US20020048541A1 - Reactor for performing a strongly heat-conditioned catalytic reaction - Google Patents

Reactor for performing a strongly heat-conditioned catalytic reaction Download PDF

Info

Publication number
US20020048541A1
US20020048541A1 US09/931,177 US93117701A US2002048541A1 US 20020048541 A1 US20020048541 A1 US 20020048541A1 US 93117701 A US93117701 A US 93117701A US 2002048541 A1 US2002048541 A1 US 2002048541A1
Authority
US
United States
Prior art keywords
reaction
reactor
process fluid
channels
synthesis
Prior art date
Legal status (The legal status 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 status listed.)
Abandoned
Application number
US09/931,177
Inventor
Nicole Schodel
Manfred Sotzek
Wolfgang Sussmann
Roland Walzl
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SUSSMANN, WOLFGANG, SCHODEL, NICOLE, SOTZEK, MANFRED, WALZL, ROLAND
Publication of US20020048541A1 publication Critical patent/US20020048541A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00Heat-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
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24Stationary reactors without moving elements inside
    • B01J19/248Reactors comprising multiple separated flow channels
    • B01J19/249Plate-type reactors
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/02Preparation of sulfur; Purification
    • C01B17/04Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0413Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the combustion step
    • C01B17/0417Combustion reactors
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/02Preparation of sulfur; Purification
    • C01B17/04Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/046Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process without intermediate formation of sulfur dioxide
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/80Apparatus
    • C01B17/803Converters
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01CAMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00Ammonia; Compounds thereof
    • C01C1/02Preparation, purification or separation of ammonia
    • C01C1/04Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/03Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/08Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
    • C07C5/09Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C9/00Aliphatic saturated hydrocarbons
    • C07C9/02Aliphatic saturated hydrocarbons with one to four carbon atoms
    • C07C9/04Methane
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07DHETEROCYCLIC COMPOUNDS
    • C07D301/00Preparation of oxiranes
    • C07D301/02Synthesis of the oxirane ring
    • C07D301/03Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
    • C07D301/04Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen
    • C07D301/08Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34Apparatus, reactors
    • C10G2/341Apparatus, reactors with stationary catalyst bed
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2451Geometry of the reactor
    • B01J2219/2453Plates arranged in parallel
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2451Geometry of the reactor
    • B01J2219/2456Geometry of the plates
    • B01J2219/2458Flat plates, i.e. plates which are not corrugated or otherwise structured, e.g. plates with cylindrical shape
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2461Heat exchange aspects
    • B01J2219/2462Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2474Mixing means, e.g. fins or baffles attached to the plates
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2476Construction materials
    • B01J2219/2477Construction materials of the catalysts
    • B01J2219/2479Catalysts coated on the surface of plates or inserts
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2491Other constructional details
    • B01J2219/2497Size aspects, i.e. concrete sizes are being mentioned in the classified document
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24Stationary reactors without moving elements inside
    • B01J2219/2401Reactors comprising multiple separate flow channels
    • B01J2219/245Plate-type reactors
    • B01J2219/2491Other constructional details
    • B01J2219/2498Additional structures inserted in the channels, e.g. plates, catalyst holding meshes
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/52Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the invention relates to a reactor for performing heat-conditioned catalytic reaction within a process fluid, equipped with plates that are arranged parallel to one another at a distance to form flat channels with lateral boundary areas that face one another, whereby a portion of the channels contain a solid catalyst and carry the process fluid, and another portion of the channels guide a heat transfer medium in indirect heat contact with the process fluid.
  • a tube reactor with catalyst particles in the tubes is known from the journal Hydrocarbon Processing, March 1997, page 134.
  • the tubes are cooled on the jacket side of the reactor with boiling water or other suitable heat transfer media.
  • the division of the reaction chamber and the catalyst particles in several tubes guarantees that in the case of a malfunction, a self-accelerating reaction, caused by local superheating, is limited to a reaction tube and does not extend to the entire reactor.
  • the reactor design has proven its value, but it also exhibits several drawbacks.
  • the reactor jacket must often be designed for high coolant pressure. As a result, the jacket is very thick and thus costly, and the reactor is difficult to transport.
  • a plate heat exchanger with a catalyst solid bed is known from DE 198 04 806 A1. It contains cooled separating walls in the bed.
  • the reactor jacket must be designed only for the pressure of the reaction gas; the reactor requires no tube bottoms. It is thus lighter overall than a tube reactor and therefore can also be made from high-grade steel at lower cost.
  • a prior art reactor closely related to the present invention is disclosed in U.S. Pat. No. 3,528,783. Rectangular channels formed with bent sheets direct, on the one hand, a reaction medium and, on the other hand, a heat transfer medium.
  • the channels through which the reaction medium flows contain solid catalyst material. These channels are sandwich-like positioned between channels through which the heat transfer medium flows.
  • An object of the invention is therefore to avoid the above-mentioned drawbacks.
  • a reactor comprising plates that are arranged parallel to one another at a distance and form flat channels with lateral boundary areas that face one another.
  • a portion of the channels contain a solid catalyst and carry a process fluid, and another portion of the channels guide a heat transfer medium in indirect heat contact with the process fluid.
  • the plates are flat or are provided with grooves or ribs and are coated at least partially with catalyst on the surface that faces the process fluid.
  • a characteristic feature of the invention is that the plates are flat, or are provided with grooves or ribs, and are coated at least partially with the catalyst on the surface that faces the process fluid.
  • a significant temperature profile cannot form crosswise to the direction of flow, since the heat input or output always takes the shortest path, namely through the plates and the layer that is applied to the plates.
  • a uniform flow through all of the channels is achieved even more readily than in catalytic-bed channels (or tubes).
  • heat transfer zones can be formed in parts of the reactor which do not also provide catalytic reaction.
  • the lateral boundary areas can be designed as jacket pieces, which form a pressure-resistant cuboid block with channels formed by the plates and collectors for the process fluid and for the heat transfer medium.
  • An advantage of this embodiment is that the reactor can be operated, both on the process fluid side and on the heat transfer medium side, at operating pressures of more than 25 bar.
  • the channels that carry the process fluid can contain corrugated and pleated sheets (fins) that form passages for the process fluid.
  • the heat transfer between the process fluid and the heat transfer medium is improved by the fins.
  • the fins can be perforated and thus form flow connections between the passages.
  • the fins can be coated on both sides at least partially with catalyst material. With the thickness of the coating being the same, in this way a more effective catalyst surface is installed per reactor volume.
  • the width of the passages for process fluid formed by the coated fins is preferably about 0.5-5 mm.
  • the catalyst layer can contain a support medium.
  • the catalyst layer can have a layer thickness of, for example, 1 to 500 ⁇ m, preferably 10 to 100 ⁇ m.
  • the distance between plates (without catalyst coating) is preferably about 2.5-20 mm.
  • the reactor according to the invention can be made of aluminum, steel or high-grade steel.
  • the reactor according to the invention is used especially advantageously when an endothermic reaction or an exothermic reaction is performed in the reactor. Without limiting the usability of the reactor, the following are examples of processes in which the reactor can be used.
  • the reactor according to the invention can advantageously be used in:
  • FIG. 1 shows a reactor according to the invention in three-dimensional representation.
  • a reactor with a volume of 13 m 3 can be used Length 6 m Width 1.2 m Depth 1.8 m Weight without catalyst 16 t
  • the catalyst-coated channels have a pressure drop of about 150 mbar.
  • a comparable reactor according to the prior art has a volume that is greater by a factor of 4 to 10.
  • the catalyst can comprise a noble metal, e.g., palladdium, and a support material, e.g., aluminum oxide.
  • the catalyst layer can be applied as a coating, e.g., a washcoat. See, e.g., Handbook of Heterogeneous Catalysis, Vol. 14, 11 Environmental Catalysis-Mobile Sources, pp. 1572-83.
  • the catalyst layer can also be applied by chemical vapor deposition (CVD)as described, e.g., in the Handbook of Heterogeneous Catalysis, Vol. 2, pp. 853-55.
  • FIG. 1 illustrates an embodiment of the invention.
  • Plates 1 that are arranged parallel to one another at a distance and form channels 2 , for a process fluid, and channels 3 , for a cooling medium, with lateral boundary areas that face one another.
  • the boundary areas can be designed as plates 4 (shown as broken lines in the figure) or as webs 5 between plates 1 and/or (not shown in the figure) between fins and plates 1 .
  • the plate surfaces inside of the channels that guide the process fluid are coated with catalyst material 6 .
  • collectors for the process fluid and the cooling medium which together with the plates form a dimensionally stable and pressure-resistant reactor 7 .
  • An acetylene-containing flow 8 is fed to, for example, reactor 7 .
  • the acetylene is hydrogenated to ethylene in the presence of catalyst material 6 , and a flow 9 containing ethylene is obtained.
  • Process heat that is formed as a result of the catalytic reaction is withdrawn from the plates by the flow of liquid butane 10 , which is fed to channels 3 . As heat is taken up, the butane is evaporated and withdrawn as a gaseous flow 11 .

Abstract

The invention relates to a reactor for performing a strongly heat-conditioned catalytic reaction in a process fluid, equipped with plates that are arranged parallel to one another at a distance and that form flat channels with lateral boundary areas that face one another, whereby a portion of the channels contains a solid catalyst and carries the process fluid, and another portion of the channels guides a heat transfer medium in indirect heat contact with the process fluid.
According to the invention, plates (1) are flat or are provided with grooves or ribs, and plates (1) are coated at least partially with catalyst (6) on the surface that faces the process fluid.

Description

  • The invention relates to a reactor for performing heat-conditioned catalytic reaction within a process fluid, equipped with plates that are arranged parallel to one another at a distance to form flat channels with lateral boundary areas that face one another, whereby a portion of the channels contain a solid catalyst and carry the process fluid, and another portion of the channels guide a heat transfer medium in indirect heat contact with the process fluid. [0001]
  • BACKGROUND OF THE INVENTION
  • Catalytic processes are often connected with high energy conversions. In most cases, a specific temperature range must be maintained to achieve a high conversion and high yield of desirable products (selectivity,) and to avoid damaging the catalyst that is used. Adiabatic reactors with intermediate cooling result in a considerable number of components or in a reactor of expensive design. Solid-bed reactors with cooling and heating devices in the bed are also known. In most cases, these are tubular reactors with a solid bed and with heat-transfer-medium-guiding tubes in the solid bed, as they are described in all standard works on reaction technology, for example in Ullmann's Encyclopedia of Industrial Chemistry, VCH 1992, Vol. 4B. A reactor with coiled coolant tubes in a solid bed is disclosed in M. Lehmbeck's “Linde Isothermal Reactor for Methanol Synthesis” 41 (1986), [0002] pages 5 to 8.
  • A tube reactor with catalyst particles in the tubes is known from the journal Hydrocarbon Processing, March 1997, page 134. The tubes are cooled on the jacket side of the reactor with boiling water or other suitable heat transfer media. The division of the reaction chamber and the catalyst particles in several tubes guarantees that in the case of a malfunction, a self-accelerating reaction, caused by local superheating, is limited to a reaction tube and does not extend to the entire reactor. The reactor design has proven its value, but it also exhibits several drawbacks. [0003]
  • In practice, the reactor jacket must often be designed for high coolant pressure. As a result, the jacket is very thick and thus costly, and the reactor is difficult to transport. [0004]
  • In the case of a large diameter, the tube bottoms are also very thick and jeopardized by thermal stress. [0005]
  • The many reaction tubes can be filled only at great expense. In particular, attention must be paid to uniform filling with equal pressure loss in the various tubes, so that a sparingly loaded reaction tube because of a large pressure drop does not become overheated. [0006]
  • Because of the high weight, in most cases C-steel is used, although rust is thus unavoidable. For many reactions, however, rust acts as a catalyst poison. [0007]
  • A plate heat exchanger with a catalyst solid bed is known from DE 198 04 806 A1. It contains cooled separating walls in the bed. The reactor jacket must be designed only for the pressure of the reaction gas; the reactor requires no tube bottoms. It is thus lighter overall than a tube reactor and therefore can also be made from high-grade steel at lower cost. [0008]
  • A prior art reactor closely related to the present invention is disclosed in U.S. Pat. No. 3,528,783. Rectangular channels formed with bent sheets direct, on the one hand, a reaction medium and, on the other hand, a heat transfer medium. The channels through which the reaction medium flows contain solid catalyst material. These channels are sandwich-like positioned between channels through which the heat transfer medium flows. [0009]
  • The drawback to this multi-layer catalytic reactor—as also to other catalytic-bed reactors—is that during operation a temperature profile forms in the channels that contain the catalyst material crosswise to the direction of flow of the reaction medium. As a result, only an average temperature can be set. An optimal conversion and an optimal selectivity can therefore not be achieved in principle. In addition, a local superheating of the catalyst material and an overflowing of the reaction in a way that is undesirable or even hazardous cannot be ruled out. In addition, the above-mentioned multi-layer reactor has the drawback that it requires a pressure-resistant outer container. [0010]
  • SUMMARY OF THE INVENTION
  • An object of the invention is therefore to avoid the above-mentioned drawbacks. [0011]
  • Upon further study of the specification and appended claims, further objects and advantages of this invention will become apparent to those skilled in the art. [0012]
  • These objects are achieved according to the invention by a reactor comprising plates that are arranged parallel to one another at a distance and form flat channels with lateral boundary areas that face one another. A portion of the channels contain a solid catalyst and carry a process fluid, and another portion of the channels guide a heat transfer medium in indirect heat contact with the process fluid. The plates are flat or are provided with grooves or ribs and are coated at least partially with catalyst on the surface that faces the process fluid. [0013]
  • A characteristic feature of the invention is that the plates are flat, or are provided with grooves or ribs, and are coated at least partially with the catalyst on the surface that faces the process fluid. With the reactor according to the invention, a significant temperature profile cannot form crosswise to the direction of flow, since the heat input or output always takes the shortest path, namely through the plates and the layer that is applied to the plates. In addition, a uniform flow through all of the channels is achieved even more readily than in catalytic-bed channels (or tubes). Also, in the case of only partial coating with catalyst, heat transfer zones can be formed in parts of the reactor which do not also provide catalytic reaction. [0014]
  • In an embodiment of the reactor according to the invention, advantageously the lateral boundary areas can be designed as jacket pieces, which form a pressure-resistant cuboid block with channels formed by the plates and collectors for the process fluid and for the heat transfer medium. An advantage of this embodiment is that the reactor can be operated, both on the process fluid side and on the heat transfer medium side, at operating pressures of more than 25 bar. [0015]
  • The channels that carry the process fluid can contain corrugated and pleated sheets (fins) that form passages for the process fluid. The heat transfer between the process fluid and the heat transfer medium is improved by the fins. [0016]
  • The fins can be perforated and thus form flow connections between the passages. [0017]
  • The fins can be coated on both sides at least partially with catalyst material. With the thickness of the coating being the same, in this way a more effective catalyst surface is installed per reactor volume. The width of the passages for process fluid formed by the coated fins is preferably about 0.5-5 mm. [0018]
  • The catalyst layer can contain a support medium. [0019]
  • The catalyst layer can have a layer thickness of, for example, 1 to 500 μm, preferably 10 to 100 μm. [0020]
  • The distance between plates (without catalyst coating) is preferably about 2.5-20 mm. [0021]
  • The reactor according to the invention can be made of aluminum, steel or high-grade steel. [0022]
  • The reactor according to the invention is used especially advantageously when an endothermic reaction or an exothermic reaction is performed in the reactor. Without limiting the usability of the reactor, the following are examples of processes in which the reactor can be used. [0023]
  • The reactor according to the invention can advantageously be used in: [0024]
  • Synthesis of methanol, [0025]
  • Synthesis of higher alcohols, [0026]
  • Hydrogenation of hydrocarbons, [0027]
  • Selective hydrogenation of C[0028] 2H2 to C2H4,
  • Non-selective hydrogenation of C[0029] 2H4 to C2H6,
  • Methanation or synthesis of methane, [0030]
  • Carbon monoxide conversion, [0031]
  • Fischer-Tropsch synthesis, [0032]
  • Epoxidation, [0033]
  • Synthesis of ethylene oxide, [0034]
  • Claus reaction, [0035]
  • Direct oxidation of H[0036] 2S to sulfur,
  • Oxidation of SO[0037] 2 to SO3
  • or in NH[0038] 3 synthesis.
  • BRIEF DESCRIPTION OF THE DRAWINGS
  • Various other features and attendant advantages of the present invention will be more fully appreciated as the same becomes better understood when considered in conjunction with the accompanying drawing. FIG. 1 shows a reactor according to the invention in three-dimensional representation. [0039]
  • In the foregoing and in the following examples, all temperatures are set forth uncorrected in degrees Celsius; and, unless otherwise indicated, all parts and percentages are by weight. [0040]
  • The entire disclosure of all applications, patents and publications, cited above and below, and of corresponding German Application No. 100 40 209.7, filed Aug. 17, 2000, is hereby incorporated by reference.[0041]
  • EXAMPLE
  • In a selective hydrogenation of acetylene to ethylene with a reactor according to the invention, with fins, operated under the following parameters [0042]
    Pressure 31 bar
    Temperature 70-80° C.
    Throughput 170,000 kg/h
  • and with use of liquid butane for cooling, a reactor with a volume of 13 m[0043] 3 can be used
    Length 6 m
    Width 1.2 m
    Depth 1.8 m
    Weight without catalyst 16 t
  • The catalyst-coated channels have a pressure drop of about 150 mbar. A comparable reactor according to the prior art has a volume that is greater by a factor of 4 to 10. [0044]
  • The catalyst can comprise a noble metal, e.g., palladdium, and a support material, e.g., aluminum oxide. The catalyst layer can be applied as a coating, e.g., a washcoat. See, e.g., Handbook of Heterogeneous Catalysis, Vol. 14, 11 Environmental Catalysis-Mobile Sources, pp. 1572-83. The catalyst layer can also be applied by chemical vapor deposition (CVD)as described, e.g., in the Handbook of Heterogeneous Catalysis, Vol. 2, pp. 853-55. [0045]
  • The invention is explained in more detail in conjunction with the following description of FIG. 1 which illustrates an embodiment of the invention. [0046]
  • The principle design of such a reactor is diagrammatically represented in the figure. The function of the reactor is described based on the example of the selective hydrogenation of acetylene to ethylene. [0047]
  • [0048] Plates 1 that are arranged parallel to one another at a distance and form channels 2, for a process fluid, and channels 3, for a cooling medium, with lateral boundary areas that face one another. The boundary areas can be designed as plates 4 (shown as broken lines in the figure) or as webs 5 between plates 1 and/or (not shown in the figure) between fins and plates 1. The plate surfaces inside of the channels that guide the process fluid are coated with catalyst material 6. Not shown in the figure are collectors for the process fluid and the cooling medium, which together with the plates form a dimensionally stable and pressure-resistant reactor 7.
  • An acetylene-containing [0049] flow 8 is fed to, for example, reactor 7. In channels 2, the acetylene is hydrogenated to ethylene in the presence of catalyst material 6, and a flow 9 containing ethylene is obtained. Process heat that is formed as a result of the catalytic reaction is withdrawn from the plates by the flow of liquid butane 10, which is fed to channels 3. As heat is taken up, the butane is evaporated and withdrawn as a gaseous flow 11.
  • By removing heat right at the point of origin, secondary reactions such as formation of ethane or oligomers (e.g., anthracene oil, green oil) are largely avoided. Thus, by the more reliable operation of the reactor according to the invention, a high ethylene yield is achieved. [0050]
  • The preceding examples can be repeated with similar success by substituting the generically or specifically described reactants and/or operating conditions of this invention for those used in the preceding examples. [0051]
  • From the foregoing description, one skilled in the art can easily ascertain the essential characteristics of this invention and, without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various usages and conditions. [0052]

Claims (24)

1. A reactor for performing a heat-conditioned catalytic reaction in a process fluid, said reactor comprising: plates that are arranged parallel to one another at a distance and that form flat channels with lateral boundary areas that face one another, wherein a portion of said channels contain a solid catalyst and carry a process fluid, and another portion of said channels carry a heat transfer medium in indirect heat contact with the process fluid, wherein said plates are flat or are provided with grooves or ribs and are coated at least partially with a catalyst on the surface that faces the process fluid.
2. A reactor according to claim 1, wherein said lateral boundary areas are jacket pieces, which form a pressure-resistant cuboid block with said channels, plates, and with collectors for the process fluid and for the heat transfer medium.
3. A reactor according to claim 1, wherein the channels which carry the process fluid contain corrugated or pleated sheets which form passages for the flow of process fluid.
4. A reactor according to claim 3, wherein said sheets are perforated and thereby provide flow connections between said passages.
5. A reactor according to claim 3, wherein said sheets are coated at least partially on both sides with catalyst material.
6. A reactor according to claim 1, wherein said catalyst layer contains a support medium.
7. A reactor according to claim 1, wherein said catalyst layer has a thickness of 1-500 μm.
8. A reactor according to claim 1, wherein said catalyst layer has a thickness of 10-100 μm.
9. A reactor according to claim 1, wherein said reactor is made of aluminum.
10. A reactor according to claim 1, wherein said reactor is made of steel or high-grade steel.
11. In a method of performing an endothermic or exothermic reaction within a reaction, the improvement wherein said reactor is according to claim 1.
12. A method according to claim 11, wherein said reaction is synthesis of methanol or synthesis of higher alcohols.
13. A method according to claim 11, wherein said reaction is hydrogenation of hydrocarbons.
14. A method according to claim 13, wherein said reaction is selective hydrogenation of C2H2 to C2H4.
15. A method according to claim 13, wherein said reaction is non-selective hydrogenation of C2H4 to C2H6.
16. A method according to claim 11, wherein said reaction is methanation or in the synthesis of methane.
17. A method according to claim 11, wherein said reaction is conversion of carbon monoxide.
18. A method according to claim 11, wherein said reaction is Fischer-Tropsch synthesis.
19. A method according to claim 11, wherein said reaction is epoxidation.
20. A method according to claim 19, wherein said reaction is synthesis of ethylene oxide.
21. A method according to claim 11, wherein said reaction is Claus reaction.
22. A method according to claim 11, wherein said reaction is direct oxidation of H2S to sulfur.
23. A method according to claim 11, wherein said reaction is oxidation of SO2 to SO3.
24. A method according to claim 11, wherein said reaction is synthesis of NH3.
US09/931,177 2000-08-17 2001-08-17 Reactor for performing a strongly heat-conditioned catalytic reaction Abandoned US20020048541A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10040209.7 2000-08-17
DE10040209A DE10040209A1 (en) 2000-08-17 2000-08-17 Reactor for carrying out a strongly heat-toned catalytic reaction

Publications (1)

Publication Number Publication Date
US20020048541A1 true US20020048541A1 (en) 2002-04-25

Family

ID=7652739

Family Applications (1)

Application Number Title Priority Date Filing Date
US09/931,177 Abandoned US20020048541A1 (en) 2000-08-17 2001-08-17 Reactor for performing a strongly heat-conditioned catalytic reaction

Country Status (5)

Country Link
US (1) US20020048541A1 (en)
EP (1) EP1180395B1 (en)
JP (1) JP2002126498A (en)
AT (1) ATE387957T1 (en)
DE (2) DE10040209A1 (en)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004058665A2 (en) * 2002-12-20 2004-07-15 Basf Aktiengesellschaft Method for the hydration of hydrocarbon compounds
US20040228781A1 (en) * 2003-05-16 2004-11-18 Tonkovich Anna Lee Microchannel with internal fin support for catalyst or sorption medium
US20050165121A1 (en) * 2004-01-28 2005-07-28 Yong Wang Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US20060115393A1 (en) * 2004-11-29 2006-06-01 Reinke Michael J Catalytic reactor/heat exchanger reactor
US20070004810A1 (en) * 2005-06-30 2007-01-04 Yong Wang Novel catalyst and fischer-tropsch synthesis process using same
US20100224616A1 (en) * 2009-03-09 2010-09-09 Jamco Corporation Steam oven for aircraft including safety valve for water leakage prevention purposes
US20110002818A1 (en) * 2003-05-16 2011-01-06 Anna Lee Tonkovich Microchannel with internal fin support for catalyst or sorption medium
WO2011148067A1 (en) * 2010-05-25 2011-12-01 IFP Energies Nouvelles Method for the conversion of synthesis gas into vapor, and apparatus for carrying out said method
WO2013126449A1 (en) * 2012-02-21 2013-08-29 Ceramatec, Inc. Compact ft combined with micro-fibrous supported nano-catalyst
US9006298B2 (en) 2012-08-07 2015-04-14 Velocys, Inc. Fischer-Tropsch process
US9011788B2 (en) 2012-02-17 2015-04-21 Ceramatec, Inc Advanced fischer tropsch system
US9023900B2 (en) 2004-01-28 2015-05-05 Velocys, Inc. Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US9199215B2 (en) 2012-02-21 2015-12-01 Ceramatec, Inc. Compact Fischer Tropsch system with integrated primary and secondary bed temperature control
WO2017089935A1 (en) * 2015-11-23 2017-06-01 Sabic Global Technologies B.V. Structural catalyst with internal heat transfer system for exothermic and endothermic reactions
WO2017174553A1 (en) * 2016-04-08 2017-10-12 Ineos Europe Ag Polymerisation unit and polymerisation process
CN109414675A (en) * 2016-07-06 2019-03-01 英尼奥斯欧洲股份公司 Polymerization
US10358604B2 (en) 2015-06-12 2019-07-23 Velocys, Inc. Method for stopping and restarting a Fischer-Tropsch process
EP4327929A1 (en) * 2022-08-26 2024-02-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Methanol synthesis plate reactor
EP4327930A1 (en) * 2022-08-26 2024-02-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Multi-stage reactor for carrying out exothermic equilibrium reactions

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10139967B4 (en) * 2001-08-14 2006-05-04 Gea Saturn Gmbh Apparatus for recovering gaseous products by catalytic gas phase reaction
EP1479883A1 (en) 2003-05-10 2004-11-24 Universität Stuttgart Method and device for exhaust gas purification
JP2005206770A (en) * 2004-01-19 2005-08-04 Ics Kk Manufacturing process of fatty acid ester and fuel containing the fatty acid ester
DE102005002129A1 (en) * 2005-01-17 2006-07-20 Basf Ag Reactor and process in a reactor with a reactor interior, which is divided into two or more separate reaction spaces
US8240367B2 (en) 2007-06-28 2012-08-14 Exxonmobil Research And Engineering Company Plate heat exchanger port insert and method for alleviating vibrations in a heat exchanger
WO2011079848A2 (en) * 2009-12-18 2011-07-07 Robert Otto Renfer Heater
WO2014159555A1 (en) 2013-03-12 2014-10-02 Battelle Memorial Institute Reactor incorporating a heat exchanger
CN110013801A (en) * 2018-01-10 2019-07-16 何巨堂 The hydrocarbon material hydrogenator system of socket type containing upper reaction zone and product gas-liquid separation zone

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3528783A (en) * 1964-06-16 1970-09-15 Marston Excelsior Ltd Multilayer catalytic reactor
US4043945A (en) * 1974-11-11 1977-08-23 Hitachi, Ltd. Method of producing thin layer methanation reaction catalyst
US6159358A (en) * 1998-09-08 2000-12-12 Uop Llc Process and apparatus using plate arrangement for reactant heating and preheating
US6168765B1 (en) * 1998-09-08 2001-01-02 Uop Llc Process and apparatus for interbed injection in plate reactor arrangement

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03181338A (en) * 1989-12-11 1991-08-07 Gebr Sulzer Ag Catalytic element and reactor for use for catalytic reaction
US5846494A (en) * 1992-04-30 1998-12-08 Gaiser; Gerd Reactor for catalytically processing gaseous fluids
US5538700A (en) * 1994-12-22 1996-07-23 Uop Process and apparatus for controlling temperatures in reactant channels
JPH0947664A (en) * 1995-05-31 1997-02-18 Seda Giken:Kk Catalytic reactor
DE19725378A1 (en) * 1997-06-16 1998-12-17 Gerhard Friedrich Compact fixed bed reactor for catalytic reactions with integrated heat exchange
US6118038A (en) * 1998-09-08 2000-09-12 Uop Llc Arrangement and process for indirect heat exchange with high heat capacity fluid and simultaneous reaction

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3528783A (en) * 1964-06-16 1970-09-15 Marston Excelsior Ltd Multilayer catalytic reactor
US4043945A (en) * 1974-11-11 1977-08-23 Hitachi, Ltd. Method of producing thin layer methanation reaction catalyst
US6159358A (en) * 1998-09-08 2000-12-12 Uop Llc Process and apparatus using plate arrangement for reactant heating and preheating
US6168765B1 (en) * 1998-09-08 2001-01-02 Uop Llc Process and apparatus for interbed injection in plate reactor arrangement

Cited By (53)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004058665A3 (en) * 2002-12-20 2004-09-16 Basf Ag Method for the hydration of hydrocarbon compounds
WO2004058665A2 (en) * 2002-12-20 2004-07-15 Basf Aktiengesellschaft Method for the hydration of hydrocarbon compounds
CN100423826C (en) * 2003-05-16 2008-10-08 万罗赛斯公司 Microchannel with internal fin support for catalyst or sorption medium
US20040228781A1 (en) * 2003-05-16 2004-11-18 Tonkovich Anna Lee Microchannel with internal fin support for catalyst or sorption medium
WO2004103550A1 (en) * 2003-05-16 2004-12-02 Velocys Inc. Microchannel with internal fin support for catalyst or support medium
US8580211B2 (en) 2003-05-16 2013-11-12 Velocys, Inc. Microchannel with internal fin support for catalyst or sorption medium
EP2463024A1 (en) * 2003-05-16 2012-06-13 Velocys Inc. Microchannel with internal fin support for catalyst or sorption medium
US7896935B2 (en) * 2003-05-16 2011-03-01 Velocys, Inc. Process of conducting reactions or separation in a microchannel with internal fin support for catalyst or sorption medium
US20110002818A1 (en) * 2003-05-16 2011-01-06 Anna Lee Tonkovich Microchannel with internal fin support for catalyst or sorption medium
AU2004241943B2 (en) * 2003-05-16 2010-05-13 Velocys Inc. Microchannel with internal fin support for catalyst or support medium
US7220390B2 (en) 2003-05-16 2007-05-22 Velocys, Inc. Microchannel with internal fin support for catalyst or sorption medium
US20070140955A1 (en) * 2003-05-16 2007-06-21 Tonkovich Anna L Microchannel with internal fin support for catalyst or sorption medium
US7084180B2 (en) 2004-01-28 2006-08-01 Velocys, Inc. Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US8188153B2 (en) 2004-01-28 2012-05-29 Velocys, Inc. Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US9023900B2 (en) 2004-01-28 2015-05-05 Velocys, Inc. Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US7722833B2 (en) 2004-01-28 2010-05-25 Velocys, Inc. Microchannel reactor
US9453165B2 (en) 2004-01-28 2016-09-27 Velocys, Inc. Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US20060251552A1 (en) * 2004-01-28 2006-11-09 Yong Wang Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
EP2955215A1 (en) * 2004-01-28 2015-12-16 Velocys, Inc. Fischer-tropsch synthesis using microchannel technology
US20050165121A1 (en) * 2004-01-28 2005-07-28 Yong Wang Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
WO2005075606A1 (en) * 2004-01-28 2005-08-18 Velocys Inc. Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
EP2607455A1 (en) * 2004-01-28 2013-06-26 Velocys Inc. Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
EP2607456A1 (en) * 2004-01-28 2013-06-26 Velocys Inc. Fischer-Tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor
US20060115393A1 (en) * 2004-11-29 2006-06-01 Reinke Michael J Catalytic reactor/heat exchanger reactor
US7618598B2 (en) 2004-11-29 2009-11-17 Modine Manufacturing Company Catalytic reactor/heat exchanger
US20070004810A1 (en) * 2005-06-30 2007-01-04 Yong Wang Novel catalyst and fischer-tropsch synthesis process using same
US20100224616A1 (en) * 2009-03-09 2010-09-09 Jamco Corporation Steam oven for aircraft including safety valve for water leakage prevention purposes
FR2960451A1 (en) * 2010-05-25 2011-12-02 Inst Francais Du Petrole STEAM CONVERSION METHOD FOR SYNTHESIS GAS AND APPARATUS FOR CARRYING OUT SAID METHOD
WO2011148067A1 (en) * 2010-05-25 2011-12-01 IFP Energies Nouvelles Method for the conversion of synthesis gas into vapor, and apparatus for carrying out said method
US9011788B2 (en) 2012-02-17 2015-04-21 Ceramatec, Inc Advanced fischer tropsch system
WO2013126449A1 (en) * 2012-02-21 2013-08-29 Ceramatec, Inc. Compact ft combined with micro-fibrous supported nano-catalyst
US9162935B2 (en) 2012-02-21 2015-10-20 Ceramatec, Inc. Compact FT combined with micro-fibrous supported nano-catalyst
US9199215B2 (en) 2012-02-21 2015-12-01 Ceramatec, Inc. Compact Fischer Tropsch system with integrated primary and secondary bed temperature control
US9359271B2 (en) 2012-08-07 2016-06-07 Velocys, Inc. Fischer-Tropsch process
US9006298B2 (en) 2012-08-07 2015-04-14 Velocys, Inc. Fischer-Tropsch process
US10358604B2 (en) 2015-06-12 2019-07-23 Velocys, Inc. Method for stopping and restarting a Fischer-Tropsch process
US11661553B2 (en) 2015-06-12 2023-05-30 Velocys, Inc. Synthesis gas conversion process
US10752843B2 (en) 2015-06-12 2020-08-25 Velocys, Inc. Synthesis gas conversion process
WO2017089935A1 (en) * 2015-11-23 2017-06-01 Sabic Global Technologies B.V. Structural catalyst with internal heat transfer system for exothermic and endothermic reactions
US10737236B2 (en) 2015-11-23 2020-08-11 Sabic Global Technologies B.V. Structural catalyst with internal heat transfer system for exothermic and endothermic reactions
WO2017174553A1 (en) * 2016-04-08 2017-10-12 Ineos Europe Ag Polymerisation unit and polymerisation process
RU2735540C2 (en) * 2016-04-08 2020-11-03 Инеос Юруоп Аг Polymerisation apparatus and polymerisation method
US11052373B2 (en) 2016-04-08 2021-07-06 Ineos Europe Ag Polymerisation unit and polymerisation process
CN108884192B (en) * 2016-04-08 2021-09-03 英尼奥斯欧洲股份公司 Polymerization apparatus and polymerization method
US11478772B2 (en) 2016-04-08 2022-10-25 Ineos Europe Ag Polymerisation unit and polymerisation process
CN108884192A (en) * 2016-04-08 2018-11-23 英尼奥斯欧洲股份公司 Polyplant and polymerization
KR20190026673A (en) * 2016-07-06 2019-03-13 이네오스 유럽 아게 Polymerization method
CN109414675A (en) * 2016-07-06 2019-03-01 英尼奥斯欧洲股份公司 Polymerization
RU2744598C2 (en) * 2016-07-06 2021-03-11 Инеос Юруоп Аг Polymerization method
US11053331B2 (en) 2016-07-06 2021-07-06 Ineos Europe Ag Polymerisation process
KR102359834B1 (en) * 2016-07-06 2022-02-07 이네오스 유럽 아게 polymerization method
EP4327929A1 (en) * 2022-08-26 2024-02-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Methanol synthesis plate reactor
EP4327930A1 (en) * 2022-08-26 2024-02-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Multi-stage reactor for carrying out exothermic equilibrium reactions

Also Published As

Publication number Publication date
EP1180395B1 (en) 2008-03-05
JP2002126498A (en) 2002-05-08
ATE387957T1 (en) 2008-03-15
DE50113680D1 (en) 2008-04-17
DE10040209A1 (en) 2002-02-28
EP1180395A2 (en) 2002-02-20
EP1180395A3 (en) 2002-12-04

Similar Documents

Publication Publication Date Title
US20020048541A1 (en) Reactor for performing a strongly heat-conditioned catalytic reaction
EP1567616B2 (en) Catalytic process
JP5667624B2 (en) Multi-stage, multi-tube shell-and-tube reactor
JP4554359B2 (en) Catalytic oxidative dehydrogenation process and microchannel reactor therefor
US7993599B2 (en) Method for enhancing catalyst selectivity
CA2451416A1 (en) Catalytic reactor
NO330499B1 (en) Catalytic reactor
NO333822B1 (en) Procedure for performing Fisher-Tropsch synthesis
US20170021322A1 (en) Pseudo-isothermal reactor
JPS5892456A (en) Reactor
US8202917B2 (en) Pillow panel reactor and process
KR20010102538A (en) Method of Gas Phase Catalytic Oxidation to Give Maleic Acid Anhydride
US6676906B1 (en) Reactor for carrying out reactions having a high enthalpy change
JPS6124372B2 (en)
JP4875283B2 (en) Reactor for chemical conversion of raw material and catalyst using cross flow while applying heat
WO2013075143A1 (en) Core in kettle reactor, methods for using, and methods of making
CA2660473C (en) Process and reactor for carrying out exothermic and endothermic reactions
US20110060149A1 (en) Process for preparing ethylene oxide
US2853371A (en) High pressure synthesis apparatus
US5728916A (en) Thermal cracking
WO2003027086A1 (en) Method for producing propylene oxide

Legal Events

Date Code Title Description
AS Assignment

Owner name: LINDE AKTIENGESELLSCHAFT, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SCHODEL, NICOLE;SOTZEK, MANFRED;SUSSMANN, WOLFGANG;AND OTHERS;REEL/FRAME:012321/0957;SIGNING DATES FROM 20011018 TO 20011115

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION