GB2314853A - Reformer comprising finned reactant tubes - Google Patents

Reformer comprising finned reactant tubes Download PDF

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Publication number
GB2314853A
GB2314853A GB9614202A GB9614202A GB2314853A GB 2314853 A GB2314853 A GB 2314853A GB 9614202 A GB9614202 A GB 9614202A GB 9614202 A GB9614202 A GB 9614202A GB 2314853 A GB2314853 A GB 2314853A
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Prior art keywords
tubes
fins
radiant section
reactor according
steam reforming
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GB9614202A
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GB9614202D0 (en
Inventor
Peter William Farnell
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Imperial Chemical Industries Ltd
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Imperial Chemical Industries Ltd
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Priority to GB9614202A priority Critical patent/GB2314853A/en
Publication of GB9614202D0 publication Critical patent/GB9614202D0/en
Publication of GB2314853A publication Critical patent/GB2314853A/en
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • 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
    • B01J2208/00088—Flow rate 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
    • B01J2208/00433—Controlling the temperature using electromagnetic heating
    • B01J2208/0046—Infrared radiation
    • 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
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • 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
    • B01J2208/00504—Controlling the temperature by means of a burner
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
    • C01B2203/0216—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0816—Heating by flames
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • C01B2203/1017—Packed bed of catalytic structures, e.g. particles, packing elements characterised by the form of the structure
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1064—Platinum group metal catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1064—Platinum group metal catalysts
    • C01B2203/107—Platinum catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1082—Composition of support materials
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons

Abstract

An endothermic reactor, especially for the catalytic steam reforming of hydrocarbons, comprising a fired furnace having at least a radiant section 3 in which a plurality of reactant tubes 2 are disposed, said tubes having fins 11 on their external surface in at least part of the radiant section of the furnace.

Description

Reactor This invention relates to a reactor, especially a reactor for effecting an endothermic reaction, and to endothermic reactions using the reactor.
Strongly endothermic reactions, such as steam reforming of hydrocarbons either catalytic for the production of synthesis gas where steam is a reactant, or non-catalytic, i.e. steam cracking to produce olefins from a paraffin feedstock where the steam acts essentially as a diluent, are normally effected by passing the feedstock to be reacted through tubes heated in a fumace.
Heat is supplied by combusting a fuel in the furnace, and passing the combustion products past the tubes. The fumace generally has a radiant section, where the heat is supplied largely through radiant heating and may also have a convective section, for example in the flue gas ducting, where the heat transfer to the tubes is largely through convection. Typically the radiant heat transfer coefficient in the radiant section is of the order of at least 50 W/m2 "C, and usually is in the range 80 to 300 W/m2 "C. In contrast, the convective heat transfer coefficient in the radiant section is much lower, usually below 10 W/m2 "C and typically in the range 1 to 5 Wlm2 "C.
In order to improve the heat transfer in the convective section, the cross section of the flow path of the heating medium, e.g. the combustion products from the fumace, is reduced so that the velocity of the heating medium is increased. It has also been proposed, for example in EP 0 314 408, to provide the tubes with an extended surface, e.g. fins, in the convective section in order to increase the heat transfer area of the tubes in this section and so enhance the rate at which heat is transferred to the tubes.
We have now realised that significant benefits can be achieved if the tubes in the radiant section are provided with fins. Heretofore it was thought that there would be no benefit in increasing the heat transfer area in the radiant section as reactants passing through the tubes would not be able to absorb the heat fast enough and so the tube temperature would increase to such an extent that metallurgical problems would result. However calculations have shown that especially with catalytic steam reforming using catalysts with good heat transfer characteristics, significant improvements can result from the use of fins on the tubes in the radiant section.
Accordingly the present invention provides an endothermic reactor comprising a fired furnace having at least a radiant section in which a plurality of reactant tubes are disposed, said tubes having an extended, e.g. finned, external surface in at least part of the radiant section of the fumace.
The radiant section is that section of the fumace wherein the amount of heating by radiation exceeds the amount of heating by convection. The tubes may also extend into the convective section of the fumace (where the amount of heating by convection exceeds the amount, if any, heating by radiation) and may also have fins in this convective section. Preferably the tubes have fins for the whole length of the tubes disposed in the radiant section.
As mentioned above the invention is of particular utility for catalytic steam reforming of hydrocarbons such as natural gas or naphtha. Catalysts for such steam reforming reactions include shaped units of a support of a suitable refractory material, for example alumina, zirconia, or calcium aluminate cement, bearing or impregnated with a catalyst composition including one or more metals selected from nickel, ruthenium, palladium, or a platinum. Such catalysts are normally randomly packed into the reforming tubes. Catalysts having good heat transfer characteristics are those in which the shaped units have a plurality of through passages, for example as described in US Reissue patent 32044.
The fins preferably extend essentially parallel to the length of the tubes and should relatively widely spaced and of low height so that they do not cast an undue shadow to radiation on the tube surface. For example the height of the fins is preferably 5 to 20% of the tube radius and the fin spacing is preferably 1 to 5 times the fin height. As an example, with a reformer tube of 100 mm diameter, there may be 8 to 30 fins evenly spaced around the circumference of the tube with each fin having a height of 4 to 15 mm. The number and height of the fins is preferably such as to increase the heat transfer surface area by 40 to 120%. Thus 12 fins of 10 mm height and 1 mm thickness on a tube of 100 mm extemal diameter gives an increase in surface area of about 76% with a fin spacinglheight ratio of about 2.5.
The increase in surface area resulting from the use of the fins enables the amount of heat to be transferred into the tubes to be increased, thus enabling the reactants throughput to be increased. Thus the provision of fins on the tubes of an existing reformer enables the reforming capacity to be increased without increasing the number of tubes. As a corollary, the same amount of reforming could be achieved but using fewer tubes. If fins were not employed, an increase in the throughput could be achieved by increasing the amount of firing in the fumace so as to increase the tube wall temperature. However this has the disadvantage of not only possibly presenting metallurgical problems resulting from the increased tube temperature, but also means that the flue gas temperature is increased, thus necessitating more heat recovery from the fumace flue gas to obtain an energy efficient process.
While it is preferred that the extended surface of the tube is provided by means of fins, other means of extending the surface may be employed, for example, serrations, or studs. The extended surface may be provided by attachments to the tubes, or may be integrally cast thereon.
The invention is illustrated by reference to the accompanying drawings wherein Figure 1 is a diagrammatic section of a fired reformer, and Figure 2 is a cross section of a tube having fins in accordance with the invention.
In Figure 1 there is shown a top fired reformer 1 having a plurality of catalyst filled reformer tubes 2 disposed vertically in the radiant section 3 of the reformer furnace. The reformer tubes are connected to a header 4 and a footer 5 by means of pigtails 6. The fumace is fired by fuel and air fed to burners 7 at the top of the radiant section 3. The combustion products pass down the radiant section 3 heating the tubes 2 mainly by radiant heating and leave the radiant section 3 at the bottom of the furnace and pass through a convection section 8 in which are disposed heat exchange coils 9 to recover heat from the combustion products. The combustion products are then discharged to the atmosphere via a flue stack 10.
Referring to Figure 2, each reformer tube, having an extemal diameter of 100 mm, an internal diameter of 80 mm, and a total length of 10 m, has 12 longitudinally extending fins 11 of height 10 mm and thickness 1 mm welded along its length. The tubes are made from HP Mod Nb high temperature alloy and the fins from alloy 800. The resulting finned tube has a heat exchange surface area about 76% greater than that of the unfinned tube.
In a calculated example, the above reformer tubes are random packed with a steam reforming catalyst of 16% by weight of nickel on a calcium aluminate support in the form of cylinders diameter 14.0 mm and length 17.6 mm, and having 4 cylindrical passages of internal diameter 4.0 mm extending axially therethrough. If used to reform desulphurised natural gas mixed with steam (3 moles of steam per gram atom of hydrocarbon carbon) preheated to 550"C, at a dry gas flow rate of 5.72 kmol/h per tube, and reacted to an exit temperature of 800"C and exit pressure of 35 bar abs., the exit gas composition and tube wall temperatures at various locations down the length of the tube were as shown in the following table. By way of comparison, with no fins on the tubes, a similar outlet gas composition could be achieved at a dry gas flow rate of 4.85 kmol/h per tube with the tube wall temperatures shown.
distance down tube (m) fins no fins 0 671 663 2 767 751 Tube wall temperature eC) 4 812 797 6 824 815 8 831 825 10 828 825 methane 7.42 7.39 hydrogen 40.37 40.44 Exit gas composition carbon monoxide 5.92 5.94 (volume monoxide 5.92 (volume %) carbon dioxide 6.10 6.10 steam 40.19 40.14 Flue gas temperature at exit of radiant section (oC) 1025 1023

Claims (5)

Claims
1 An endothermic reactor comprising a fired furnace having at least a radiant section in which a plurality of reactant tubes are disposed, said tubes having fins on their external surface in at least part of the radiant section of the fumace.
2 A reactor according to claim 1 wherein the fins extend longitudinally along the extemal surface of the tubes and the fins have a height in the range 5 to 20% of the tube radius and the fin spacing is 1 to 5 times the fin height.
3 An endothermic reactor according to claim 1 or claim 2 wherein the reactant tubes are filled with a steam reforming catalyst.
4 An endothermic reactor according to claim 3 wherein the steam reforming catalyst comprises shaped units of a support of a suitable refractory material bearing or impregnated with a catalyst composition including one or more metals selected from nickel, ruthenium, palladium, or a platinum, said shaped units being in the form of cylindrical pieces with a plurality of axially extending through passages.
5 A process for the catalytic steam reforming of hydrocarbons comprising passing a mixture of a hydrocarbon feedstock and steam through the tubes of a reactor according to claim 3 or claim 4.
GB9614202A 1996-07-05 1996-07-05 Reformer comprising finned reactant tubes Withdrawn GB2314853A (en)

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GB9614202A GB2314853A (en) 1996-07-05 1996-07-05 Reformer comprising finned reactant tubes

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GB2314853A true GB2314853A (en) 1998-01-14

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012129643A1 (en) * 2011-03-31 2012-10-04 Nova Chemicals (International) S.A. Furnace coil fins
WO2012145820A1 (en) * 2011-04-28 2012-11-01 Nova Chemicals (International) S.A. Furnace coil with protuberances on the external surface
FR3027381A1 (en) * 2014-10-21 2016-04-22 Air Liquide REFORMING OVEN COMPRISING FINNED REFORMING TUBES
FR3047423A1 (en) * 2016-02-09 2017-08-11 Air Liquide DISMANTLING FINAL DEVICE FOR REFORMING TUBE
WO2022106058A1 (en) * 2020-11-19 2022-05-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Reforming reactor comprising reformer tubes with enlarged outer surface area and structured catalyst

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4371452A (en) * 1979-05-18 1983-02-01 Toyo Engineering Corporation Process for hydrocarbon reforming and apparatus therefor
JPS62138307A (en) * 1985-12-10 1987-06-22 Yamaha Motor Co Ltd Device for reforming fuel for fuel cell
EP0305799A1 (en) * 1987-09-01 1989-03-08 Abb Lummus Crest Inc. Pyrolysis heater
US4847051A (en) * 1988-03-21 1989-07-11 International Fuel Cells Corporation Reformer tube heat transfer device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4371452A (en) * 1979-05-18 1983-02-01 Toyo Engineering Corporation Process for hydrocarbon reforming and apparatus therefor
JPS62138307A (en) * 1985-12-10 1987-06-22 Yamaha Motor Co Ltd Device for reforming fuel for fuel cell
EP0305799A1 (en) * 1987-09-01 1989-03-08 Abb Lummus Crest Inc. Pyrolysis heater
US4847051A (en) * 1988-03-21 1989-07-11 International Fuel Cells Corporation Reformer tube heat transfer device

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
WPI Abstract Acc. No. 87-210660/198730 & JP620138307 A (YMHA) See abstract *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012129643A1 (en) * 2011-03-31 2012-10-04 Nova Chemicals (International) S.A. Furnace coil fins
WO2012145820A1 (en) * 2011-04-28 2012-11-01 Nova Chemicals (International) S.A. Furnace coil with protuberances on the external surface
EP2702120A1 (en) * 2011-04-28 2014-03-05 Nova Chemicals (International) S.A. Furnace coil with protuberances on the external surface
JP2014520241A (en) * 2011-04-28 2014-08-21 ノヴァ ケミカルズ（アンテルナショナル）ソシエテ アノニム Furnace coil with protrusions on the outer surface
EP2702120A4 (en) * 2011-04-28 2014-09-24 Nova Chem Int Sa Furnace coil with protuberances on the external surface
FR3027381A1 (en) * 2014-10-21 2016-04-22 Air Liquide REFORMING OVEN COMPRISING FINNED REFORMING TUBES
WO2016062932A1 (en) * 2014-10-21 2016-04-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Reforming furnace comprising reforming tubes with fins
CN107073426A (en) * 2014-10-21 2017-08-18 乔治洛德方法研究和开发液化空气有限公司 Include the reformer of the reformer tubes with fin
US20170312721A1 (en) * 2014-10-21 2017-11-02 L'Air Liquide, Société Anonyme pour I'Etude et I'Exploitation des Procédés Georges Claude Reforming furnace comprising reforming tubes with fins
FR3047423A1 (en) * 2016-02-09 2017-08-11 Air Liquide DISMANTLING FINAL DEVICE FOR REFORMING TUBE
WO2022106058A1 (en) * 2020-11-19 2022-05-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Reforming reactor comprising reformer tubes with enlarged outer surface area and structured catalyst

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Publication number Publication date
GB9614202D0 (en) 1996-09-04

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