was then sent to the second sector where it was heated up before being supplied to the second sector.
  • the combustion gas left the reactor at 469° C. after having given up 88.198 million KJ/h (21.1 MM Kcal/h) to the reaction mixture.
  • the effluent combustion gas was sent to a second combustion chamber where 2560 kg/h of fuel gas was burned in order to reach 760° C. at a pressure of 3.4 bars absolute at the inlet to an expansion turbine.
  • This turbine had a polytropic efficiency of 85% and provided approximately 26 MW of electrical power which could drive the air compressor and supply sufficient electricity for the catalytic reforming and pre-treatment units.
  • the gaseous effluent was at a temperature of 526° C. which meant that either more electricity could be produced by generating steam, or a heat transfer fluid could be re-heated, which could reboil the columns of the process (the stripping column for pre-treatment and stabilization of reforming).
  • tubular exchangers to simplify the calculations, but the scope of the invention also encompasses using other types of exchanger, for example Packinox type welded plate exchangers, which could result in a much more compact configuration.
  • the catalyst was installed in an annular zone with an internal diameter of 3.2 m and over a height of close to 14 m. There were 35 tonnes of catalyst, i.e. about 50 m 3 , and thus 3.6 m 2 of catalytic zone (50/14). The external diameter of the annular catalytic zone was thus 3.85 m.
  • the amount of coke produced was very small in the first sector and increased from sector to sector, being highest in the last sector (8% of coke if the catalyst moved in that sector for 2.5 days).
  • One solution is to circulate the catalyst at the same rate throughout, to mix the catalyst at the reactor outlet in order to send it to the regenerator and to regenerate it as a mixture, the mean coke content then being only approximately 4%, thus allowing safe regeneration.

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US12/746,249 2007-12-06 2008-12-01 Reactor and process for endothermic gas phase reactions on a solid catalyst Abandoned US20100252482A1 (en)

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FR0708560 2007-12-06
FR0708560A FR2924624B1 (fr) 2007-12-06 2007-12-06 Reacteur et procede pour les reactions endothermiques en phase gazeuse sur catalyseur solide
PCT/FR2008/001675 WO2009101280A1 (fr) 2007-12-06 2008-12-01 Reacteur et procede pour les reactions endothermiques en phase gazeuse sur catalyseur solide

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US10661242B2 (en) 2017-03-01 2020-05-26 IFP Energies Nouvelles Low-capacity compartmentalized reactor

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FR3103714B1 (fr) * 2019-11-28 2021-12-03 Commissariat Energie Atomique Reacteur tubulaire a lit fixe
FR3114520B1 (fr) * 2020-09-29 2022-08-26 Commissariat Energie Atomique Reacteur tubulaire a lit fixe
FR3114519B1 (fr) * 2020-09-29 2022-08-26 Commissariat Energie Atomique Reacteur tubulaire a lit fixe

Citations (4)

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Publication number Priority date Publication date Assignee Title
US3907665A (en) * 1972-10-26 1975-09-23 Universal Oil Prod Co Dehydrogenation process
US4071325A (en) * 1976-08-16 1978-01-31 National Distillers And Chemical Corporation Ethylene polymerization reactor
US4681701A (en) * 1985-08-30 1987-07-21 Shell Oil Company Process for producing synthesis gas
US20040018124A1 (en) * 2001-10-04 2004-01-29 Ermanno Filippi Heterogeneous catalytic reactor with a modular catalytic cartridge

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JP2001038195A (ja) * 1999-06-28 2001-02-13 Basf Ag 熱交換板を備えた反応器
EP1153653A1 (fr) * 2000-05-11 2001-11-14 Methanol Casale S.A. Réacteur pour des réactions exothermiques ou endothermiques

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3907665A (en) * 1972-10-26 1975-09-23 Universal Oil Prod Co Dehydrogenation process
US4071325A (en) * 1976-08-16 1978-01-31 National Distillers And Chemical Corporation Ethylene polymerization reactor
US4681701A (en) * 1985-08-30 1987-07-21 Shell Oil Company Process for producing synthesis gas
US20040018124A1 (en) * 2001-10-04 2004-01-29 Ermanno Filippi Heterogeneous catalytic reactor with a modular catalytic cartridge

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10661242B2 (en) 2017-03-01 2020-05-26 IFP Energies Nouvelles Low-capacity compartmentalized reactor

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TW200940171A (en) 2009-10-01
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SA108290772B1 (ar) 2013-04-30
WO2009101280A1 (fr) 2009-08-20
FR2924624B1 (fr) 2009-11-20
FR2924624A1 (fr) 2009-06-12

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