+

US20090056696A1 - Flameless combustion heater - Google Patents

Flameless combustion heater Download PDF

Info

Publication number
US20090056696A1
US20090056696A1 US12/176,220 US17622008A US2009056696A1 US 20090056696 A1 US20090056696 A1 US 20090056696A1 US 17622008 A US17622008 A US 17622008A US 2009056696 A1 US2009056696 A1 US 2009056696A1
Authority
US
United States
Prior art keywords
conduit
fuel
oxidation
centralizer
heater
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
US12/176,220
Other languages
English (en)
Inventor
Abdul Wahid Munshi
Peter Veenstra
Rachel Anna Worthen
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.)
Shell USA Inc
Original Assignee
Individual
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 Individual filed Critical Individual
Priority to US12/176,220 priority Critical patent/US20090056696A1/en
Assigned to SHELL OIL COMPANY reassignment SHELL OIL COMPANY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MUNSHI, ABDUL WAHID, VEENSTRA, PETER, WORTHEN, RACHEL ANNA
Publication of US20090056696A1 publication Critical patent/US20090056696A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C3/00—Combustion apparatus characterised by the shape of the combustion chamber
    • F23C3/002—Combustion apparatus characterised by the shape of the combustion chamber the chamber having an elongated tubular form, e.g. for a radiant tube
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/03009—Elongated tube-shaped combustion chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/99001—Cold flame combustion or flameless oxidation processes
    • Y—GENERAL 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • This invention relates to a flameless combustion heater and a method for providing heat to a process.
  • Flameless combustion heaters are described in U.S. Pat. No. 7,025,940.
  • the patent describes a process heater utilizing flameless combustion, which is accomplished by preheating a fuel and combustion air to a temperature above the auto-ignition temperature of the mixture.
  • the fuel is introduced in relatively small increments over time through a plurality of orifices in a fuel gas conduit, which provide communication between the fuel gas conduit and an oxidation reaction chamber.
  • a process chamber is in heat exchange relationship with the oxidation reaction chamber.
  • Flameless combustion heaters provide several benefits over conventional fired heaters as described in the aforementioned patent. Flameless combustion heaters can, however, encounter problems related to the mixing of the fuel and oxidant in the oxidation reaction chamber.
  • Peak temperatures can occur near each opening in the fuel conduit, and this non-uniform heating causes non-uniform thermal expansion of the fuel conduit. Therefore, the fuel conduit has a tendency to bend, which bending positions the fuel conduit openings close to the wall of the oxidation reaction chamber and can result in hot spots that may lead to failure of the oxidation reaction chamber wall.
  • the fuel passing through the openings may exhibit a jet effect as it enters the oxidation reaction chamber. If the wall of the oxidation reaction chamber is too close to the opening then the fuel will impinge directly on the wall. This requires that a minimum distance be maintained between the outside of the fuel conduit and the inside of the oxidation reaction chamber.
  • the invention provides a flameless combustion heater comprising: an oxidation conduit and a fuel conduit having a plurality of centralizers attached to the external wall of the fuel conduit wherein at least one centralizer or portion of a centralizer is angled with respect to the longitudinal axis of the fuel conduit.
  • the invention also provides a method for providing heat to a process conduit comprising providing an oxidation conduit; providing a fuel conduit having a plurality of openings that provide fluid communication from within the fuel conduit to the oxidation conduit, and a plurality of centralizers attached to the fuel conduit wherein at least one centralizer or portion of a centralizer is angled with respect to the longitudinal axis of the fuel conduit; providing a process conduit in a heat exchange relationship with the oxidation conduit; introducing fuel into the fuel conduit; introducing an oxidant into the oxidation conduit; and introducing the fuel into the oxidation conduit through the plurality of openings such that flameless combustion occurs in the oxidation conduit.
  • FIG. 1 a depicts a two-tube flameless combustion heater with angled centralizers.
  • FIG. 1 b depicts an external view of a fuel conduit with angled centralizers.
  • the invention provides a flameless combustion heater that is used in the direct transfer of heat energy released by the flameless combustion of fuel.
  • the heater has many possible uses and applications including heating underground formations and heating process streams.
  • the flameless combustion heater is especially useful in conjunction with processes that carry out endothermic reactions, for example, dehydrogenation of alkylaromatic compounds and steam methane reforming.
  • the invention provides a flameless combustion heater with an improved design of the centralizers attached to the external wall of the fuel conduit.
  • the centralizers are protrusions attached to the external wall of the fuel conduit to prevent contact between the fuel conduit and the oxidation conduit.
  • the present invention addresses the aforementioned problems.
  • the use of angled centralizers results in improved mixing of the fuel and air within the heater, reduces or eliminates peak temperatures and helps prevent fuel impingement on the inside of the oxidation conduit.
  • Flameless combustion in a heater can be accomplished by preheating an oxidant stream and a fuel stream sufficiently that when the two streams are combined the temperature of the mixture exceeds the auto-ignition temperature of the mixture, but the temperature of the mixture is less than a temperature that would result in the oxidation upon mixing being limited by the rate of mixing as described in U.S. Pat. No. 7,025,940 which is herein incorporated by reference.
  • the auto ignition temperature of the mixture depends on the types of fuel and oxidant and the fuel/oxidant ratio.
  • the auto ignition temperature of mixtures used in a flameless combustion heater may be in a range of from 850° C. to 1400° C.
  • the auto ignition temperature may be reduced if an oxidation catalyst is employed in the heater because this type of catalyst effectively lowers the auto-ignition temperature of the mixture.
  • the fuel conduit provides for the controlled rate of fuel introduction into an oxidation conduit in a manner so as to provide for a desired heat release.
  • the heat release is determined in part by the location and number of openings, which can be tailored to each heater application.
  • the heat release may be constant over the length of the heater, or it may be decreasing or increasing over the length of the heater.
  • the flameless combustion reaction occurs at a lower temperature than that observed in conventional fired heaters. Due to the lower temperatures observed, and the efficiency of direct heating, the heater may be designed using lower cost materials resulting in reduced capital expenditure.
  • the flameless combustion heater has two main elements: an oxidation conduit and a fuel conduit.
  • the oxidation conduit may be a tube or pipe that has an inlet for oxidant, an outlet for oxidation products and a flow path between the inlet and outlet. Suitable oxidants include air, oxygen, and nitrous oxide.
  • the oxidant that is introduced into the oxidation conduit may be preheated such that when mixed with fuel, the mixture is at a temperature above the auto-ignition temperature of the mixture.
  • the oxidant may be heated externally to the flameless combustion heater.
  • the oxidant may be heated inside the heater by heat exchange with any of the streams inside the heater.
  • the oxidation conduit may have an internal diameter of from about 2 cm to about 20 cm.
  • the oxidant conduit may however be larger or smaller than this range depending on the heater requirements.
  • the fuel conduit transports fuel into the heater and introduces it into the oxidation conduit.
  • the fuel conduit may be a tube or pipe that has an inlet for fuel and a plurality of openings that provide fluid communication from within the fuel conduit to the oxidation conduit.
  • the fuel conduit may be located within and surrounded by the oxidation conduit. The fuel passes through the openings and into the oxidation conduit where it mixes with the oxidant and results in flameless combustion.
  • the fuel conduit may have an internal diameter of from about 1 cm to about 10 cm, preferably from about 1.5 cm to 5 cm. Depending on the design, however, the fuel conduit may have a diameter greater than 10 cm or less than 1 cm.
  • the openings can be drilled or cut into the wall of the fuel conduit.
  • the wall of the fuel conduit typically has a thickness of from about 0.25 cm to about 2.5 cm.
  • the openings may have cross sections that are circular, elliptical, rectangular, of another shape, or even irregularly shaped.
  • the openings preferably have a circular cross-section.
  • the openings may have a cross-sectional area of from about 0.001 cm 2 to about 2 cm 2 , preferably from about 0.03 cm 2 to about 0.2 cm 2 .
  • the size of the openings is determined by the desired rate of fuel introduction into the oxidation conduit, but openings that are too small may result in plugging.
  • the openings may be located along the fuel conduit at a distance of from 1 cm to 100 cm in the axial direction from any other opening.
  • the openings are preferably spaced from 15 cm to 50 cm apart in the axial direction.
  • the openings may be positioned in their respective radial planes at different orientations along the length of the fuel conduit.
  • the position of the openings may alternate 180 degrees in the radial plane along the length of the fuel conduit, or they may alternate 120 degrees or 90 degrees. Therefore the position of the openings in the fuel conduit may be such that their orientation in the radial plane alternates along the length of the fuel conduit with their orientations separated by 30 degrees to 180 degrees. It is preferred for the radial orientation of the openings to alternate at from 60 degrees to 120 degrees along the length of the fuel conduit.
  • a sintered plate may be used in addition to openings to provide fluid communication from the fuel conduit to the oxidation zone, and the openings in a sintered plate may have a diameter on the order of 10-100 microns.
  • Different openings along the length of the heater typically have the same cross-sectional area.
  • the cross-sectional area of the openings may be different to provide a desired heat release.
  • the spacing between openings along the fuel conduit may be different to provide a desired heat release.
  • the openings are typically the same shape. In the alternative, the openings may be different shapes.
  • Each centralizer has a proximal end, the end closest to the fuel inlet, and a distal end, the end farthest from the fuel inlet.
  • the centralizers may be triangular, rectangular, semicircular or any other shape.
  • the centralizers may be made of or coated with a material that is softer than the material used for the oxidation conduit so the centralizers do not damage the oxidation conduit when the fuel conduit is installed or removed.
  • the centralizers may be made of a softer metal or a ceramic.
  • the fuel conduit has a longitudinal axis defined by the line connecting the centers of the cross-sections of the conduit. At least one of the centralizers is angled with respect to the longitudinal axis of the fuel conduit.
  • the centralizer may be at any angle that is not parallel and not perpendicular to the longitudinal axis of the fuel conduit.
  • a centralizer that is neither parallel nor perpendicular to the longitudinal axis of the fuel conduit is hereinafter referred to as an angled centralizer.
  • An angled centralizer may be angled such that the angle formed between the centralizer and the longitudinal axis of the fuel conduit is less than ninety degrees.
  • An angled centralizer may be angled such that the angle formed between the centralizer and the longitudinal axis of the fuel conduit is less than sixty degrees or preferably less than forty-five degrees.
  • Positioning angled centralizers upstream (closer to the oxidant inlet) of a fuel conduit opening causes the oxidant to flow in a partially tangential direction as it passes the fuel conduit opening.
  • This tangential flow component reduces the jet effect and minimizes the minimum distance required between the conduits.
  • the partially tangential flow also contributes to improved mixing and a more even radial temperature profile. The heat is distributed more evenly around the circumference of the fuel conduit.
  • the angled centralizers may be straight or curved to provide desired flow characteristics of the oxidant in the oxidant conduit.
  • a straight centralizer is one in which the centralizer is located in one geometric plane.
  • a curved centralizer has portions that are in at least two non-parallel geometric planes. If the centralizer is curved, a portion of the centralizer may be parallel to the longitudinal axis of the fuel conduit.
  • FIGS. 1 a and 1 b depict a flameless combustion heater ( 10 ) with angled centralizers ( 16 ) as described above.
  • the heater ( 10 ) has a fuel conduit ( 12 ) and an oxidation conduit ( 14 ).
  • This type of heater is referred to as a two-tube heater.
  • Fuel conduit ( 12 ) is a cylindrical pipe that has an inlet ( 24 ) for fuel and a plurality of openings ( 20 ).
  • the oxidation conduit ( 14 ) is a cylindrical pipe that has an inlet ( 26 ) for preheated oxidant and an outlet ( 30 ) for combustion products. In the alternative, the oxidant may enter at ( 30 ) and the combustion products may exit at ( 26 ).
  • the fuel enters fuel conduit ( 12 ) via inlet ( 24 ) and then is mixed with oxidant in oxidation conduit ( 14 ) after it passes through the openings ( 20 ).
  • an angled centralizer ( 16 ) is positioned upstream (closer to the oxidant inlet) of each opening ( 20 ).
  • the flameless combustion heater may be operated at a variety of conditions depending on the particular configuration of heater and the heater application. Various examples and conditions are described in U.S. Pat. No. 5,255,742 and U.S. Pat. No. 7,025,940, which are herein incorporated by reference.
  • the flameless combustion heater may be used in an ethylbenzene dehydrogenation unit.
  • a process feedstock containing steam and ethylbenzene is fed to the dehydrogenation reactor.
  • the dehydrogenation reactor contains a suitable dehydrogenation catalyst, which may be an iron oxide based catalyst, and provides means for contacting the process feedstock with the dehydrogenation catalyst.
  • a dehydrogenation reactor effluent is discharged from the dehydrogenation reactor and introduced into the flameless combustion heater. Because the dehydrogenation reaction is an endothermic reaction, the dehydrogenation reactor effluent will have a lower temperature than that of the process feedstock to the dehydrogenation reactor.
  • the flameless combustion heater is used to heat the dehydrogenation reactor effluent before it is introduced into the second stage dehydrogenation reactor.
  • a dehydrogenation reactor effluent is discharged from the second stage reactor.
  • the dehydrogenation process may be carried out with more than two reactors in which case a flameless combustion heater may be placed in front of each additional reactor.
  • the flameless combustion heater described herein can be used in any application with any variation of the described details of centralizer orientation.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Pre-Mixing And Non-Premixing Gas Burner (AREA)
  • Combustion Of Fluid Fuel (AREA)
  • Fuel Cell (AREA)
US12/176,220 2007-07-20 2008-07-18 Flameless combustion heater Abandoned US20090056696A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US12/176,220 US20090056696A1 (en) 2007-07-20 2008-07-18 Flameless combustion heater

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US95094307P 2007-07-20 2007-07-20
US12/176,220 US20090056696A1 (en) 2007-07-20 2008-07-18 Flameless combustion heater

Publications (1)

Publication Number Publication Date
US20090056696A1 true US20090056696A1 (en) 2009-03-05

Family

ID=39869934

Family Applications (1)

Application Number Title Priority Date Filing Date
US12/176,220 Abandoned US20090056696A1 (en) 2007-07-20 2008-07-18 Flameless combustion heater

Country Status (11)

Country Link
US (1) US20090056696A1 (fr)
EP (1) EP2176587B1 (fr)
JP (1) JP2010534312A (fr)
KR (1) KR101495377B1 (fr)
CN (1) CN101918761B (fr)
AR (1) AR067577A1 (fr)
AT (1) ATE511062T1 (fr)
BR (1) BRPI0814093A2 (fr)
RU (1) RU2461775C2 (fr)
TW (1) TW200925520A (fr)
WO (1) WO2009014979A2 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070154855A1 (en) * 2006-01-05 2007-07-05 Great Southern Flameless, Llc System, apparatus and method for flameless combustion absent catalyst or high temperature oxidants
US20190168156A1 (en) * 2016-05-17 2019-06-06 Shailendra Inamdar Flameless thermal oxidizer for oxidizing gaseous effluent streams containing hydrogen gas

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014206898A1 (fr) 2013-06-24 2014-12-31 Chiesi Farmaceutici S.P.A. Procédé amélioré pour la préparation de dérivés d'acide 1-(2-fluoro[1,1'-biphényl]-4-yl)-cyclopropanecarboxylique
KR101876890B1 (ko) * 2016-07-27 2018-07-10 이명재 수산소 혼합가스를 이용한 히터
CN106402861B (zh) * 2016-11-11 2018-03-06 江苏弗雷姆环境科技有限公司 工业燃气超低氮节能螺旋燃烧头及燃烧器
CN114353085A (zh) * 2020-09-30 2022-04-15 芜湖美的厨卫电器制造有限公司 预混组件、燃烧组件和制热设备

Citations (89)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US26990A (en) * 1860-01-31 Oak-coupling
US1920124A (en) * 1931-12-03 1933-07-25 D H Gunn Burner
US2819761A (en) * 1956-01-19 1958-01-14 Continental Oil Co Process of removing viscous oil from a well bore
US2902270A (en) * 1953-07-17 1959-09-01 Svenska Skifferolje Ab Method of and means in heating of subsurface fuel-containing deposits "in situ"
US3376932A (en) * 1966-03-04 1968-04-09 Pan American Petroleum Corp Catalytic heater
US3519396A (en) * 1968-01-04 1970-07-07 Pullman Inc Means for injecting a gaseous reactant
US3527052A (en) * 1967-08-10 1970-09-08 Technology Uk Combustion system with aerodynamically variable geometry
US3810732A (en) * 1971-07-01 1974-05-14 Siemens Ag Method and apparatus for flameless combustion of gaseous or vaporous fuel-air mixtures
US3817332A (en) * 1969-12-30 1974-06-18 Sun Oil Co Method and apparatus for catalytically heating wellbores
US4029146A (en) * 1974-04-01 1977-06-14 John Zink Company Corrugated sheet heat exchanger
US4104018A (en) * 1976-11-26 1978-08-01 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Combuster
US4245701A (en) * 1979-06-12 1981-01-20 Occidental Oil Shale, Inc. Apparatus and method for igniting an in situ oil shale retort
US4273188A (en) * 1980-04-30 1981-06-16 Gulf Research & Development Company In situ combustion process for the recovery of liquid carbonaceous fuels from subterranean formations
US4353712A (en) * 1980-07-14 1982-10-12 Texaco Inc. Start-up method for partial oxidation process
US4377205A (en) * 1981-03-06 1983-03-22 Retallick William B Low pressure combustor for generating steam downhole
US4400179A (en) * 1980-07-14 1983-08-23 Texaco Inc. Partial oxidation high turndown apparatus
US4445570A (en) * 1982-02-25 1984-05-01 Retallick William B High pressure combustor having a catalytic air preheater
US4597734A (en) * 1984-03-05 1986-07-01 Shell Oil Company Surface-combustion radiant burner
US4692306A (en) * 1986-03-24 1987-09-08 Kinetics Technology International Corporation Catalytic reaction apparatus
US4706751A (en) * 1986-01-31 1987-11-17 S-Cal Research Corp. Heavy oil recovery process
US4818371A (en) * 1987-06-05 1989-04-04 Resource Technology Associates Viscosity reduction by direct oxidative heating
US4909808A (en) * 1987-10-14 1990-03-20 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Steam reformer with catalytic combustor
US4928605A (en) * 1985-11-15 1990-05-29 Nippon Sanso Kabushiki Kaisha Oxygen heater, hot oxygen lance having an oxygen heater and pulverized solid fuel burner
US5154599A (en) * 1990-06-29 1992-10-13 Wuenning Joachim Method for apparatus for combusting fuel in a combustion chamber
US5181990A (en) * 1986-01-16 1993-01-26 Babcock-Hitachi Kabushiki Kaisha Pyrolysis furnace for olefin production
US5255742A (en) * 1992-06-12 1993-10-26 Shell Oil Company Heat injection process
US5297626A (en) * 1992-06-12 1994-03-29 Shell Oil Company Oil recovery process
US5306481A (en) * 1989-02-14 1994-04-26 Manufacturing And Technology Conversion International, Inc. Indirectly heated thermochemical reactor apparatus and processes
US5321191A (en) * 1991-11-08 1994-06-14 Institut Francais Du Petrole Process for the thermal pyrolysis of hydrocarbons using an electric furnace
US5330970A (en) * 1991-03-27 1994-07-19 Betz Laboratories, Inc. Composition and method for inhibiting coke formation and deposition during pyrolytic hydrocarbon processing
US5392854A (en) * 1992-06-12 1995-02-28 Shell Oil Company Oil recovery process
US5404952A (en) * 1993-12-20 1995-04-11 Shell Oil Company Heat injection process and apparatus
US5411089A (en) * 1993-12-20 1995-05-02 Shell Oil Company Heat injection process
US5424095A (en) * 1994-03-07 1995-06-13 Eniricerche S.P.A. Ceramic vapor deposited coating using a steam-containing carrier gas and non-alkoxy silane precursors
US5426655A (en) * 1991-07-16 1995-06-20 International Business Machines Corporation Method and apparatus for magnetic recording of data
US5427655A (en) * 1990-11-29 1995-06-27 Stone & Webster Engineering Corp. High capacity rapid quench boiler
US5433271A (en) * 1993-12-20 1995-07-18 Shell Oil Company Heat injection process
US5446229A (en) * 1992-12-18 1995-08-29 Amoco Corporation Thermal cracking process with reduced coking
US5463159A (en) * 1994-03-22 1995-10-31 Phillips Petroleum Company Thermal cracking process
US5513981A (en) * 1991-11-22 1996-05-07 Aichelin Gmbh Burner with variable volume combination chamber
US5523502A (en) * 1993-11-10 1996-06-04 Stone & Webster Engineering Corp. Flexible light olefins production
US5536488A (en) * 1991-07-01 1996-07-16 Manufacturing And Technology Conversion Indirectly heated thermochemical reactor processes
US5554347A (en) * 1994-02-02 1996-09-10 Institut Francais Du Petrole Apparatus for carrying out chemical reactions requiring addition of heat at least during start up
US5559510A (en) * 1995-04-12 1996-09-24 Northrop Grumman Corporation Aircraft landing site indication and light
US5567305A (en) * 1993-08-06 1996-10-22 Jo; Hong K. Method for retarding corrosion and coke formation and deposition during pyrolytic hydrocarbon processing
US5600051A (en) * 1995-05-19 1997-02-04 Corning Incorporated Enhancing olefin yield from cracking
US5665009A (en) * 1996-08-08 1997-09-09 Sherwood; Brad L. Correlated set of golf club irons
US5692562A (en) * 1995-04-13 1997-12-02 Enterra Patco Oilfield Products Limited Well rod, centralizer and centralizer stop interfaces with wear reducing surface
US5743723A (en) * 1995-09-15 1998-04-28 American Air Liquide, Inc. Oxy-fuel burner having coaxial fuel and oxidant outlets
US5862858A (en) * 1996-12-26 1999-01-26 Shell Oil Company Flameless combustor
US5871343A (en) * 1998-05-21 1999-02-16 Air Products And Chemicals, Inc. Method and apparatus for reducing NOx production during air-oxygen-fuel combustion
US5899269A (en) * 1995-12-27 1999-05-04 Shell Oil Company Flameless combustor
US6153152A (en) * 1990-04-03 2000-11-28 The Standard Oil Company Endothermic reaction apparatus and method
US6221117B1 (en) * 1996-10-30 2001-04-24 Idatech, Llc Hydrogen producing fuel processing system
US6296686B1 (en) * 1998-06-03 2001-10-02 Praxair Technology, Inc. Ceramic membrane for endothermic reactions
US20020015670A1 (en) * 1997-10-08 2002-02-07 Rashmi K. Shah Flameless combustor process heater
US20020027001A1 (en) * 2000-04-24 2002-03-07 Wellington Scott L. In situ thermal processing of a coal formation to produce a selected gas mixture
US6402988B1 (en) * 1998-06-03 2002-06-11 Praxair Technology, Inc. Process for producing a syngas
US20030068260A1 (en) * 2001-03-05 2003-04-10 Wellington Scott Lee Integrated flameless distributed combustion/membrane steam reforming reactor and zero emissions hybrid power system
US20030068269A1 (en) * 2001-03-05 2003-04-10 Matzakos Andreas Nikolaos Integrated flameless distributed combustion/steam reforming membrane reactor for hydrogen production and use thereof in zero emissions hybrid power system
US20030101650A1 (en) * 2001-11-22 2003-06-05 Mitsubishi Denki Kabushiki Kaisha Reformer
US20030101651A1 (en) * 2000-03-01 2003-06-05 Weedon Geoffrey G. Endothermic reaction process and an apparatus therefor
US6620386B1 (en) * 1998-07-09 2003-09-16 Stone & Webster, Inc. Radial flow reactor
US20040022724A1 (en) * 2002-08-02 2004-02-05 Robb Gary M. Primary reactor liquid water and air injection for improved management of a fuel processor
US20040033455A1 (en) * 2002-08-15 2004-02-19 Tonkovich Anna Lee Integrated combustion reactors and methods of conducting simultaneous endothermic and exothermic reactions
US20040057898A1 (en) * 2002-09-23 2004-03-25 Kellogg Brown & Root, Inc. Hydrogen enrichment scheme for autothermal reforming
US6783741B2 (en) * 1996-10-30 2004-08-31 Idatech, Llc Fuel processing system
US20040185398A1 (en) * 2002-12-20 2004-09-23 Fina Technology, Inc. Method for reducing the formation of nitrogen oxides in steam generation
US6796789B1 (en) * 2003-01-14 2004-09-28 Petro-Chem Development Co. Inc. Method to facilitate flameless combustion absent catalyst or high temperature oxident
US20050051327A1 (en) * 2003-04-24 2005-03-10 Vinegar Harold J. Thermal processes for subsurface formations
US6889619B2 (en) * 2001-11-16 2005-05-10 Hitachi, Ltd. Solid fuel burner, burning method using the same, combustion apparatus and method of operating the combustion apparatus
US6905328B2 (en) * 2000-03-13 2005-06-14 John Zink Company, Llc Low NOx radiant wall burner
US20050178064A1 (en) * 2000-03-03 2005-08-18 Nippon Chemical Plant Consultant Co., Ltd. Method for internal heating reformation by oxidation
US6951247B2 (en) * 2001-04-24 2005-10-04 Shell Oil Company In situ thermal processing of an oil shale formation using horizontal heat sources
US20060000395A1 (en) * 2004-07-01 2006-01-05 Joshi Mahendra L Staged combustion system with ignition-assisted fuel lances
US20060021280A1 (en) * 2004-07-30 2006-02-02 Hamilton Daniel B Reformer, and methods of making and using the same
US7037472B2 (en) * 2000-10-10 2006-05-02 Tokyo Gas Co., Ltd. Single-pipe cylinder-type reformer
US7063145B2 (en) * 2001-10-24 2006-06-20 Shell Oil Company Methods and systems for heating a hydrocarbon containing formation in situ with an opening contacting the earth's surface at two locations
US20060199127A1 (en) * 2005-03-01 2006-09-07 Fina Technology, Inc. Heating hydrocarbon process flow using flameless oxidation burners
US20060199119A1 (en) * 2005-03-07 2006-09-07 Gas Technology Institute Multi-ported, internally recuperated burners for direct flame impingement heating applications
US20060210468A1 (en) * 2005-03-10 2006-09-21 Peter Veenstra Heat transfer system for the combustion of a fuel and heating of a process fluid and a process that uses same
US20060210936A1 (en) * 2005-03-10 2006-09-21 Peter Veenstra Multi-tube heat transfer system for the combustion of a fuel and heating of a process fluid and the use thereof
US20060222578A1 (en) * 2005-03-10 2006-10-05 Peter Veenstra Method of starting up a direct heating system for the flameless combustion of fuel and direct heating of a process fluid
US20060248800A1 (en) * 2002-09-05 2006-11-09 Miglin Maria T Apparatus and process for production of high purity hydrogen
US7205940B2 (en) * 2002-04-02 2007-04-17 Fuji Xerox Co., Ltd. Antenna and communication device
US20070151152A1 (en) * 2003-12-09 2007-07-05 Matsushita Electric Industrial Co., Ltd. Hydrogen generating apparatus
US20070175094A1 (en) * 2006-01-30 2007-08-02 Reinke Michael J Integrated autothermal reformer recuperator
US20070254251A1 (en) * 2006-04-26 2007-11-01 Jin Cao Ultra-low NOx burner assembly
US20080244973A1 (en) * 2004-01-30 2008-10-09 Idemitsu Kosan Co., Ltd. Reformer

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS597885B2 (ja) * 1978-12-15 1984-02-21 株式会社日立製作所 ガスバ−ナノズル
DE3447603C2 (de) * 1984-12-28 1987-02-05 Aichelin GmbH, 7015 Korntal-Münchingen Keramisches Flammrohr für das Mantelstrahlheizrohr eines Industriebrenners
JPH0596738U (ja) * 1991-01-31 1993-12-27 財団法人工業技術研究院 渦発生器の軸流羽根構造
AU2002212320B2 (en) * 2001-04-24 2006-11-02 Shell Internationale Research Maatschappij B.V. In-situ combustion for oil recovery

Patent Citations (100)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US26990A (en) * 1860-01-31 Oak-coupling
US1920124A (en) * 1931-12-03 1933-07-25 D H Gunn Burner
US2902270A (en) * 1953-07-17 1959-09-01 Svenska Skifferolje Ab Method of and means in heating of subsurface fuel-containing deposits "in situ"
US2819761A (en) * 1956-01-19 1958-01-14 Continental Oil Co Process of removing viscous oil from a well bore
US3376932A (en) * 1966-03-04 1968-04-09 Pan American Petroleum Corp Catalytic heater
US3527052A (en) * 1967-08-10 1970-09-08 Technology Uk Combustion system with aerodynamically variable geometry
US3519396A (en) * 1968-01-04 1970-07-07 Pullman Inc Means for injecting a gaseous reactant
US3817332A (en) * 1969-12-30 1974-06-18 Sun Oil Co Method and apparatus for catalytically heating wellbores
US3810732A (en) * 1971-07-01 1974-05-14 Siemens Ag Method and apparatus for flameless combustion of gaseous or vaporous fuel-air mixtures
US4029146A (en) * 1974-04-01 1977-06-14 John Zink Company Corrugated sheet heat exchanger
US4104018A (en) * 1976-11-26 1978-08-01 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Combuster
US4245701A (en) * 1979-06-12 1981-01-20 Occidental Oil Shale, Inc. Apparatus and method for igniting an in situ oil shale retort
US4273188A (en) * 1980-04-30 1981-06-16 Gulf Research & Development Company In situ combustion process for the recovery of liquid carbonaceous fuels from subterranean formations
US4353712A (en) * 1980-07-14 1982-10-12 Texaco Inc. Start-up method for partial oxidation process
US4400179A (en) * 1980-07-14 1983-08-23 Texaco Inc. Partial oxidation high turndown apparatus
US4377205A (en) * 1981-03-06 1983-03-22 Retallick William B Low pressure combustor for generating steam downhole
US4445570A (en) * 1982-02-25 1984-05-01 Retallick William B High pressure combustor having a catalytic air preheater
US4597734A (en) * 1984-03-05 1986-07-01 Shell Oil Company Surface-combustion radiant burner
US4928605A (en) * 1985-11-15 1990-05-29 Nippon Sanso Kabushiki Kaisha Oxygen heater, hot oxygen lance having an oxygen heater and pulverized solid fuel burner
US5181990A (en) * 1986-01-16 1993-01-26 Babcock-Hitachi Kabushiki Kaisha Pyrolysis furnace for olefin production
US4706751A (en) * 1986-01-31 1987-11-17 S-Cal Research Corp. Heavy oil recovery process
US4692306A (en) * 1986-03-24 1987-09-08 Kinetics Technology International Corporation Catalytic reaction apparatus
US5008085A (en) * 1987-06-05 1991-04-16 Resource Technology Associates Apparatus for thermal treatment of a hydrocarbon stream
US4818371A (en) * 1987-06-05 1989-04-04 Resource Technology Associates Viscosity reduction by direct oxidative heating
US4909808A (en) * 1987-10-14 1990-03-20 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Steam reformer with catalytic combustor
US5306481A (en) * 1989-02-14 1994-04-26 Manufacturing And Technology Conversion International, Inc. Indirectly heated thermochemical reactor apparatus and processes
US6153152A (en) * 1990-04-03 2000-11-28 The Standard Oil Company Endothermic reaction apparatus and method
US5154599A (en) * 1990-06-29 1992-10-13 Wuenning Joachim Method for apparatus for combusting fuel in a combustion chamber
US5427655A (en) * 1990-11-29 1995-06-27 Stone & Webster Engineering Corp. High capacity rapid quench boiler
US5330970A (en) * 1991-03-27 1994-07-19 Betz Laboratories, Inc. Composition and method for inhibiting coke formation and deposition during pyrolytic hydrocarbon processing
US5536488A (en) * 1991-07-01 1996-07-16 Manufacturing And Technology Conversion Indirectly heated thermochemical reactor processes
US5426655A (en) * 1991-07-16 1995-06-20 International Business Machines Corporation Method and apparatus for magnetic recording of data
US5321191A (en) * 1991-11-08 1994-06-14 Institut Francais Du Petrole Process for the thermal pyrolysis of hydrocarbons using an electric furnace
US5513981A (en) * 1991-11-22 1996-05-07 Aichelin Gmbh Burner with variable volume combination chamber
US5255742A (en) * 1992-06-12 1993-10-26 Shell Oil Company Heat injection process
US5392854A (en) * 1992-06-12 1995-02-28 Shell Oil Company Oil recovery process
US5297626A (en) * 1992-06-12 1994-03-29 Shell Oil Company Oil recovery process
US5446229A (en) * 1992-12-18 1995-08-29 Amoco Corporation Thermal cracking process with reduced coking
US5567305A (en) * 1993-08-06 1996-10-22 Jo; Hong K. Method for retarding corrosion and coke formation and deposition during pyrolytic hydrocarbon processing
US5523502A (en) * 1993-11-10 1996-06-04 Stone & Webster Engineering Corp. Flexible light olefins production
US5411089A (en) * 1993-12-20 1995-05-02 Shell Oil Company Heat injection process
US5404952A (en) * 1993-12-20 1995-04-11 Shell Oil Company Heat injection process and apparatus
US5433271A (en) * 1993-12-20 1995-07-18 Shell Oil Company Heat injection process
US5554347A (en) * 1994-02-02 1996-09-10 Institut Francais Du Petrole Apparatus for carrying out chemical reactions requiring addition of heat at least during start up
US5424095A (en) * 1994-03-07 1995-06-13 Eniricerche S.P.A. Ceramic vapor deposited coating using a steam-containing carrier gas and non-alkoxy silane precursors
US5463159A (en) * 1994-03-22 1995-10-31 Phillips Petroleum Company Thermal cracking process
US5559510A (en) * 1995-04-12 1996-09-24 Northrop Grumman Corporation Aircraft landing site indication and light
US5692562A (en) * 1995-04-13 1997-12-02 Enterra Patco Oilfield Products Limited Well rod, centralizer and centralizer stop interfaces with wear reducing surface
US5600051A (en) * 1995-05-19 1997-02-04 Corning Incorporated Enhancing olefin yield from cracking
US5743723A (en) * 1995-09-15 1998-04-28 American Air Liquide, Inc. Oxy-fuel burner having coaxial fuel and oxidant outlets
US6269882B1 (en) * 1995-12-27 2001-08-07 Shell Oil Company Method for ignition of flameless combustor
US5899269A (en) * 1995-12-27 1999-05-04 Shell Oil Company Flameless combustor
US6019172A (en) * 1995-12-27 2000-02-01 Shell Oil Company Flameless combustor
US5665009A (en) * 1996-08-08 1997-09-09 Sherwood; Brad L. Correlated set of golf club irons
US6783741B2 (en) * 1996-10-30 2004-08-31 Idatech, Llc Fuel processing system
US6221117B1 (en) * 1996-10-30 2001-04-24 Idatech, Llc Hydrogen producing fuel processing system
US5862858A (en) * 1996-12-26 1999-01-26 Shell Oil Company Flameless combustor
US20030182858A1 (en) * 1997-10-08 2003-10-02 Shah Rashmi K. Method for providing controlled heat to a process
US20020015670A1 (en) * 1997-10-08 2002-02-07 Rashmi K. Shah Flameless combustor process heater
US7108730B2 (en) * 1997-10-08 2006-09-19 Shell Oil Company Method for providing controlled heat to a process
US5871343A (en) * 1998-05-21 1999-02-16 Air Products And Chemicals, Inc. Method and apparatus for reducing NOx production during air-oxygen-fuel combustion
US6402988B1 (en) * 1998-06-03 2002-06-11 Praxair Technology, Inc. Process for producing a syngas
US6296686B1 (en) * 1998-06-03 2001-10-02 Praxair Technology, Inc. Ceramic membrane for endothermic reactions
US6620386B1 (en) * 1998-07-09 2003-09-16 Stone & Webster, Inc. Radial flow reactor
US20030101651A1 (en) * 2000-03-01 2003-06-05 Weedon Geoffrey G. Endothermic reaction process and an apparatus therefor
US20050178064A1 (en) * 2000-03-03 2005-08-18 Nippon Chemical Plant Consultant Co., Ltd. Method for internal heating reformation by oxidation
US6905328B2 (en) * 2000-03-13 2005-06-14 John Zink Company, Llc Low NOx radiant wall burner
US6877554B2 (en) * 2000-04-24 2005-04-12 Shell Oil Company In situ thermal processing of a hydrocarbon containing formation using pressure and/or temperature control
US6966372B2 (en) * 2000-04-24 2005-11-22 Shell Oil Company In situ thermal processing of a hydrocarbon containing formation to produce oxygen containing formation fluids
US6749021B2 (en) * 2000-04-24 2004-06-15 Shell Oil Company In situ thermal processing of a coal formation using a controlled heating rate
US20020027001A1 (en) * 2000-04-24 2002-03-07 Wellington Scott L. In situ thermal processing of a coal formation to produce a selected gas mixture
US7037472B2 (en) * 2000-10-10 2006-05-02 Tokyo Gas Co., Ltd. Single-pipe cylinder-type reformer
US20030068269A1 (en) * 2001-03-05 2003-04-10 Matzakos Andreas Nikolaos Integrated flameless distributed combustion/steam reforming membrane reactor for hydrogen production and use thereof in zero emissions hybrid power system
US20030068260A1 (en) * 2001-03-05 2003-04-10 Wellington Scott Lee Integrated flameless distributed combustion/membrane steam reforming reactor and zero emissions hybrid power system
US6951247B2 (en) * 2001-04-24 2005-10-04 Shell Oil Company In situ thermal processing of an oil shale formation using horizontal heat sources
US7063145B2 (en) * 2001-10-24 2006-06-20 Shell Oil Company Methods and systems for heating a hydrocarbon containing formation in situ with an opening contacting the earth's surface at two locations
US6889619B2 (en) * 2001-11-16 2005-05-10 Hitachi, Ltd. Solid fuel burner, burning method using the same, combustion apparatus and method of operating the combustion apparatus
US20030101650A1 (en) * 2001-11-22 2003-06-05 Mitsubishi Denki Kabushiki Kaisha Reformer
US7205940B2 (en) * 2002-04-02 2007-04-17 Fuji Xerox Co., Ltd. Antenna and communication device
US20040022724A1 (en) * 2002-08-02 2004-02-05 Robb Gary M. Primary reactor liquid water and air injection for improved management of a fuel processor
US20040033455A1 (en) * 2002-08-15 2004-02-19 Tonkovich Anna Lee Integrated combustion reactors and methods of conducting simultaneous endothermic and exothermic reactions
US20060248800A1 (en) * 2002-09-05 2006-11-09 Miglin Maria T Apparatus and process for production of high purity hydrogen
US20040057898A1 (en) * 2002-09-23 2004-03-25 Kellogg Brown & Root, Inc. Hydrogen enrichment scheme for autothermal reforming
US20050223643A1 (en) * 2002-12-20 2005-10-13 Fina Technology, Inc. Method for reducing the formation of nitrogen oxides in steam generation
US20040185398A1 (en) * 2002-12-20 2004-09-23 Fina Technology, Inc. Method for reducing the formation of nitrogen oxides in steam generation
US6796789B1 (en) * 2003-01-14 2004-09-28 Petro-Chem Development Co. Inc. Method to facilitate flameless combustion absent catalyst or high temperature oxident
US20070131411A1 (en) * 2003-04-24 2007-06-14 Vinegar Harold J Thermal processes for subsurface formations
US7121342B2 (en) * 2003-04-24 2006-10-17 Shell Oil Company Thermal processes for subsurface formations
US20050051327A1 (en) * 2003-04-24 2005-03-10 Vinegar Harold J. Thermal processes for subsurface formations
US20070151152A1 (en) * 2003-12-09 2007-07-05 Matsushita Electric Industrial Co., Ltd. Hydrogen generating apparatus
US20080244973A1 (en) * 2004-01-30 2008-10-09 Idemitsu Kosan Co., Ltd. Reformer
US20060000395A1 (en) * 2004-07-01 2006-01-05 Joshi Mahendra L Staged combustion system with ignition-assisted fuel lances
US20060021280A1 (en) * 2004-07-30 2006-02-02 Hamilton Daniel B Reformer, and methods of making and using the same
US20060199127A1 (en) * 2005-03-01 2006-09-07 Fina Technology, Inc. Heating hydrocarbon process flow using flameless oxidation burners
US20060199119A1 (en) * 2005-03-07 2006-09-07 Gas Technology Institute Multi-ported, internally recuperated burners for direct flame impingement heating applications
US20060222578A1 (en) * 2005-03-10 2006-10-05 Peter Veenstra Method of starting up a direct heating system for the flameless combustion of fuel and direct heating of a process fluid
US20060210936A1 (en) * 2005-03-10 2006-09-21 Peter Veenstra Multi-tube heat transfer system for the combustion of a fuel and heating of a process fluid and the use thereof
US20060210468A1 (en) * 2005-03-10 2006-09-21 Peter Veenstra Heat transfer system for the combustion of a fuel and heating of a process fluid and a process that uses same
US20070175094A1 (en) * 2006-01-30 2007-08-02 Reinke Michael J Integrated autothermal reformer recuperator
US20070254251A1 (en) * 2006-04-26 2007-11-01 Jin Cao Ultra-low NOx burner assembly

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070154855A1 (en) * 2006-01-05 2007-07-05 Great Southern Flameless, Llc System, apparatus and method for flameless combustion absent catalyst or high temperature oxidants
US20070269755A2 (en) * 2006-01-05 2007-11-22 Petro-Chem Development Co., Inc. Systems, apparatus and method for flameless combustion absent catalyst or high temperature oxidants
US20190168156A1 (en) * 2016-05-17 2019-06-06 Shailendra Inamdar Flameless thermal oxidizer for oxidizing gaseous effluent streams containing hydrogen gas
US10895380B2 (en) * 2016-05-17 2021-01-19 Linde Engineering North America Inc. Flameless thermal oxidizer for oxidizing gaseous effluent streams containing hydrogen gas

Also Published As

Publication number Publication date
RU2010106151A (ru) 2011-08-27
EP2176587A2 (fr) 2010-04-21
CN101918761A (zh) 2010-12-15
ATE511062T1 (de) 2011-06-15
CN101918761B (zh) 2012-06-27
KR101495377B1 (ko) 2015-02-24
BRPI0814093A2 (pt) 2015-02-03
JP2010534312A (ja) 2010-11-04
RU2461775C2 (ru) 2012-09-20
KR20100061448A (ko) 2010-06-07
AR067577A1 (es) 2009-10-14
TW200925520A (en) 2009-06-16
EP2176587B1 (fr) 2011-05-25
WO2009014979A3 (fr) 2010-02-18
WO2009014979A2 (fr) 2009-01-29

Similar Documents

Publication Publication Date Title
US20090136879A1 (en) Flameless combustion heater
US7704070B2 (en) Heat transfer system for the combustion of a fuel heating of a process fluid and a process that uses same
US7651331B2 (en) Multi-tube heat transfer system for the combustion of a fuel and heating of a process fluid and the use thereof
EP2176587B1 (fr) Réchauffeur à combustion sans flamme
EP1856444B1 (fr) Procede de demarrage d'un systeme de chauffage direct pour combustion de combustible sans flamme et chauffage direct d'un fluide de processus

Legal Events

Date Code Title Description
AS Assignment

Owner name: SHELL OIL COMPANY, TEXAS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:MUNSHI, ABDUL WAHID;VEENSTRA, PETER;WORTHEN, RACHEL ANNA;REEL/FRAME:021814/0574;SIGNING DATES FROM 20080723 TO 20080730

STCB Information on status: application discontinuation

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

点击 这是indexloc提供的php浏览器服务，不要输入任何密码和下载