WO2003043727A1 - Reacteur chimique modulaire - Google Patents

Reacteur chimique modulaire Download PDF

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Publication number
WO2003043727A1
WO2003043727A1 PCT/EP2001/013362 EP0113362W WO03043727A1 WO 2003043727 A1 WO2003043727 A1 WO 2003043727A1 EP 0113362 W EP0113362 W EP 0113362W WO 03043727 A1 WO03043727 A1 WO 03043727A1
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WO
WIPO (PCT)
Prior art keywords
shell
reactor
tubular portion
catalytic
chemical reactor
Prior art date
Application number
PCT/EP2001/013362
Other languages
English (en)
Inventor
Giancarlo Sioli
Original Assignee
Casale Chemicals S.A.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Casale Chemicals S.A. filed Critical Casale Chemicals S.A.
Priority to AU2002229553A priority Critical patent/AU2002229553A1/en
Priority to PCT/EP2001/013362 priority patent/WO2003043727A1/fr
Publication of WO2003043727A1 publication Critical patent/WO2003043727A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F28D7/1615—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation the conduits being inside a casing and extending at an angle to the longitudinal axis of the casing; the conduits crossing the conduit for the other heat exchange medium
    • 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
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • 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
    • 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
    • B01J8/0446—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 flow within the beds being predominantly vertical
    • B01J8/0449—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 flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—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 flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • 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
    • B01J8/0446—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 flow within the beds being predominantly vertical
    • B01J8/0476—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 flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/048—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 flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being superimposed one above the other
    • 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
    • B01J8/0496—Heating or cooling the reactor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F28D7/0083—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium
    • F28D7/0091—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium the supplementary medium flowing in series through the units
    • 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
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194—Tubes
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00018—Construction aspects
    • B01J2219/0002—Plants assembled from modules joined together
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • 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
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/192—Details relating to the geometry of the reactor polygonal
    • B01J2219/1923—Details relating to the geometry of the reactor polygonal square or square-derived
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • 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

Definitions

  • the present invention relates to a reactor for catalytic reactions in gaseous phase. More in particular, the invention relates to low and medium pressure reactors for catalytic reactions in gaseous phase.
  • low and medium pressure reactors it is intended to mean reactors operating at a pressure comprised in the range between 1-20 bar.
  • a chemical reactor of the aforesaid type essentially comprises:
  • the heat exchangers remove or provide the heat to the chemical reactants depending if the chemical reactor carries out an exothermic or an endothermic chemical reaction.
  • the chemical reactor to which the present invention relates may also comprise:
  • each chemical reaction - a plurality of inlet pipes to feed the reactants and the heat exchange fluids and outlet pipes to remove the products and the heat exchange fluids.
  • each chemical reaction and particularly but not exclusively, each catalytic chemical reaction requires to be carried out, especially for industrial production, a specific reactor designed and built for such special purpose. In fact, to carry out an industrial scale production with a combined high production yield, the reactor should be designed specifically due to the many variables involved in the chemical reaction to be carried out.
  • variables involved in a chemical reaction are parameters, such as heat of reaction, residence time, catalytic activity, reaction pressure and temperature. Such variables are controlled specifically by appropriate means like thermocouples, flow meters and pressure gauges.
  • the shell In order to appropriately carrying out a chemical reaction the shell must thus have, for example, suitable dimension, shape, apertures, wall- thickness and it must be made of suitable construction materials. The same applies to the number, dimension and reciprocal distance of catalytic beds as well as to the catalyst and all the equipment and instruments, which have to be determined according to the catalytic reaction to be carried out.
  • each chemical reaction or reaction type has to be carried out by a specific reactor.
  • Such a reactor cannot be used or adapted - in general - for any other reaction or reaction type, even if very much alike, but only for the single purpose it has been designed and built.
  • Chemical reactors are in general made with a one-piece external shell closed at the opposite ends thereof by corresponding covers and it is almost impossible to modify their structure once the reactors are built up.
  • the problem underlying the present invention is that of providing a reactor for chemical reactions, which can be adapted easily and in a reliable way to different reaction types, operating conditions and production capacities at low investment and operating costs and without the need of replacing it or supporting it with a new reactor.
  • Said problem is solved according to the present invention by a modular chemical reactor for catalytic reactions in gaseous phase comprising a shell, which is characterized by the fact that the reactor comprises:
  • the present invention makes possible to provide a low or medium- pressure reactor made of one or more of said first and second portions, which can be assembled the one with the other in order to build up a specific reactor depending on the particular chemical reaction to be carried out or on the productivity to be performed.
  • a reactor according to the present invention originally designed for a specific reaction, can be modified (quickly and economically) in order to adapt it to different production requirements for the same reaction or even to carry out different reactions.
  • each first and second portion one catalytic bed and one heat exchanger are associated respectively, so defining the reaction section and the heat exchange section of the reactor.
  • the necessary number of shell portions is properly assembled.
  • the catalytic bed associated portions can be assembled with intermediate heat exchanger associated portions to set up a reactor based on adiabatic reaction sections with intermediate cooling.
  • the reactor can be made of a plurality of shell portions associated to a respective catalytic bed containing heat exchange means immersed into the catalytic bed so as to obtain a plurality of contiguous isothermal reaction sections.
  • the length of the reactor simply changes with the number of shell portions assembled together.
  • each single first and second portion is an independent body, the portions being thus advantageously structurally independent one from the other.
  • the shell portions are all identical modules, having the same size one with respect to the other.
  • the catalytic beds and the heat exchangers associated to the first and second shell portions, respectively, are removable with respect to the latter.
  • FIG.1 schematically shows a reactor made by shell tubular portions in accordance with a first embodiment of the present invention
  • FIG. 2 schematically shows a detail of a tubular shell portion associated to a catalytic bed according to the invention
  • FIG.3 schematically shows a detail of a tubular shell portion associated to a heat exchanger according to the invention
  • FIG.4 schematically shows a reactor made by shell tubular portions in accordance with a further embodiment of the present invention.
  • FIG.5 schematically shows a reactor made by shell tubular portions in accordance with a further embodiment of the present invention.
  • tubular reactor comprising a shell 2 closed at both ends thereof by respective covers 3 and 4.
  • Said reactor 1 is in particular of the type defined as low or medium pressure reactor, i.e. operating at a pressure comprised in the range between 1-20 bar, advantageously used for catalytic reactions in gaseous phase as for instance methanol oxidation to formaldehyde, ethylene oxide production by ethylene oxidation, methylciclohexane dehydrogenation to toluene, sulphur dioxide oxidation to sulphur trioxide, sryrene production by ethylbenzene dehydrogenation, toluene oxidation to benzoic acid, phtalic anhydride by naphtalene or o-xylene oxidation, maleic anhydride by oxidation of benzene or butane.
  • low or medium pressure reactor i.e. operating at a pressure comprised in the range between 1-20 bar
  • the shell 2 comprises at least one first shell tubular portion 5 (shown in detail in FIG.2).
  • Each first shell portion 5 internally comprises one catalytic bed 6, which is preferably associated to the corresponding shell portion 5.
  • the first shell portion 5 and the catalytic bed are reciprocally assembled in a removable manner in order to allow various insertion and removal of the catalyst in and from the first shell portion 5.
  • Each catalytic bed 6 is placed inside each first shell portion 5, transversally to the reactor longitudinal axis A.
  • the shell 2 further comprises at least one second shell tubular portion 7 (shown in detail in FIG.3).
  • Each second shell tubular portion 7 comprises internally one heat exchanger 8, for instance of the tube bundle type, which is preferably associated to the corresponding second shell portion 7 in a removable manner.
  • the second shell portion 7 and the heat exchanger 8 can be reciprocally assembled in a removable manner in order to allow various insertion and removal of the heat exchanger 8 in and from the second shell portion 7.
  • Each heat exchanger 8 is placed inside each second shell portion 7, transversally to the reactor longitudinal axis A.
  • said shell portions 5 and 7 are also structurally independent from each other so that they can be designed and dimensioned for carrying out specific stages of the chemical reaction and of the cooling or the heating.
  • the first shell tubular portion 5 comprising the catalytic bed will be also defined in the subsequent description as “catalytic bed associated portion", while the second shell tubular portion 7 comprising the heat exchanger will be also defined in the subsequent description as "heat exchanger associated portion”.
  • first and second shell portions 5, 7 and thus shell 2 are characterized by a rectangular cross section area.
  • cross section area it is intended to mean the shell area perpendicular to the reactor longitudinal axis A.
  • the rectangular cross section area of the shell 2 allows an optimal use of the internal reactor space for housing the catalyst of the catalytic beds 6 and the tubes of the heat exchangers 8.
  • first and second shell portions 5, 7 are advantageously modules of identical cross size.
  • each portion 5, 7 has the same cross section area and shape. Possibly, such portions may also have identical width.
  • the portions 5 and 7 can be assembled together in different order, so as to alternate the catalytic beds and the heat exchangers according to the specific chemical reaction that it is intended to carry out.
  • Examples of reactors thus obtained are shown in FIGS. 1 and 4.
  • the reactor of FIG. 1 is particularly suitable for reactions of catalytic oxidation, hydrogenation, dehydrogenation, and dehydration.
  • the reactor of FIG. 4 is advantageous when a certain residence time must be provided to the reactant gas between successive catalytic reaction stages, or when the amount of catalyst to be provided is obtained by coupling two or more standard size first portions, or when reactants or dilution means are introduced between two successive catalytic beds.
  • each catalytic bed associated portion 5 is equipped with a catalyst inlet opening 11 and catalyst outlet opening 12 for loading to, or discharging from the catalytic bed 6 the catalyst required specifically for the chemical reaction.
  • each heat exchanger associated portion 7 of the reactor 1 is advantageously equipped, with an inlet nozzle 9 and outlet nozzle 10 for the inlet and the outlet of a heat exchange fluid can be a cooling fluid, such as cooling water, boiler water, diathermic oil, boiling fluids, in case of an exothermic reaction or a heating fluid, such as steam, condensing fluids, molten salts, in case of an endothermic reaction.
  • a cooling fluid such as cooling water, boiler water, diathermic oil, boiling fluids
  • a heating fluid such as steam, condensing fluids, molten salts
  • Shell portions 5 and 7 are assembled together by conventional means (not represented) at corresponding coupling flanges 15.
  • Conventional means for fixing the flanges 15 are for example screws, bolts or tie-rods.
  • covers 3 and 4 are equipped with openings 13 and 14 for the reaction gas inlet and for the reaction products outlet, respectively.
  • the synthesis gas are fed in the inlet opening 13 and then flow in the first catalytic bed 6 associated to first portion 5 where the first catalytic stage of the reaction is performed.
  • the catalytic stage is followed by a heat exchange stage performed in the heat exchanger 8 associated to second portion 7.
  • the flanges 15 are designed in order to be easily assembled together to enhance the proper gas tightness within all the shell portions of the reactor.
  • each portion-to-portion assembly or portion-from-portion disassembly can be carried out several times, without incurring in any mechanical or structural inconvenience.
  • the reactor is horizontally oriented.
  • Other orientations such as vertical can be obtained by utilizing the above shell portions.
  • first and second portions assembled together makes the length of the reactor 1.
  • FIG.2 a detail of a catalytic bed associated portion 5 is shown.
  • the first shell tubular portion 5, with parallelepiped shape has a rectangular cross-section area and is open on both front and rear sides, both indicated with 16.
  • the area of the rectangular openings 16, corresponds to the inner cross section area of the first shell portion 5.
  • the catalytic bed 6, containing the catalyst, is housed inside the shell first portion 5, in a space defined by the inner wall of the shell portion and by two gas permeable walls 18, placed on both front and rear sides 16.
  • Each catalytic bed 6 of this invention is perpendicularly placed with respect to the reactor longitudinal axis A; in this way the distance between each catalytic bed is advantageously reduced to the rninimum.
  • This opening is either circular or rectangular.
  • Each of the openings has a proper cover 19 to enable closing the catalytic bed 6 during the operation period.
  • the catalyst can be easily loaded and removed by gravity in the catalytic bed associated portion 5 by the aforementioned openings 11 and 12.
  • the catalyst changing procedure becomes fast and economic using the reactor of the present invention even for low and medium pressure reactions characterized by frequent catalyst change.
  • the coupling flanges 15 can be rectangular and are placed along the outside perimeter of the front and rear sides 16 of the portion 5. Each coupling flange 15 has preferably a plurality of circular holes 17 along its entire perimeter.
  • a heat exchanger 8 made by a plurality of tubes 20 supported by tube plates, 21 at the top end and 22 at the bottom end of the tubes 20.
  • the tubes 20 are in fluid communication with a chamber 23 over the tube plate 21.
  • Said chamber 23 is defined in the shell by a box (or channel) 7a collecting the fluid passing inside the tube bundle. At the bottom end of the tubes there is a chamber 24, below the plate 22. Said chamber 24 is in fluid communication with the tubes 20 and is defined in the shell by a box (or channel) 7b.
  • the cooling fluid inlet nozzle 9 Placed on the bottom of the second shell portion 7 is the cooling fluid inlet nozzle 9, as far as the cooling fluid outlet nozzle 10 on the top.
  • First and second shell portions 5, 7 are assembled together by conventional means, for example screws, passing trough holes 17 so as to fix the coupling flanges 15.
  • the plurality of holes 17 is made equal in size and position for each single coupling flange 15 allowing in this way to screw together the contacting flanges of two adjacent shell portions. This can be also made with interposition of gaskets, using conventional bolts or tie-rods.
  • the coupling flanges 15 can be without holes 17, and simply held together by using clamps.
  • the reactor according to the present invention ensures advantageously an optimal temperature control during all the thermal stages.
  • each heat exchanger 8 is enhanced to control the temperature within the reactor in a range that can be contained below 1°C.
  • each catalytic bed 6 is perpendicular to the reactor 1 longitudinal axis A, this orientation provides an outstanding space reduction.
  • the invention is made with a circular cross section area.
  • both catalytic bed and heat exchanger associated portions have a circular cross section area. Consequently all the parts composing said shell portions are designed to fit the circular cross section.
  • the reactor described above shown in FIG. l comprises catalytic bed and heat exchanger associated portions 5 and 7 placed in order to obtain a catalytic stage alternate to a heat exchanging stage. The assembly of these portions constitutes a typical reactor based on adiabatic reaction stages, in which heat is exchanged after each catalytic stage.
  • reactor 25 is obtained as shown in FIG.4.
  • Reactor 25 is made by the same kind of portions with respect to the reactor 1 in FIG. l, but enables to carry out a substantially different reaction from the one carried out in the reactor 1.
  • a modular reactor can be conceived for carrying out isothermal or pseudo- isothermal catalytic chemical reactions.
  • a modular chemical reactor 26 for exothermic or endothermic catalytic reactions in gaseous phase comprises a plurality of tubular portions 27 of the shell 2.
  • At least one catalytic bed 6 is internally associated to each shell tubular portion 27 and contains heat exchange means, such as one heat exchanger 8, immersed into the catalyst.
  • Means (not shown) for assembling the plurality of shell tubular portions 27 at the corresponding coupling flanges 15 are also provided in the reactor 26.
  • assembly means are screws, bolts or tie-rods that allow a gas-tight fixing of the flanges 15. Thanks to the provision of a heat exchanger 8 V ⁇ thin the catalyst bed 6 in the shell tubular portions 27, heat can be advantageously supplied or removed during the chemical reaction thus keeping the temperature of each catalytic stage substantially constant.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un réacteur chimique modulaire pour des réactions catalytiques en phase gazeuse, comprenant au moins une première partie (5) tubulaire en coque, associée intérieurement à au moins un lit catalytique (6), au moins une seconde partie tubulaire (7) associée intérieurement à au moins un échangeur de chaleur (8), et un moyen permettant l'assemblage de la première partie tubulaire en coque à au moins une seconde partie tubulaire en coque.
PCT/EP2001/013362 2001-11-19 2001-11-19 Reacteur chimique modulaire WO2003043727A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU2002229553A AU2002229553A1 (en) 2001-11-19 2001-11-19 Modular chemical reactor
PCT/EP2001/013362 WO2003043727A1 (fr) 2001-11-19 2001-11-19 Reacteur chimique modulaire

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2001/013362 WO2003043727A1 (fr) 2001-11-19 2001-11-19 Reacteur chimique modulaire

Publications (1)

Publication Number Publication Date
WO2003043727A1 true WO2003043727A1 (fr) 2003-05-30

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PCT/EP2001/013362 WO2003043727A1 (fr) 2001-11-19 2001-11-19 Reacteur chimique modulaire

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AU (1) AU2002229553A1 (fr)
WO (1) WO2003043727A1 (fr)

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US7232848B2 (en) 2002-09-09 2007-06-19 Conocophillips Company Gas agitated multiphase reactor with stationary catalyst solid phase
CN103411449A (zh) * 2013-08-28 2013-11-27 长沙华成换热设备有限公司 大型组合式箱体换热器
US8922074B2 (en) 2008-06-09 2014-12-30 Otis Elevator Company Elevator machine motor and drive and cooling thereof
CN112595160A (zh) * 2020-12-24 2021-04-02 季华实验室 一种航空燃油滑油热交换器

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GB597501A (en) * 1945-08-22 1948-01-27 Gas Light & Coke Co Improvements in or relating to apparatus for bringing gases into contact with solids
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US2273865A (en) * 1937-08-05 1942-02-24 Houdry Process Corp Apparatus for catalysis and the use thereof
FR877663A (fr) * 1940-12-11 1942-12-14 Metallgesellschaft Ag Dispositif pour effectuer des réactions catalytiques exothermiques
CH238685A (fr) * 1942-03-10 1945-08-15 Fontaine L Eveque Societe Anon Appareil pour l'exécution de réactions catalytiques.
GB597501A (en) * 1945-08-22 1948-01-27 Gas Light & Coke Co Improvements in or relating to apparatus for bringing gases into contact with solids
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US7232848B2 (en) 2002-09-09 2007-06-19 Conocophillips Company Gas agitated multiphase reactor with stationary catalyst solid phase
US8922074B2 (en) 2008-06-09 2014-12-30 Otis Elevator Company Elevator machine motor and drive and cooling thereof
CN103411449A (zh) * 2013-08-28 2013-11-27 长沙华成换热设备有限公司 大型组合式箱体换热器
CN112595160A (zh) * 2020-12-24 2021-04-02 季华实验室 一种航空燃油滑油热交换器

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