WO2000017946A2 - Procede d'evaluation d'une reaction d'emballement thermique - Google Patents

Procede d'evaluation d'une reaction d'emballement thermique Download PDF

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Publication number
WO2000017946A2
WO2000017946A2 PCT/US1999/018690 US9918690W WO0017946A2 WO 2000017946 A2 WO2000017946 A2 WO 2000017946A2 US 9918690 W US9918690 W US 9918690W WO 0017946 A2 WO0017946 A2 WO 0017946A2
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Prior art keywords
reactor
tube
flow
reactants
tubes
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PCT/US1999/018690
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English (en)
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WO2000017946A3 (fr
Inventor
Philip M. Colling
Robert L. Ii King
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Celanese International Corporation
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Publication of WO2000017946A2 publication Critical patent/WO2000017946A2/fr
Publication of WO2000017946A3 publication Critical patent/WO2000017946A3/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
    • 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
    • B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • 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
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • 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
    • B01J2208/00212—Plates; Jackets; 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00193—Sensing a parameter
    • B01J2219/00195—Sensing a parameter of the reaction system
    • B01J2219/002—Sensing a parameter of the reaction system inside 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00211—Control algorithm comparing a sensed parameter with a pre-set value
    • B01J2219/0022—Control algorithm comparing a sensed parameter with a pre-set value calculating difference
    • 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
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00222—Control algorithm taking actions
    • B01J2219/00225—Control algorithm taking actions stopping the system or generating an alarm
    • 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
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00259—Preventing runaway of the chemical reaction
    • B01J2219/00261—Predicting runaway of the chemical reaction

Definitions

  • the present invention is directed to a method of evaluating a reaction in a shell and tube reactor for signs of thermal runaway and an associated apparatus for reducing the flow of reactants into a reactor tube inside of a shell and tube reactor.
  • Shell and tube reactors are useful in many chemical processes. They are particularly useful in the vapor-phase production of vinyl acetate, ethylene oxide, and acrylic acid.
  • Shell and tube reactors are commonly comprised of a plurality of tubes spaced apart from one another inside the shell of the reactor.
  • the tubes are usually loaded with a catalyst.
  • the catalyst is loaded onto a support which is often in the form of pellets.
  • the support bearing the catalyst is loaded into each of the reaction tubes.
  • VA vinyl acetate
  • the reactants, acetic acid, ethylene, and oxygen are maintained in the vapor phase and passed through each tube over the catalyst. Thus, the reaction takes place within the tubes.
  • thermal runaway When the heat of reaction exceeds the heat removal capability of the reactor, a dangerous condition known as thermal runaway or "runaway reaction” occurs thus causing hot spots. In a thermal runaway, there is also an increase in the production of reaction byproducts, primarily CO 2 .
  • thermocouples may be placed to detect, determine and monitor temperatures within each of the selected reaction tubes.
  • Shell and tube reactors vary in size and tubes may exceed 20 feet in length. Accordingly, multiple thermocouples, called multi-point thermocouples, may be placed in a given tube so that thermocouples are positioned inside the selected tube over its entire length.
  • Such multi-point thermocouples commonly include a series of thermocouples contained inside a thin- walled, small diameter stainless steel (or other suitable material) tube.
  • the stainless steel tube containing the multiple thermocouples is normally placed in the center of a reaction tube within the reactor and catalyst packed around the thermocouple tube in normal fashion.
  • Each thermocouple tube is hardwired to a junction box outside the reactor which is then in turn hardwired to the control room so that the data generated from each thermocouple can be detected and stored in computer memory in the control room. In a commercial setting, the data can also be read out by operators in the control room.
  • thermocouples give the operator valuable information regarding the operation of the process and the functioning of the reactor.
  • the temperature of the reaction can be evaluated at multiple points or levels within that reaction tube.
  • hot spots can be detected, within monitored tubes, and inferred for the others, so that appropriate action can be taken.
  • the method of the present invention is directed to evaluating a reaction within a shell and tube reactor for the signs of thermal runaway.
  • the method of the present invention involves restricting the flow of reactants through selected reaction tubes containing thermocouples in order to make these selected reactor tubes more susceptible to changes in reaction conditions and aging of the catalyst. These restricted flow thermocouple tubes will tend to register hotter than the remainder of the reaction tubes (due to the lower heat transfer coefficient which results from the lower velocity of the gases inside the tubes) in response to reaction condition changes and aging of the catalyst thus warning of the potential for thermal runaway.
  • the flow of reactants may be from the top to the bottom or bottom to top of the tubes (down flow or up flow respectively). Most convenient are downflow type tubes wherein the flow is from the top of the reactor tube to the bottom of the tube. Catalyst is typically loaded into the individual reactor tubes from the top of the tube.
  • Flow may be restricted in one of these tubes by any number of means.
  • One means is a restrictive orifice insert positioned in the inlet or top of a down flow reactor tube.
  • the restrictive orifice would be configured so as to reduce reactant flow generally by approximately 10%.
  • Another means for restricting flow in a thermocouple tube is to use a smaller inert support in the upper portion of the reaction tube. For example, where a catalyst is loaded on 7 mm diameter support particles, 5 mm inert particles would be used above the 7 mm catalyst support. This matrix of inert particles would restrict the flow of reactants through that reactor tube.
  • a method for evaluating a reaction within a shell and tube reactor for signs of thermal runaway includes the steps of equipping a plurality of reactor tubes with a thermocouple; restricting the flow of reactants through selected reactor tubes which contain a thermocouple; operating the process at desired reaction conditions; determining a temperature profile for each reactor tube containing a thermocouple; comparing the differences between the temperature profiles for the reactor tubes into which the flow of reactants is restricted and the temperature profiles for the reactor tubes into which the flow of reactants is not restricted; and correlating the differences between the temperature profiles with signs of thermal runaway.
  • the reaction conditions could then be adjusted in response to signs of thermal runaway.
  • an apparatus for restricting the flow of reactants into a reactor tube within a tube and shell reactor is provided.
  • the apparatus is a restrictive flow insert configured to be positionable in an end of the reactor tube within the shell and tube reactor.
  • the restrictive flow insert is designed to reduce the flow of reactants into the tube by a predetermined amount, for example, by about 10-15%.
  • a means for restricting the flow of reactants into a reactor tube within a tube and shell reactor is provided.
  • the flow restricting means is positionable within the reactor tube within the shell and tube reactor and is configured to reduce the flow of reactants through the reactor tube by a predetermined amount, for example, by about 10-15%.
  • Numerous flow restricting means are possible.
  • the means could be configured as a reactor tube entrance or exit diameter reduction device such as a restrictive orifice insertable in the reaction tube; the inside diameter of a portion of a particular reactor tube could be reduced by some predetermined amount using a diameter reducing insert; the use of a smaller diameter catalyst support loaded into the reactor tube above, or below, the catalyst charge; and the like.
  • a reactor tube could likewise be constricted during design and have a restriction built-in to the tube.
  • a shell and tube reactor is provided.
  • the reactor includes a reactor shell; a plurality of reactor tubes positioned spaced apart within the reactor shell; a first tube sheet affixing the reactor tubes at a first end thereof; a second tube sheet affixing the reactor tubes at a second end thereof; a plurality of multi-point thermocouples wherein a single multi-point thermocouple is positioned within a single reactor tube in a selected number of reactor tubes; and a plurality of means for restricting the flow of reactants through a reactor tube wherein a flow restricting means is positioned in at least one of the reactor tubes equipped with a multi-point thermocouple.
  • Fig. 1 is a diagrammatic illustration of a vapor-phase process for producing vinyl acetate.
  • Fig. 2 is a side view of a partial breakaway of a shell and tube reactor.
  • Fig. 3 is a top view of a cross section of the reactor illustrated in Fig. 2.
  • Fig. 4 is a close up view of a segment of Fig. 3.
  • FIG. 5 is a side view of a cross section of several of the reactor tubes illustrated in Fig. 4. DESCRIPTION OF SPECIFIC EMBODIMENTS Although the present invention will be described relative to production of VA, it is understood to be generally applicable to reactions involving use of shell and tube reactors.
  • Figure 1 illustrates diagrammatically a very simplified vapor-phase process for producing vinyl acetate. Vinyl acetate is produced in the vapor-phase from reactants ethylene, acetic acid, and oxygen which are passed over a catalyst which typically contains palladium.
  • the catalyst is typically supported on some form of an inert support which is typically in the form of pellets of various shapes and sizes.
  • the supports are typically spherical in nature.
  • the supported catalyst would be loaded into a shell and tube reactor 10.
  • Ethylene enters the reactor loop 20 from line 30, where it mixes with recycled gases from compressor 100.
  • the acetic acid enters the acetic acid vaporizer 40 through line 50 where it is mixed with the resultant ethylene enriched recycle gas and vaporized.
  • the recycle gas/acetic acid mixture in the vapor-phase pass through the vaporizer overhead 60 toward the reactor 10.
  • Oxygen enters the reactor loop 20 and vaporizer overhead 60 through line 65. Ethylene, acetic acid, and oxygen along with other components of the recycle gas are all passed into reactor 10.
  • the reactants, ethylene, acetic acid, oxygen, and other gaseous components are passed through reactor tubes over the supported catalyst under conditions favorable for reaction. Vinyl acetate, unreacted ethylene, acetic acid, and oxygen all pass out of reactor 10 into product recovery section 70.
  • product recovery section 70 crude vinyl acetate is separated out from the reactants and sent on to purification by way of line 80.
  • Fig. 2 illustrates a shell and tube reactor represented as reactor 10 in Fig. 1.
  • Shell and tube reactor 10 includes a reactor shell 110 encompassing a plurality of reactor tubes 120.
  • the reactor tubes 120 are supported at their top and bottom ends by tube sheets 130. In Fig. 2, only the upper tube sheet 130 is shown.
  • the reactor tubes 120 are spaced apart such that, as seen in Figure 2, there is space 135 between each and every reactor tube 120.
  • the space 135 is for water to be circulated between and amongst the reactor tubes 120 for heat exchange and dissipation.
  • thermocouples 150 positioned inside them. These thermocouples 150 are positioned centrally within the reactor tubes 120 and the supported catalyst for the vapor-phase reaction loaded around the thermocouple 150.
  • Thermocouples 150 may be single point thermocouples so that they measure temperature at a specific point or they may be multi-point thermocouples such that a series of individual thermocouples is positioned along the entire length of a reactor tube 120.
  • Multi-point thermocouples are typically a series of thermocouples positioned within a small diameter tube.
  • the tube containing the thermocouples may be a thin- walled stainless steel and it is positioned in the center of a reactor tube 120 and the supported catalyst loaded around the multi-point thermocouple tube in the usual manner.
  • Multi-point thermocouples typically extend the entire length of the reactor tube 120 and are hard- wired to a junction box outside of the reactor, which is in turn hard- wired to the reaction control room where the data gathered from the various thermocouples may be assessed and stored.
  • Reactor tubes 120 may exceed 20 feet in length. Thus, using a multi-point thermocouple, temperature evaluations can be made of the reaction at various points or levels within the reactor. Such data gives a more complete picture of the reaction conditions in the shell and tube reactor 10 with respect to temperature.
  • reactor tubes which exhibit a restricted flow of reactants will tend to operate at a higher temperature than surrounding unrestricted reactor tubes. Furthermore, it has been learned that with respect to the vapor-phased production of vinyl acetate, that reactor tubes containing a multi-point thermocouple and having a restricted flow of reactants will tend to operate at temperatures within normal limits of the other reactor tubes containing thermocouples during typical operating conditions. However, under certain reaction conditions, particularly when reaction rates are increased or as the catalyst ages, these restricted flow tubes tend to flare up or run hotter than the unrestricted tubes. These flare-ups tend to indicate that the reaction may be reaching thermal runaway conditions.
  • the amount of restriction should be sufficient to cause tubes being restricted to develop "hot spots" before or instead of the non-restricted tubes.
  • "Before” here refers to a period of time wherein as the process conditions change, the restricted tubes will exhibit “hot spots” before, or instead of, the non-restricted thermocouple tubes.
  • reactor tubes 120 are open at each end. Accordingly, the flow of reactants may be restricted at either the inlet end or the outlet end.
  • Reactor tubes 120 are generally loaded with catalyst from the top. Referring to Figure 2, reactor tubes 120 would be loaded from the head space 140, or inlet end, of reactor tubes 120. Thus, for convenience sake, it would be easier to place a flow restricting means in the inlet end of reactor tubes 120.
  • reactor tubes 120 There are numerous means for restricting the flow of reactants through reactor tubes 120.
  • a smaller diameter support material may be substituted for the supported catalyst in the last several feet nearest the inlet end of reactor tube 120.
  • a 7 mm diameter support with catalyst on its surface would be loaded into the reactor tube 120 up to within several feet of the inlet end of reactor tube 120.
  • the last several feet of reactor tube 120 would be loaded with a 5 mm diameter support either with or without catalyst on it and the flow of reactants through reactor tube 120 would be reduced. The amount of flow reduction could be measured and adjustments made until reaching the desired amount.
  • Devices which would change either the inlet or the outlet diameter of reactor tube 120 could also serve to restrict the flow of reactants through reactor tube 120.
  • Such a device could be configured as an insert positionable within the inside diameter of reactor tube 120.
  • the insert would include an restricted orifice.
  • the diameter of the orifice could be engineered to achieve a desired flow reduction.
  • reactor tubes 120 interspersed among reactor tubes 120 are reactor tubes containing thermocouples 150 and reactor tubes 120 containing both thermocouples 150 and flow restricting devices 160.
  • Figure 4 better illustrates the presence of the three separately configured reactor tubes 120.
  • An embodiment of the apparatus of the present invention as illustrated in Figure 4 is that of an insert positioned in the opening of reactor tube 120.
  • the insert 160 is configured to fit securely in the inlet opening of reactor tube 120.
  • Insert 160 may be positioned within reactor tube 120 using a frictional fit, it may be threaded with the reactor tube having reciprocal threading, it may be secured using an additional resilient member disposed about the circumference of the insert so that there is a frictional engagement of the inner diameter of reactor tube 120, and the like.
  • the insert 160 may be permanently secured such as by welding onto the tube.
  • a further alternate may be a restricting means such as a washer or washer-like device which is placed above the catalyst bed, within or on top of the inert materials.
  • the washer does not necessarily have to be secured permanently or fit securely within the tube. It may also have a single hole or multiple holes, provided that the object of flow restriction is achieved. Those skilled in the art will be aware of and appreciate numerous ways of securing or designing insert 160 within the inner diameter of reactor tube 120.
  • reactor tubes 120 are spaced apart and fixed in position by tube sheet 130 both at the inlet and outlet ends of reactor tubes 120.
  • the arrows present just above each of the illustrated reactor tubes 120 indicates their inlet end.
  • Flow restricting insert 160 is positioned in the end of reactor tube 120. Insert 160 is configured in the form of an insert possessing a channel running through the plug and having an orifice at either end of the channel. The diameter of channel 170 in insert 160 may be designed and engineered to provide a predetermined reduction in the flow of reactants into reactor tube 120.
  • T Thermocouple
  • the non-restricted tubes produced peak exotherm temperatures of between 365-385 °C while the restricted flow tubes produced peak exotherm temperatures in the range of about 350 °C to about 700 °C over the same monitoring period.

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

Abstract

Un emballement thermique d'une réaction dans un réacteur à enveloppe et à tubes se produit lorsque la vitesse de réaction dépasse la vitesse d'élimination de la chaleur et doit être évitée. La présente invention concerne un procédé d'évaluation d'une réaction à l'intérieur d'un réacteur à enveloppe et tubes en recherchant les signes d'un emballement thermique. Le procédé comprend les étapes consistant à équiper une pluralité de tubes du réacteur d'un thermocouple, à limiter le flux de réactifs dans certains tubes du réacteur contenant un thermocouple, à exécuter le processus dans des conditions de réaction voulues, à déterminer un profil de température pour chaque tube du réacteur contenant un thermocouple, à comparer les différences entre les profils de température des tubes du réacteur dans lesquels le flux de réactifs est limité et les profils de température des tubes du réacteur dans lesquels le flux de réactifs n'est pas limité, et à corréler les différences entre les profils de température et des signes d'emballement thermique. Les conditions de réaction pourraient alors être ajustées en réponse aux signes d'emballement thermique.
PCT/US1999/018690 1998-09-22 1999-08-17 Procede d'evaluation d'une reaction d'emballement thermique WO2000017946A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US15874598A 1998-09-22 1998-09-22
US09/158,745 1998-09-22

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Publication Number Publication Date
WO2000017946A2 true WO2000017946A2 (fr) 2000-03-30
WO2000017946A3 WO2000017946A3 (fr) 2000-11-23

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1270065A1 (fr) * 2001-06-26 2003-01-02 Nippon Shokubai Co., Ltd. Appareillage pour effectuer des mesures de pression et de température dans des réacteurs tubulaires
WO2003066216A1 (fr) 2002-02-04 2003-08-14 Siemens Aktiengesellschaft Systeme microfluidique
US7402288B2 (en) * 2001-06-06 2008-07-22 Basf Aktiengesellschaft Reactor for testing catalyst systems
WO2008087306A1 (fr) * 2007-01-09 2008-07-24 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de remplacement des tubes de catalyseur d'un reformeur d'hydrocarbures
EP2075058A1 (fr) 2007-12-20 2009-07-01 MAN DWE GmbH Réacteur à faisceau tubulaire
US7588739B2 (en) * 2003-07-14 2009-09-15 Mitsubishi Rayon Co., Ltd. Fixed bed multitube reactor
WO2022064210A3 (fr) * 2020-09-25 2022-05-05 Johnson Matthey Davy Technologies Limited Perfectionnements apportés ou se rapportant à des thermocouples pour réacteurs tubulaires
WO2022153214A1 (fr) * 2021-01-15 2022-07-21 Cri, Ehf Réacteur de synthèse du méthanol
US11801493B2 (en) 2016-12-02 2023-10-31 Shell Usa, Inc. Methods for conditioning an ethylene epoxidation catalyst and associated methods for the production of ethylene oxide

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US4929798A (en) * 1984-03-05 1990-05-29 Canadian Patents And Development Limited Pseudoadiabatic reactor for exothermal catalytic conversions
EP0873783A1 (fr) * 1997-04-23 1998-10-28 Basf Aktiengesellschaft Dispositif et méthode pour mesure la temperature dans de réacteurs tubulaire

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Publication number Priority date Publication date Assignee Title
US4929798A (en) * 1984-03-05 1990-05-29 Canadian Patents And Development Limited Pseudoadiabatic reactor for exothermal catalytic conversions
EP0873783A1 (fr) * 1997-04-23 1998-10-28 Basf Aktiengesellschaft Dispositif et méthode pour mesure la temperature dans de réacteurs tubulaire

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Title
SMART ARTHURE M, CELANESE CHEMICAL CO: "On-Line Validation of Reactor Temperature Measurement" CHEM ENG PROG, vol. 77, no. 11, 1981, pages 61-63, XP002143723 *

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7402288B2 (en) * 2001-06-06 2008-07-22 Basf Aktiengesellschaft Reactor for testing catalyst systems
SG102053A1 (en) * 2001-06-26 2004-02-27 Nippon Catalytic Chem Ind Reactor filled with solid particle and gas-phase catalytic oxidation with the reactor
US7534339B2 (en) 2001-06-26 2009-05-19 Nippon Shokubai Co., Ltd Reactor filled with solid particle and gas-phase catalytic oxidation with the reactor
EP1270065A1 (fr) * 2001-06-26 2003-01-02 Nippon Shokubai Co., Ltd. Appareillage pour effectuer des mesures de pression et de température dans des réacteurs tubulaires
WO2003066216A1 (fr) 2002-02-04 2003-08-14 Siemens Aktiengesellschaft Systeme microfluidique
EP1472002A1 (fr) * 2002-02-04 2004-11-03 Siemens Aktiengesellschaft Systeme microfluidique
US7588739B2 (en) * 2003-07-14 2009-09-15 Mitsubishi Rayon Co., Ltd. Fixed bed multitube reactor
WO2008087306A1 (fr) * 2007-01-09 2008-07-24 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de remplacement des tubes de catalyseur d'un reformeur d'hydrocarbures
US8355891B2 (en) 2007-01-09 2013-01-15 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method of replacing the catalyst tubes of a hydrocarbon reformer
DE102007061477A1 (de) 2007-12-20 2009-07-02 Man Dwe Gmbh Rohrbündelreaktor
EP2075058A1 (fr) 2007-12-20 2009-07-01 MAN DWE GmbH Réacteur à faisceau tubulaire
US8524156B2 (en) 2007-12-20 2013-09-03 Man Dwe Gmbh Tube bundle reactor
US11801493B2 (en) 2016-12-02 2023-10-31 Shell Usa, Inc. Methods for conditioning an ethylene epoxidation catalyst and associated methods for the production of ethylene oxide
WO2022064210A3 (fr) * 2020-09-25 2022-05-05 Johnson Matthey Davy Technologies Limited Perfectionnements apportés ou se rapportant à des thermocouples pour réacteurs tubulaires
WO2022153214A1 (fr) * 2021-01-15 2022-07-21 Cri, Ehf Réacteur de synthèse du méthanol
US11738317B2 (en) 2021-01-15 2023-08-29 CRI, hf Reactor for synthesizing methanol or other products

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