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WO2019020705A1 - Réacteur catalytique comprenant un support de particules de catalyseur fibreux - Google Patents

Réacteur catalytique comprenant un support de particules de catalyseur fibreux Download PDF

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Publication number
WO2019020705A1
WO2019020705A1 PCT/EP2018/070207 EP2018070207W WO2019020705A1 WO 2019020705 A1 WO2019020705 A1 WO 2019020705A1 EP 2018070207 W EP2018070207 W EP 2018070207W WO 2019020705 A1 WO2019020705 A1 WO 2019020705A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst particles
support
fibrous
layer
reactor
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.)
Ceased
Application number
PCT/EP2018/070207
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English (en)
Inventor
Roberta Cenni
Emir Zahirovic
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.)
Topsoe AS
Original Assignee
Haldor Topsoe AS
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 Haldor Topsoe AS filed Critical Haldor Topsoe AS
Priority to EP18746175.1A priority Critical patent/EP3658268A1/fr
Priority to CN201880049598.XA priority patent/CN110944740A/zh
Priority to RU2020108186A priority patent/RU2020108186A/ru
Priority to JP2020503976A priority patent/JP2020528345A/ja
Priority to US16/632,957 priority patent/US20200156033A1/en
Publication of WO2019020705A1 publication Critical patent/WO2019020705A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • 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
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/0092—Perforated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00938—Flow distribution elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst

Definitions

  • Catalytic Reactor comprising fibrous catalyst particles support
  • This invention relates to a catalytic reactor comprising a fibrous catalyst particles mesh material.
  • the reactor can be a down-flow trickle flow catalytic reactor which includes at least one packed bed and sometimes a plurality of vertically superimposed packed beds of particulate catalytic material.
  • This type of reactor is used in the petroleum and chemical processing industries for carrying out various catalytic reactions, such as sulphur and nitrogen
  • HDS/HDN conversion of olefins
  • HID hydrogenation of olefins
  • hydrodearomatisation - HDA hydrodearomatisation - HDA
  • metals removal hydrodemetallisation - HDM
  • oxygen conversion hydrodeoxygenation - HDO
  • hydrocracking hydrocracking
  • a further general need of the process industry is that equipment maintenance is rapid. This is both because rapid maintenance implies higher plant availability, and because it involves shorter permanence time of a worker inside the equipment, in this case a reactor, which in turn improves overall safety.
  • 2-10% of the volume available in a reactor is used for inert material retaining catalyst particles, and thus unavailable for catalyst.
  • a fibrous mat having a ratio between width and thickness of at least 50:1 , a significant increase in the volume available for catalyst particles may be obtained.
  • a significant decrease of the time spent for maintaining a reactor may be achieved if the fibrous mat does not trap catalyst particles debris, or if it is so cheap that it can be disposed of and replaced after each cycle.
  • metal wool shall be understood as a material consisting of entangled metal fibres.
  • a fibrous non-woven material shall be understood as a material made from fibres, which are interconnected by entanglement.
  • a fibrous thread shall be understood as a thread made from multiple fibres, which are interconnected by
  • a fibrous woven material shall be understood as a material woven or knitted from fibrous threads.
  • a screen shall be understood as a non-fibrous structured metallic material with the function of retaining particles.
  • the non-fibrous structured metallic material may be woven from single metal strains or made from other metal structures.
  • a structural support shall be understood as material with the function of providing structural support to e.g. a screen or a fibrous material, without necessarily having a particle retaining ability.
  • a catalytic cycle relevant to this discussion shall be understood as the time lagged between the loading and the removal of the catalytic particles.
  • trickle flow shall be understood as a flow of a gas phase and a liquid phase over catalyst particles
  • a trickle flow reactor shall be understood as a reactor suitable for such a flow.
  • resistance to a flow of a gas/liquid mixture is determined as the pressure drop when a mixture comprises a gas and a liquid, where the gas has a viscosity of 0.017 cP and flowing through the fibrous catalyst particles support with a linear flow rate of 250 m/h; and the liquid has a viscosity of 0.15 cP, flowing through the fibrous catalyst particles support with a linear flow rate of 25 m/h
  • the present disclosure relates to a reactor containing of catalyst particles, a layer of fibrous catalyst particles support below said catalyst particles and a lower means of structural support below said catalyst particles , wherein the ratio between width and thickness of the fibrous catalyst particles support is at least 50:1 and the fibrous catalyst particles support allows passage of a liquid, with the associated benefit of such a reactor having increased space for catalyst particles, compared to a reactor with inert particles supporting the catalyst particles.
  • said layer of fibrous catalyst particles support comprises oxide fibres, such as alumina, silica or borosilicates, with the associated benefit of such materials being stable and inert under a wide range of conditions.
  • said layer of fibrous catalyst particles support comprises non-oxide material, such as carbon fibre or metal wool, with the associated benefit of such materials being mechanically stable under a wide range of conditions.
  • said layer of fibrous catalyst particles support comprises oxidic fibers as well as non-oxide material, with the associated benefit of such a fibrous catalyst particles support being thermally stable and structurally strong.
  • said layer of fibrous catalyst particles support is a composite on fibre level, with the associated benefit of such a fibrous catalyst particles support being thermally stable and structurally strong.
  • said layer of fibrous catalyst particles support is a layered composite comprising a layer of a material comprising oxidic fibres and a second layer comprising non-oxide fibres, with the associated benefit of such a fibrous catalyst particles support being thermally stable and structurally strong and simple to produce from existing materials.
  • said layer of fibrous catalyst particles support provides retention for particles with a diameter above 0.1 mm, 0.5 mm or 1 mm, with the associated benefit of such a fibrous catalyst particles support retaining small catalyst particles, as well as debris of such particles, while having a minimal influence on the flow in said reactor.
  • said layer of fibrous catalyst particles support provides a resistance to a flow of a mixture preferably below 1 .5 kPa, even preferably below 0.7 kPa, and even preferably below 0.3 kPa when said mixture comprises a gas with a viscosity of 0.017 cP and flowing through the fibrous catalyst particles support with a linear flow rate of 250 m/h; and a liquid with a viscosity of 0.15 cP, flowing through the fibrous catalyst particles support with a linear flow rate of 25 m/h, with the associated benefit of such a support having minimal influence on the flow in the reactor, and minimizing the requirements for compressor power in the process.
  • said reactor further comprises an upper means of structural support between said catalyst particles and said fibrous catalyst particles support, with the associated benefit of said upper means of structural support stabilizing the position of the fibrous catalyst particles support.
  • said reactor further comprises a means for separating said upper means of support from said lower means of support by a difference of 2 mm, 6 mm or 20 mm, with the associated benefit of avoiding excessive compression of the fibrous catalyst particles support.
  • said reactor further comprises a layer of inert particles between below said catalyst particles and above said fibrous catalyst particles support, with the associated benefit of distributing the mechanical load of catalyst particles over a wider area of said fibrous catalyst particles support.
  • said reactor further comprises a non-fibrous screen, such as a single strand woven structure or a plate having cut slits positioned below said fibrous catalyst particles support, with the associated benefit of stabilizing said layer of fibrous catalyst particles support to better support the bed of catalyst particles above.
  • a non-fibrous screen such as a single strand woven structure or a plate having cut slits positioned below said fibrous catalyst particles support
  • a further aspect of the present disclosure relates to the use of a fibrous material as a fibrous catalyst particles support retaining catalyst particles in a reactor bed of a trickle flow reactor, wherein the fibrous catalyst particles support is positioned below the bed of catalyst particles and above a structural support, with the associated benefit of using such a material over inert particles being a reducing requirement for reactor volume.
  • a catalyst loading comprises inert material to separate the outlet collector from the catalyst bed. Inert material is often in the shape of sphere. We will refer to this material as inert particles in this document. Depending upon the size of the catalyst particles vs.
  • inert particles loading pattern is chosen such to increase the size of the inert particles the further one moves from the catalyst particles towards the outlet collector screen.
  • US 4968651 A discloses a method to prepare inert ceramic support of improved characteristics and US4229418A discloses a method to use inert balls as a filter support.
  • fibrous materials for catalyst support is known from gas phase reactors, but only for very specific applications.
  • US3865555A describes a multiple tube gas phase reactor, have a wire gauze skein as particles support.
  • the height of the support is similar to the width individual tube.
  • US5202097A describes a radial flow gas phase reactor, in which a fibrous material is used a catalyst support and for directing the gas flow.
  • the fibrous material is not permeable for the gas flowing in the reactor.
  • a catalyst particles support comprises a structural support with screens, designed with similar consideration as an outlet collector screen.
  • a bed loading of small-sized catalyst particles above a catalyst particles support as known from the art comprises at least one layer of inert particles between the catalyst particles and the screen of the catalyst particles support. Often, multiple layers of inert particles with different sizes are present, the smallest being in contact with the catalyst particles and the largest being in contact with the catalyst particles support screen.
  • Inert particles may be reused at the end of a catalytic cycle. However, most often inert particles are disposed of after a cycle. Solid particles, comprising debris of catalyst particles and inert particles, have a tendency to get stuck in the openings of metallic screens, both on the catalyst particles support and on the outlet collector. The screens have to be thoroughly cleaned during a catalyst changeover, so that at the start of the operation the effluent flow is evenly distributed over the surface of the screen and the pressure difference across the reactor is not higher than anticipated from design. The cleaning operations for removing the solid particles stuck in the metallic screens tend to be long and cumbersome and thereby increase the downtime of the equipment and the time that operators spend in the confined space.
  • the fibrous catalyst particles support separates a structural support from particulate solid material or two layers of particulate solid material.
  • the fibrous catalyst particles support is laid between a screen and the inert particles.
  • the fibrous catalyst particles support is laid between a screen and catalyst particles.
  • the fibrous catalyst particles support is laid between inert particles and catalyst particles.
  • Fibrous materials useful for the disclosure are impenetrable to catalyst particles and catalyst debris, but they are permeable to gas and liquid. Thus, they offer only a modest filter resistance to the flow of the effluents from the bed above. Fibrous materials useful for the disclosure may change shape during loading and/or during operations, this may cause an increase of the filter resistance.
  • the layer of fibrous catalyst particles support may be a sheet of fibrous material, such as a fiber mat, which in a vertical reactor may be compressed due to the catalyst weight upon loading. The sheet of fibrous material, may be compressed even further, during operations, due to the load of the processed feedstock.
  • the height of the fibrous catalyst particles support which replaces in full or in part the inert particles, as measured during and after catalyst loading, should be as low as possible. This has the further advantage to minimize the pressure drop across the fibrous catalyst particles support.
  • Typical loadings of inert particles have a height in the range of 100-300 mm.
  • the height of the fibrous catalyst particles support after compression is at least less than the loading height of inert particles, and preferably much shorter, for example 10-20 mm, or 6-10 mm, or even less than 6 mm.
  • the flow resistance of a suitable fibrous catalyst particles support is so low that a reactor comprising a fiber mat has same or lower pressure drop compared to a reactor as known from the art, comprising the same loading of catalyst, but not part or all of the inert particles.
  • Fibrous materials suitable for the disclosure are inert in the reaction
  • Suitable fibrous materials are inexpensive and easy to dispose, such that at the end of a cycle the fibrous material may be disposed of and replaced by a new. This eliminates the need to cumbersome and lengthy cleaning operation of the screen.
  • fibrous materials which possess the above mentioned properties, and therefore will be suitable for use in catalytic reactors, some examples are glass wools, fiberglass, ceramic mats or blankets, metal fibers, metal wool and synthetic materials.
  • the materials used must of course be compatible with the conditions inside the process unit, in terms of temperature, reactants, flow and pressure. Ceramic mats or blankets fibers made for example by alumina, silica, borosilicate and other glass or ceramic materials are compatible with a great number of reactive environments.
  • Metal fibers may be made for example from elemental metal or from alloys such as stainless steel, carbon fibers may be made from elemental carbon and synthetic polymer fibers may be made from e.g. aramides.
  • Fibrous material suitable for the disclosure may contain non fibrous fillers to adjust the mechanical, physical and chemical properties of the material, for example the porosity.
  • a fibrous catalyst particles support is positioned between a structural support or a screen and the catalyst particles.
  • all the inert particles may be replaced by the fibrous catalyst particles support, which is in contact on the one side with the structural support / screen, and on the other side with the catalyst particles.
  • only part (for example 1 layer out of 2 or 3 or more layers of inert particles) of the inert particles are eliminated and replaced by the fibrous catalyst particles support.
  • the fibrous catalyst particles support is in contact with inert particles on one of the two sides or on both sides.
  • Fig. 1 shows an example of a loading diagram in a multi-layer three-bed reactor for hydroprocessing in the current art.
  • Fig. 2 shows an example of a loading diagram in a multi-layer three-bed reactor for hydroprocessing according to an embodiment of the invention.
  • a catalytic bed reactor may comprise one or more catalytic beds.
  • Figure 1 shows an example of a catalytic bed from the art.
  • the reactor of this example (01 ) receives a flow of feed (13) and treat gas (14), as well as two quench (16) streams for cooling and providing extra hydrogen.
  • Effluent (17) is withdrawn at the reactor outlet (22).
  • the reactor is a hydroprocessing reactor with 3 beds: a top (10,1 1 ), a middle (08,09) and a lower bed (05,06,07), all the three beds comprising multiple layers of catalyst particles (05-1 1 ).
  • Above the beds are a distribution tray (23) and a void (15), allowing for mixing.
  • the catalyst particles in the layers are not necessarily all different and do not necessarily all have catalytic properties - some of the catalyst particles may be selected because of physical properties and functionalities.
  • the reactor furthermore comprises an outlet collector (21 ), at the exit of a reactor, typically at the bottom, as in Figure 1 .
  • An outlet collector has the function to prevent catalyst particles from leaving the reactor and being transported to the downstream equipment through the outlet pipe (22).
  • the outlet collector comprises a metallic screen (not shown).
  • the outlet collector and the screen are subject to strength and durability requirements.
  • the screen mesh is required to hold small catalyst particles and avoid unnecessary pressure differential across the outlet collector.
  • a catalyst loading comprises inert particles to separate the outlet collector from the catalyst particles bed (02-04).
  • Each bed of the reactor further comprises a catalyst particles support (20).
  • a catalyst particles support comprises a structural support with screens (not shown), designed with similar consideration as an outlet collector screen.
  • a bed loading of a small-sized catalyst particles above a catalyst particles support as known from the art comprises at least one layer of inert particles between the catalyst particles and the screen of the catalyst particles support.
  • inert particles there are two layers of inert particles, of type 34 and 44 (small and in contact with the catalyst particles), and of type 33 and 43, of intermediate size, in contact with the catalyst particles support screen
  • Figure 2 shows an embodiment of the reactor according to the disclosure.
  • Nomenclature is the same as in Fig. 1 .
  • the reactor (01 ) receives a flow of feed (13) and treat gas (14), as well as two quench (16) streams for cooling and providing extra hydrogen.
  • Effluent (17) is withdrawn at the reactor outlet pipe (22).
  • this reactor has distribution trays (23) and a voids (15), allowing for mixing.
  • Fibrous catalyst particles support (24, 25, and 26) positioned on the catalyst support grid (20) replaces almost all of the inert particles (indicated with 03, 04, 33, 34, 43, 44 in Fig.1 ) at the bottom of the three catalyst particles beds, leaving only a single layer (02).
  • the fibrous catalyst particles support (24) may be laid on the screen of the outlet collector (21 ) replacing also the layer of inert particles (02).
  • a fibrous catalyst particles support (25, 26) is placed on top of the catalyst particles support holding the top bed (10,1 1 ) and the middle bed (08,09) and the catalyst particles bed is loaded directly on the fibrous catalyst particles support.
  • an additional volume of the same type of catalyst particles (10) may fill the space filled by the inert particles in Fig.1 and not occupied by the catalyst particles screen for the top bed.
  • a new catalyst type (12) fills the space left free by the inert particles and not occupied by the catalyst particles screen.
  • the fibrous catalyst particles support (24) is placed above inert particles of the largest type (02) and allows to increase the height of catalyst particle layer (05).
  • the catalyst loading volume provided by replacing inert particles by fibrous catalyst particles support allows flexibility to the selection and design of the catalyst loading. This may result in a flexibility for increasing or decreasing the height of the layer of catalyst particle type 4 (08) in the middle bed of Fig. 2, relative to the same layer in Fig. 1 , as appropriate for the optimization of the operations.
  • the fibrous catalyst particles supports (24, 25, 25) may be of the same type, but they may also be of different types depending upon the material that they have to retain and other characteristics required by the process.
  • each layer for a hydroprocessing reactor as from the art is given in Table 1 (second column). If part of the inert particles is replaced by the fibrous catalyst particles support, as shown in the embodiment of Figure 2 with respect to the current art loading of Figure 1 , the height available for the catalyst changes as in Table 1 , third column.
  • the disclosure allows an increase of catalyst volume type 6 (layer 10) by 5.8%.
  • the disclosure allows introducing a layer of 75+75-6 mm of catalyst particle type 8 (layer 12) below catalyst particle type 4 (08), being this layer 6.1 % of the original layer of catalyst particle type 4 (08); and a further increase of catalyst volume of catalyst particle type 1 (05) by 18.7% at the bottom bed.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

La présente invention concerne un réacteur contenant des particules de catalyseur, une couche de support de particules de catalyseur fibreux au-dessous desdites particules de catalyseur et un dispositif inférieur de support structurel sous ladite couche de particules de catalyseur, l'avantage associé a un tel réacteur étant un espace accru pour des particules de catalyseur comparativement à un réacteur avec des particules inertes supportant les particules de catalyseur.
PCT/EP2018/070207 2017-07-27 2018-07-25 Réacteur catalytique comprenant un support de particules de catalyseur fibreux Ceased WO2019020705A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP18746175.1A EP3658268A1 (fr) 2017-07-27 2018-07-25 Réacteur catalytique comprenant un support de particules de catalyseur fibreux
CN201880049598.XA CN110944740A (zh) 2017-07-27 2018-07-25 包含纤维状催化剂颗粒载体的催化反应器
RU2020108186A RU2020108186A (ru) 2017-07-27 2018-07-25 Каталитический реактор, содержащий волокнистую подложку частиц катализатора
JP2020503976A JP2020528345A (ja) 2017-07-27 2018-07-25 繊維状触媒粒子支持体を含む触媒反応器
US16/632,957 US20200156033A1 (en) 2017-07-27 2018-07-25 Catalytic reactor comprising fibrous catalyst particles support

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201762537742P 2017-07-27 2017-07-27
US62/537,742 2017-07-27
DKPA201700436 2017-08-07
DKPA201700436 2017-08-07

Publications (1)

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WO2019020705A1 true WO2019020705A1 (fr) 2019-01-31

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Cited By (5)

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US10500581B1 (en) 2003-03-25 2019-12-10 Crystaphase International, Inc. Separation method and assembly for process streams in component separation units
US10557486B2 (en) 2016-02-12 2020-02-11 Crystaphase Products, Inc. Use of treating elements to facilitate flow in vessels
US10744426B2 (en) 2015-12-31 2020-08-18 Crystaphase Products, Inc. Structured elements and methods of use
US11052363B1 (en) 2019-12-20 2021-07-06 Crystaphase Products, Inc. Resaturation of gas into a liquid feedstream
US11752477B2 (en) 2020-09-09 2023-09-12 Crystaphase Products, Inc. Process vessel entry zones

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US3865555A (en) * 1972-06-28 1975-02-11 Rheinstahl Ag Reactor for catalytic gas phase oxidation
US4348362A (en) * 1980-09-24 1982-09-07 Minnesota Mining And Manufacturing Company Air pollution control apparatus and process
WO1991010496A1 (fr) * 1990-01-18 1991-07-25 International Fuel Cells Corporation Reacteur catalytique pour reactions en phase gazeuse
US5202097A (en) * 1990-06-15 1993-04-13 Institut Francais Du Petrole Reactor with a lower wall and/or an upper wall having a layer of a flexible refractory material
EP0993335A1 (fr) * 1997-07-03 2000-04-19 E.I. Dupont De Nemours And Company Reacteur catalytique a chauffage par induction
WO2000061706A1 (fr) * 1999-04-13 2000-10-19 Chevron U.S.A. Inc. Systeme de reaction a circulation ascendante comportant un lit catalytique en couches pour l'hydrogenation de charges d'alimentation lourdes
US20070104621A1 (en) * 2005-11-07 2007-05-10 Bilal Zuberi Catalytic Exhaust Device for Simplified Installation or Replacement
US20070259779A1 (en) * 2004-09-13 2007-11-08 Collier Paul J Catalyst Carrier Substrate Coated with Washcoat Comprising Fibrous Material
WO2009137110A1 (fr) * 2008-05-09 2009-11-12 Gary Lee Carson Traitement de l'échappement d'un moteur à combustion interne en utilisant des matériaux en fibres de céramique immobilisées
US20110171101A1 (en) * 2007-07-23 2011-07-14 Evonik Roehm Gmbh Reactor for preparing hydrogen cyanide by the andrussow process

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3865555A (en) * 1972-06-28 1975-02-11 Rheinstahl Ag Reactor for catalytic gas phase oxidation
US4348362A (en) * 1980-09-24 1982-09-07 Minnesota Mining And Manufacturing Company Air pollution control apparatus and process
WO1991010496A1 (fr) * 1990-01-18 1991-07-25 International Fuel Cells Corporation Reacteur catalytique pour reactions en phase gazeuse
US5202097A (en) * 1990-06-15 1993-04-13 Institut Francais Du Petrole Reactor with a lower wall and/or an upper wall having a layer of a flexible refractory material
EP0993335A1 (fr) * 1997-07-03 2000-04-19 E.I. Dupont De Nemours And Company Reacteur catalytique a chauffage par induction
WO2000061706A1 (fr) * 1999-04-13 2000-10-19 Chevron U.S.A. Inc. Systeme de reaction a circulation ascendante comportant un lit catalytique en couches pour l'hydrogenation de charges d'alimentation lourdes
US20070259779A1 (en) * 2004-09-13 2007-11-08 Collier Paul J Catalyst Carrier Substrate Coated with Washcoat Comprising Fibrous Material
US20070104621A1 (en) * 2005-11-07 2007-05-10 Bilal Zuberi Catalytic Exhaust Device for Simplified Installation or Replacement
US20110171101A1 (en) * 2007-07-23 2011-07-14 Evonik Roehm Gmbh Reactor for preparing hydrogen cyanide by the andrussow process
WO2009137110A1 (fr) * 2008-05-09 2009-11-12 Gary Lee Carson Traitement de l'échappement d'un moteur à combustion interne en utilisant des matériaux en fibres de céramique immobilisées

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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