WO2004035198A1 - Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions - Google Patents

Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions Download PDF

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Publication number
WO2004035198A1
WO2004035198A1 PCT/EP2003/009931 EP0309931W WO2004035198A1 WO 2004035198 A1 WO2004035198 A1 WO 2004035198A1 EP 0309931 W EP0309931 W EP 0309931W WO 2004035198 A1 WO2004035198 A1 WO 2004035198A1
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WO
WIPO (PCT)
Prior art keywords
flow
reactants
catalytic bed
pseudo
distribution
Prior art date
Application number
PCT/EP2003/009931
Other languages
French (fr)
Inventor
Ermanno Filippi
Enrico Rizzi
Mirco Tarozzo
Keith A. Clayton
Original Assignee
Ammonia Casale 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
Priority to UAA200504638A priority Critical patent/UA79646C2/en
Application filed by Ammonia Casale S.A. filed Critical Ammonia Casale S.A.
Priority to BRPI0315333-9A priority patent/BR0315333B1/en
Priority to CA2502570A priority patent/CA2502570C/en
Priority to MXPA05004010A priority patent/MXPA05004010A/en
Priority to AU2003273834A priority patent/AU2003273834A1/en
Priority to US10/531,189 priority patent/US8529861B2/en
Priority to DE60317545T priority patent/DE60317545T2/en
Priority to EP03757798A priority patent/EP1551544B1/en
Publication of WO2004035198A1 publication Critical patent/WO2004035198A1/en

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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
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0031—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by paired plates touching 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
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • B01J8/0242—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 flow within the bed being predominantly vertical
    • B01J8/0257—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 flow within the bed being predominantly vertical in a cylindrical annular shaped bed
    • 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
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
    • 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
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0006—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the plate-like or laminated conduits being enclosed within a pressure vessel
    • 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
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/0015—Plates; Cylinders
    • 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
    • B01J2208/00548—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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00628—Controlling the composition of the reactive mixture

Definitions

  • the present invention refers to a method for carrying out exothermic chemical reactions in pseudo-isothermal conditions .
  • pseudo-isothermal conditions we mean to indicate those conditions in which the reaction temperature is controlled in a limited range of values around a predetermined optimal value .
  • this invention concerns a method for carrying out, in pseudo-isothermal conditions, highly exothermic catalyzed reactions, like oxidative reactions, for example ammonia oxidation to give nitric acid and ethanol oxidation to give formaldehyde.
  • the present invention also refers to an apparatus for carrying out the aforementioned method.
  • This type of reactor suffers from many recognized drawbacks, such as excessive energy consumption caused by the need to feed large quantities of air so as to keep the ammonia concentration below the explosivity threshold, greater constructive complexity with respect to fixed bed reactors and problems of dust recovery.
  • the catalyst in movement inside said fluid bed reactors carries out a corrosive action against the walls of the reactors themselves.
  • the technical problem underlying the present invention is that of providing a method for carrying out highly exothermic oxidative reactions, in pseudo-isothermal conditions, between reactants fed in continuous flow to a predetermined catalytic bed, capable of overcoming the aforementioned drawbacks with reference to the prior art, in other words to operate below explosivity limits of the mixtures of reactants and of reactants-products and to promote a longer lifetime of the catalyst.
  • the aforementioned technical problem is solved, according to the present invention, by a method characterized in that at least part of said continuous flow of reactants is fed at different points of said catalytic bed corresponding to different successive stages of the reaction, at respective different predetermined temperatures and flow-rates, where the concentration of the reactants is low.
  • the successive stages of the reaction are defined at different respective heights in the catalytic bed, wherein the reactants are fed at the predetermined flow-rates and temperatures.
  • Figure 1 schematically shows a chemical reactor for carrying out the method according to the invention
  • Figure 2 schematically shows an enlarged view of a detail of the reactor of figure 1.
  • a chemical reactor with a vertical axis, used to carry out highly exothermic reactions, for example and preferably oxidative reactions like ammonia oxidation to give nitric acid, is globally and schematically indicated with 1.
  • Said reactor 1 comprises a cylindrical shell 2, opposite end plates, lower 3 and upper 4.
  • the upper end plate 4 is equipped with a manhole 5, whereas the lower end plate 3 is equipped with an opening 6 for discharging the reaction products .
  • a reaction zone 7 is defined, representatively situated between a lower line 8 and an upper line 9, to receive a predetermined catalytic bed (L) , intended to be crossed axially by the reactant gases and by the reaction products .
  • the catalytic bed (L) is supported in a per se known way and therefore it is not represented.
  • a plurality of heat exchangers 10 and a corresponding plurality of distribution-supplier devices 12 are immersed and supported; said heat exchangers 10 are plate-shaped, rectangular, preferably arranged radially, in many rows concentric and coaxial to said shell and with long sides 11 parallel to the axis of the shell itself.
  • each exchanger 10 is associated, in particular is fixed, a couple of distribution-suppliers 12, for which it constitutes an appropriate support, as shall become clear from the rest of the description.
  • each heat exchanger 10 comprises a wall 27 and a wall 28, juxtaposed, joined at the perimeter, for example through appropriate welding, in a mutually distanced relationship, so as to form a first chamber 18 between them.
  • a second chamber 19 is also defined, separated fluid- tight from said first chamber 18.
  • the chamber 18 is equipped with an inlet fitting 29, and with an outlet fitting 31, whereas the chamber 19 comprises only one inlet fitting 34.
  • Two box-shaped carters 20 and 22 are fixed to the wall 27 of each exchanger 10, extending perpendicularly to said side 1 for the whole width of the respective exchanger 10.
  • the carters 20 and 22 define with the wall 27 respective ducts 21 and 23, in fluid communication, on one side, with said second chamber 18 through openings 36 and 37, formed in the wall 27 and, on the other side, with the outside of the exchanger 10, and therefore with the catalytic bed (L) in which said exchanger 10 is immersed, through a plurality of holes 26, formed in the carters themselves.
  • said holes 26 are arranged in rectilinear alignments, extending longitudinally to the respective carter (20, 22) .
  • the plurality of exchangers 10 with relative distribution- suppliers 12, constitutes, in accordance with the present invention, an apparatus suitable for controlling the temperature and the concentration of the reactants in the catalytic bed ( ) , as shall become clear in the rest of the description.
  • the reactor 1 also comprises:
  • a flow of reactants for example ammonia and oxygen for the production of nitric acid, is continuously fed to the reactor 1, and is separated into two parts upon entry.
  • a first part or main part of said flow is preheated to the most appropriate temperature to trigger the desired reaction (ammonia oxidation) through heat exchange with the catalytic bed (L) ; for such a purpose and in the specific case illustrated, said main part of the flow of reactants is divided, through the distributor 12, between all of the ducts 15 - fittings 30, for feeding the chambers 18 of all of the exchangers 10.
  • the reactants thus preheated are collected by the collector 20, which conveys them to the lower end of the central duct 24.
  • the preheated reactants are distributed above the catalytic bed (L) , crossing which they start off the desired highly exothermic oxidation reaction.
  • a second part of said flow of reactants, or control flow, is divided between all the chambers 18 of the plurality of exchangers 10, from each of which it is fed to the respective pairs of distribution-suppliers 19, 20.
  • said distribution-suppliers 19, 20 are positioned in the catalytic mass of the bed (L) , at heights strictly corresponding to the stages of the reaction taking place in correspondence of which it is foreseen to control the concentration and temperature of the reactants.
  • the reaction products are discharged from the reactor 1 through the opening 6.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Fluid Mechanics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Steroid Compounds (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

Method and apparatus for carrying out highly exothermic catalyzed reactions, like so-called oxidative reactions, in pseudo-isothermal conditions, for example the reaction for producing nitric acid and the reaction for producing formaldehyde. At least part of the continuous flow of reactants is fed at different points of the catalytic bed corresponding to different successive stages of the reaction.

Description

Title: "Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions"
DESCRIPTION
Field of the invention
In its most general aspect the present invention refers to a method for carrying out exothermic chemical reactions in pseudo-isothermal conditions .
In the rest of the description and in the subsequent claims, with the term pseudo-isothermal conditions we mean to indicate those conditions in which the reaction temperature is controlled in a limited range of values around a predetermined optimal value .
In particular, this invention concerns a method for carrying out, in pseudo-isothermal conditions, highly exothermic catalyzed reactions, like oxidative reactions, for example ammonia oxidation to give nitric acid and ethanol oxidation to give formaldehyde.
The present invention also refers to an apparatus for carrying out the aforementioned method.
Prior Art
Regarding highly exothermic oxidative reactions it is well known that, in order to avoid clearly dangerous operating conditions, it is required to control one or more operating variables, like reaction temperature and concentration of at least one reactant.
Thus, for example, in the production of formaldehyde through methanol oxidation, the high concentration of the reactants and the high exothermicity of the reaction quickly lead to operate in explosive conditions; from here arises the need to strictly control both the concentration of the reactants and the reaction temperature below well- determined values.
Moreover, when the reaction temperature and concentration of the reactants exceed said values, there may happen phenomena of "poisoning" and degeneration of the catalyst, with the consequent inevitable yield reduction. This is the case of ammonia oxidation to give nitric acid, where the catalyst based upon Co30 undergoes a rapid CoO reduction, a much less active form of Co304, right when the concentration of the reactant exceeds a predetermined threshold at a predetermined temperature.
To control the temperature and the concentration of the reactants, it has been suggested to carry out the reactions of the considered type in fluid bed reactors.
This type of reactor, however, suffers from many recognized drawbacks, such as excessive energy consumption caused by the need to feed large quantities of air so as to keep the ammonia concentration below the explosivity threshold, greater constructive complexity with respect to fixed bed reactors and problems of dust recovery.
Moreover, the catalyst in movement inside said fluid bed reactors carries out a corrosive action against the walls of the reactors themselves.
Summary of the invention
The technical problem underlying the present invention is that of providing a method for carrying out highly exothermic oxidative reactions, in pseudo-isothermal conditions, between reactants fed in continuous flow to a predetermined catalytic bed, capable of overcoming the aforementioned drawbacks with reference to the prior art, in other words to operate below explosivity limits of the mixtures of reactants and of reactants-products and to promote a longer lifetime of the catalyst.
The aforementioned technical problem is solved, according to the present invention, by a method characterized in that at least part of said continuous flow of reactants is fed at different points of said catalytic bed corresponding to different successive stages of the reaction, at respective different predetermined temperatures and flow-rates, where the concentration of the reactants is low.
In the non-limiting case of use of a pseudo-isothermal reactor with a vertical axis, with a catalytic bed crossed axially by the reactants, the successive stages of the reaction are defined at different respective heights in the catalytic bed, wherein the reactants are fed at the predetermined flow-rates and temperatures.
The characteristics and advantages of the method of the present invention shall become clearer from the following description of an example embodiment thereof, made with reference to the attached drawings given for indicating and not limiting purposes.
Brief description of the drawings
Figure 1 schematically shows a chemical reactor for carrying out the method according to the invention; Figure 2 schematically shows an enlarged view of a detail of the reactor of figure 1.
Detailed description of the figures
With reference to figure 1, a chemical reactor, with a vertical axis, used to carry out highly exothermic reactions, for example and preferably oxidative reactions like ammonia oxidation to give nitric acid, is globally and schematically indicated with 1.
Said reactor 1 comprises a cylindrical shell 2, opposite end plates, lower 3 and upper 4. The upper end plate 4 is equipped with a manhole 5, whereas the lower end plate 3 is equipped with an opening 6 for discharging the reaction products .
In said shell 2 a reaction zone 7 is defined, representatively situated between a lower line 8 and an upper line 9, to receive a predetermined catalytic bed (L) , intended to be crossed axially by the reactant gases and by the reaction products .
The catalytic bed (L) is supported in a per se known way and therefore it is not represented.
In the catalytic bed (L) a plurality of heat exchangers 10 and a corresponding plurality of distribution-supplier devices 12 are immersed and supported; said heat exchangers 10 are plate-shaped, rectangular, preferably arranged radially, in many rows concentric and coaxial to said shell and with long sides 11 parallel to the axis of the shell itself.
In accordance with a characteristic of the present invention, and according to a preferred embodiment, with each exchanger 10 is associated, in particular is fixed, a couple of distribution-suppliers 12, for which it constitutes an appropriate support, as shall become clear from the rest of the description.
In particular, with reference to figure 2, each heat exchanger 10 comprises a wall 27 and a wall 28, juxtaposed, joined at the perimeter, for example through appropriate welding, in a mutually distanced relationship, so as to form a first chamber 18 between them.
Near to a side 11 of said exchanger 1 and through a welding line 25, having a portion 32 parallel to said side 11 and a portion 33 perpendicular to it, between said walls 27 and 28 a second chamber 19 is also defined, separated fluid- tight from said first chamber 18.
The chamber 18 is equipped with an inlet fitting 29, and with an outlet fitting 31, whereas the chamber 19 comprises only one inlet fitting 34.
Two box-shaped carters 20 and 22 are fixed to the wall 27 of each exchanger 10, extending perpendicularly to said side 1 for the whole width of the respective exchanger 10.
The carters 20 and 22 define with the wall 27 respective ducts 21 and 23, in fluid communication, on one side, with said second chamber 18 through openings 36 and 37, formed in the wall 27 and, on the other side, with the outside of the exchanger 10, and therefore with the catalytic bed (L) in which said exchanger 10 is immersed, through a plurality of holes 26, formed in the carters themselves. Preferably, said holes 26 are arranged in rectilinear alignments, extending longitudinally to the respective carter (20, 22) .
The carters 20 and 22, supported by a respective exchanger 10, essentially constitute a distribution-supplier device 12 for a predetermined fluid, fed to said carters through the chamber 18.
The plurality of exchangers 10 with relative distribution- suppliers 12, constitutes, in accordance with the present invention, an apparatus suitable for controlling the temperature and the concentration of the reactants in the catalytic bed ( ) , as shall become clear in the rest of the description.
The reactor 1 also comprises:
- feed ducts for the predetermined reactants (13 and 14) which are in fluid communication with the chamber 18 and 19 respectively of each exchanger 10, through a system which includes ducts (15 and 16) and respective fittings (30 and 35) .
- collector ducts 17 for the reaction products, which are in fluid communication, on one side, with the outlet fittings 31 of each exchanger and, on the other side, with a central duct 24 axially provided in the reactor.
With reference to the aforementioned apparatus, the method of the present invention for carrying out highly exothermic oxidative reactions in pseudo-isothermal conditions, through simultaneous control of the reaction temperature and of the concentration of reactants around respective predetermined values, shall now be described. A flow of reactants, for example ammonia and oxygen for the production of nitric acid, is continuously fed to the reactor 1, and is separated into two parts upon entry.
A first part or main part of said flow is preheated to the most appropriate temperature to trigger the desired reaction (ammonia oxidation) through heat exchange with the catalytic bed (L) ; for such a purpose and in the specific case illustrated, said main part of the flow of reactants is divided, through the distributor 12, between all of the ducts 15 - fittings 30, for feeding the chambers 18 of all of the exchangers 10.
Exiting from the plurality of exchangers 10, the reactants thus preheated are collected by the collector 20, which conveys them to the lower end of the central duct 24. Exiting from the upper end of said duct 24, the preheated reactants are distributed above the catalytic bed (L) , crossing which they start off the desired highly exothermic oxidation reaction.
A second part of said flow of reactants, or control flow, is divided between all the chambers 18 of the plurality of exchangers 10, from each of which it is fed to the respective pairs of distribution-suppliers 19, 20.
As described above, said distribution-suppliers 19, 20 are positioned in the catalytic mass of the bed (L) , at heights strictly corresponding to the stages of the reaction taking place in correspondence of which it is foreseen to control the concentration and temperature of the reactants.
In accordance with the present invention such a control is substantially made possible by the injection in predetermined points of the catalytic bed of a fresh flow — o —
of reactants, the concentration of which is regulated continuously adjusting suitably and in a per se known way the flow rate of the second part of said flow of reactants .
The reaction products are discharged from the reactor 1 through the opening 6.
The invention thus conceived is susceptible to variants and modifications, all of which are covered by the scope of protection of the present invention defined by the following claims .

Claims

1. Method for carrying out highly exothermic oxidative reactions in pseudo-isothermal conditions, between reactants fed in continuous flow to a predetermined catalytic bed, characterized in that at least a part of said continuous flow of reactants is fed at different points of said catalytic bed corresponding to different successive stages of the reaction, at respective different predetermined temperatures and flow-rates .
2. Method for carrying out highly exothermic oxidative reactions in pseudo-isothermal conditions, between reactants fed in a continuous flow to a predetermined catalytic bed (L) , in which a plurality of heat exchangers (10) is immersed and supported, characterized in that:
- a plurality of distribution-suppliers (20, 22) is positioned in said catalytic bed (L) , at different points thereof strictly corresponding to different predetermined stages of said oxidative reaction,
- said continuous flow of reactants is divided into a first part or main flow and a second part or control flow with a predetermined temperature and flow-rate,
- said first part or main flow is preheated through heat exchange with said catalytic bed (L) , feeding it through said plurality of exchangers (10) ,
- said main flow of preheated reactants is recovered and it is fed continuously to said catalytic bed (L) ,
said second part or control flow is fed to said plurality of distribution-suppliers (20, 22) to inject respective fresh flows of reactants at a predetermined temperature and flow-rate into the catalytic bed (L) .
3. Apparatus for carrying out a highly exothermic oxidative reaction in pseudo-isothermal conditions according to the method of claims 1 and 2, comprising a plurality of heat exchangers (10), characterized in that with each of said exchangers is associated at least one distribution-supplier (20, 22) suitable for being fed continuously by a flow a reactants at a predetermined temperature and flow-rate.
4. Apparatus according to claim 3, characterized in that said at least one distribution-supplier (20, 22) is supported fixed by said respective heat exchanger (10) .
5. Apparatus according to claim 4, characterized in that said heat exchanger (10) is plate-shaped and substantially rectangular, inside which a first chamber (18), intended to be crossed by a respective flow of reactants to be preheated, and a second chamber (19) , separated fluid-tight from said first chamber (18) and in fluid communication with said at least one distribution-supplier (20, 22) are defined.
6. Apparatus according to claim 5, characterized in that said distribution-supplier (20, 22) comprises a carter fixed to a wall of a respective plate-shaped heat exchanger (10), with which it substantially defines a duct in fluid communication, on one side, with said second chamber (19) of the exchanger (10) and, on the other side, with the outside of the exchanger (10) itself, through a plurality of holes formed in said carter.
7. Reactor for carrying out highly exothermic catalyzed oxidative reactions in pseudo-isothermal conditions, comprising a shell in which is defined a reaction zone at least partially occupied by a catalytic bed (L) , characterized in that it comprises an apparatus according to claims 3 to 6, immersed in said catalytic bed (L) .
PCT/EP2003/009931 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions WO2004035198A1 (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
UAA200504638A UA79646C2 (en) 2002-10-17 2003-08-09 Method for carrying out highly exothermic oxidative reactions in pseudo-isothermal conditions
BRPI0315333-9A BR0315333B1 (en) 2002-10-17 2003-09-08 METHOD FOR CARRYING OUT STRONGLY EXOTHERMAL OXIDATION REACTIONS IN PSEUDO-ISOTHERMIC CONDITIONS
CA2502570A CA2502570C (en) 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions
MXPA05004010A MXPA05004010A (en) 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions.
AU2003273834A AU2003273834A1 (en) 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions
US10/531,189 US8529861B2 (en) 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions
DE60317545T DE60317545T2 (en) 2002-10-17 2003-09-08 METHOD FOR IMPLEMENTING HARD EXOTHEROUS OXIDATION REACTIONS UNDER PSEUDO-ISOTHERMAL CONDITIONS
EP03757798A EP1551544B1 (en) 2002-10-17 2003-09-08 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP02023316.9 2002-10-17
EP20020023316 EP1410842A1 (en) 2002-10-17 2002-10-17 Method to carry out strongly exothermic oxidizing reactions in pseudo-isothermal conditions

Publications (1)

Publication Number Publication Date
WO2004035198A1 true WO2004035198A1 (en) 2004-04-29

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Country Status (13)

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US (1) US8529861B2 (en)
EP (2) EP1410842A1 (en)
CN (1) CN100344360C (en)
AT (1) ATE378105T1 (en)
AU (1) AU2003273834A1 (en)
BR (1) BR0315333B1 (en)
CA (1) CA2502570C (en)
DE (1) DE60317545T2 (en)
MX (1) MXPA05004010A (en)
MY (1) MY136339A (en)
RU (1) RU2321456C2 (en)
UA (1) UA79646C2 (en)
WO (1) WO2004035198A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11065591B2 (en) 2017-12-20 2021-07-20 Haldor Topsoe A/S Method and reactor for performing exothermic reactions

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1787715A1 (en) * 2005-11-18 2007-05-23 Methanol Casale S.A. Plate type heat exchanger for a isothermal chemical reactor
DE102008025887A1 (en) 2008-05-29 2009-12-03 Bayer Technology Services Gmbh Process for the preparation of formaldehyde
EP2311554A1 (en) * 2009-10-07 2011-04-20 Linde Aktiengesellschaft Method for reaction control of exothermic reaction and apparatus therefore
DE102014001499A1 (en) * 2014-02-06 2015-08-06 Api Schmidt-Bretten Gmbh & Co. Kg For heat and / or mass transfer suitable plate apparatus
CN109954451A (en) * 2019-04-25 2019-07-02 镇江李长荣高性能材料有限公司 A kind of reactor for the production of silver-colored formaldehyde
EP4005974A1 (en) * 2020-11-27 2022-06-01 Casale Sa Ammonia burner for nitric acid production
TW202330103A (en) 2021-11-30 2023-08-01 新加坡商阿瓦克科技私人有限公司 Sorbent for dialysis and sorbent system for regenerative dialysis

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB680605A (en) * 1950-05-09 1952-10-08 California Research Corp Phosphoric acid polymerization of olefins
FR2029533A1 (en) * 1969-01-28 1970-10-23 Basf Ag Control of exothermic reactions including - hydrogenation
US6153149A (en) * 1997-08-06 2000-11-28 The Trustees Of Princeton University Adaptive feedback control flow reactor
EP1236505A1 (en) * 2001-02-27 2002-09-04 Methanol Casale S.A. Method for carrying out chemical reactions in pseudo-isothermal conditions

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB391444A (en) * 1931-10-26 1933-04-26 British Celanese Improvements in or relating to the manufacture of acetaldehyde

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB680605A (en) * 1950-05-09 1952-10-08 California Research Corp Phosphoric acid polymerization of olefins
FR2029533A1 (en) * 1969-01-28 1970-10-23 Basf Ag Control of exothermic reactions including - hydrogenation
US6153149A (en) * 1997-08-06 2000-11-28 The Trustees Of Princeton University Adaptive feedback control flow reactor
EP1236505A1 (en) * 2001-02-27 2002-09-04 Methanol Casale S.A. Method for carrying out chemical reactions in pseudo-isothermal conditions

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11065591B2 (en) 2017-12-20 2021-07-20 Haldor Topsoe A/S Method and reactor for performing exothermic reactions
US11161084B2 (en) 2017-12-20 2021-11-02 Haldor Topsoe A/S Cooled axial flow converter

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