• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A gas mixer and distributor fof a reactor has first and second inlet chambers with the second inlet chamber being interposed between the first inlet chamber and an entrance to a reaction chamber. Walls form tubular or slit-like passageways extending from the first chamber to the entrance of the reaction chamber through the second chamber. Upper portions of the passageways have uniform cross-sections selected to produce gas velocities above the flashback velocity, as well as producing turbulence to completely mix gas passing from the second chamber through orifices in the walls of the passageways. Lower sections of the passageways gradually increase in cross-section to reduce velocity and minimize vortexing and recirculation at the entrance to the reactor chamber.
    公开号:SU1711659A3
    申请号:SU4356534
    申请日:1988-08-12
    公开日:1992-02-07
    发明作者:Данстер Майкл；Д.Корчнак Джозеф；Х.Мартен Джером
    申请人:Дейви Макки Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    h17
    dimensions; figure 6 is a view In figure 5, illustrating a modified design of the distributor; in FIG. 7 an enlarged vertical cross section, identical to FIG. 2, but illustrating the modified mixer and distributor unit; Fig. 8 is a modification of a removable mixer unit with a gas distributor; figure 9 is a view of G on Fig; in fig. 10 is a node II on Fig; figure 11 is a modified tubular element shown in figure 10, a cross-section.
    The reaction apparatus for the partial oxidation of the gaseous feedstock (FIG. 1) contains a mixer unit 1 with a feedstock dispenser. The mixer unit 1 with the distributor mixes the feedstock with the oxidant and supplies the formed mixture to the entrance to the reaction chamber of the catalytic apparatus 2, in which the partial oxidation of the feedstock occurs with the final formation of the product, which then passes through the outlet section 3. The feedstock can be represented by hydrocarbon gas or a vaporizable hydrocarbon liquid that is subject to conversion or conversion. The oxidant is represented by an oxygen-rich gas stream, which can be pure oxygen, air, or oxygen-rich air. Steam can be introduced into the hydrocarbon feedstock and / or into the gaseous oxidant stream.
    Mixer unit 1 with a distributor can be used in many types of reaction apparatus, in addition to the catalytic reaction apparatus described in the example for the partial oxidation of the original hydrocarbon stream. In the latter case, two or more gaseous reactants introduced into the reaction chamber must be necessarily and uniformly mixed beforehand. Block 1 is particularly suitable for exothermic reactions when it is necessary to carry out the reaction in some controlled manner inside the catalyst. The most common other types of reaction apparatus are those used in the autothermal reforming or secondary reforming process in order to obtain





    products such as ammonia, methanol, synthesis gas, etc. The reaction apparatus includes an outer shell of a structural metal, for example carbon steel, together with the upper part 5 attached to the shell with bolts (not shown) or otherwise. An insulation layer 6, for example, of a temperature resistant 12b) C (2300 ° F) insulation material based on ceramic HRSG fiber, is attached to the inner side of the upper part of the shell kt
    5, including the upper part 5. In the lower part of the unit 1, in the section of the reaction apparatus 2 and in section 3 of the outlet, layers 7-9 are fixed on the inner side of the shell.
    0 is represented by a molded or equivalent insulating material, for example, withstanding a temperature in 10 ° C (2000 ° F) ceramic insulating material with a low content
    5 iron and high purity. Layer 8 is also represented by a molded f or equivalent layer of insulating material, but containing 60%. alumina, which allows it to withstand temperatures of 1–50 ° C (3,000 ° F). The inner layer 9 is represented by a refractory or equivalent layer, for example, an insulating material layer consisting of at least 97% alumina with ceramic anchors, or an insulating brick consisting of at least 97% alumina and capable of withstanding internal reaction temperatures. - .0 onnogo apparatus.
    In addition, in order to prevent diffusion of the reactants, and therefore combustion inside the refractory layer, a shell made of a non-porous metal alloy (not shown) can be placed between the inner side of the refractory layer and the catalyst layer.
    In the section of the reaction apparatus 2 a stack of monolithic Kata® of the lytic discs 10 of an industrial design is installed, with rings 11 made of a material with a high content of aluminum oxide laid between each adjacent pair of discs.
    5 rests on a lattice represented by rods 12 made from mother-ala high-alumina content. Starting material for catalo0
    five
    ten
    15
    20
    25
    517P659
    the mash is selected based on the reaction taking place. For carrying out partial oxidation reactions, platinum-palladium catalytic materials, rhodium catalytic materials and other catalytic materials with a strongly developed surface area, such as alumina or catalytic materials, which are used in catalytic converters of automobile exhaust systems, are quite acceptable.
    In the lower part of the apparatus 2 there is a hole 1 3 in which a tube 14 is installed, extending below the lower catalytic disk 10 and intended for measuring temperature or for withdrawing samples of the product.
    The outlet section 3 is designed in such a way that it can be reliably and simply connected to a waste heat boiler located below (not shown) and / or other process equipment.
    In the mixer unit 1 with the distributor, the first inlet 15, located in the center of the upper part 5, communicates with the first chamber 16 in the form of a supply funnel. The funnel is securely fixed to the upper part 5 by means of the support members 17. The second inlet holes 18 pass through the side openings of the shell 4 and communicate with the second chamber 19, which is installed between the upper chamber 16 and the inlet section of the catalytic apparatus 2. Installed in the central parts of the upper wall 20 of the chamber 19 ring 21 provides. . hermetic engagement with the lower edge of the funnel so that the wall 20 will form a common wall between the first chamber 16 and the second chamber 19. The chamber 19 is provided with an upper outer ring, a different part 22, which rests on the upper surface of the refractory slab 9 or is attached to the shell A. B. Chamber 19 is provided with a bundle of pipes .23 that extends down into the refractory layer 9.
    The plurality of elongated tubes 2k have upper ends which are located in the upper wall 20 of chamber 19, the tubes form channels communicating with the first chamber 16. The lower ends of tubes 2k are attached to ELR55 b
    thirty
    35
    40
    45
    50
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    ment 25. Channels are made in two sections. The first section 26 has a constant flow area, and the second section 27 has a continuous flow section along the gas flow. Element 25 forms the bottom wall of the second chamber 19, separating it from the reaction chamber. Holes 28 are formed in the walls of the tubes 24, and rye direct the flows from the chamber 19 to the channels of the tubes 24.
    The inlets 15 and 18, the funnel and the supporting elements 17 are made from a conventional corrosion resistant and high temperature material, such as stainless steel or high temperature resistant alloy, while chamber 19, tubes 2k and element 25 are made from a standard high temperature resistant alloy, for example, from a firm Hastella X alloy or from a refractory type material.
    The number of tubes 24, the inner diameter D (Fig. 5) of the tubes 24, as well as the size d and the number of holes 28 in each tube are selected depending on the pressures and rates of gas injection through the inlet holes 15 and 8 and so that inside the tubes 24 a turbulent flow was formed at a rate that would exceed the rate of flashback (flame breakthrough) of the mixture. The minimum distance h of the holes 28 from the bottom of the section 26 of the tube 24 is chosen so that it is equal to or greater than the distance necessary to guarantee essentially complete mixing of the gas streams from the chambers t6 and 19 under the conditions of turbulence in the channels. The size of the inner diameter D of the tubes 24 as well as the length of the same tubes are chosen so as to form. The pressure difference in the gas passing from chamber 16 into the reaction chamber is sufficient to form essentially uniform gas flows through the tubes. 24 of the curves 16. Similarly, the size of the holes 28 is chosen so as to create a pressure differential between the chamber 19 and the interior of the pipe-5-side 24 sufficient to form (mostly uniform volumes of gas streams that pass through holes 28 and fall into mp killers 24,
    0
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    The minimum gas flow rate inside the 2k tubes is selected depending on the type, temperature and density of the reacting gas. For a mixture of natural gas and air, in which there is almost no hydrogen at ambient temperature and pressure, a speed of I m / s (3 ft / s) is chosen (minimum), but for higher temperatures and pressures at the inlet or if the mixture contains a relatively high percentage of hydrogen, the minimum temperature may be higher. Typical minimum rates for mixtures of hydrocarbon gas and air at an inlet port of 2750 kPa (OD psi) and at temperatures in the inlet 59O C (these parameters are typical for partial oxidation reactions) are from 6 to 55 m / s (or 20 to 180 pounds per second) or higher.
    The expanding channels in the element 25 are designed in such a way that they provide a reduction in the gas flow rate with the final formation of a uniform distribution of the gas flow over the entire catalyst section. The side walls of the channels in the element
    25 MAY BE EXECUTED DIRECTLY OR FROM 1
    chunks in a vertical section of the plane. The degree of increase in the cross-sectional area of the channel in section 27 downwards, i.e. The gullet that forms between the channel wall and the straight wall of 2k tubes must be equal to or less than 15 °, and optimally equal to or less than 7 ° to be able to minimize or even eliminate altogether the possibility of vortexing inside the expanding channels to stimulate the formation of fee money in the channel. The configuration of the bottom of the channel of section 27 (Fig. 0 is round. To avoid the formation of sections 29 that contribute to a vortex in the outlet of the element 25, the channels of section 27 can be lengthened, which will necessarily reduce the area of section 29 to a simple point. In FIG. 6 shows a modified embodiment of the invention in which the channels of section 27 are made with six
    five
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    by the angular section. In this case, other sections of the bottom openings can be used, for example, they can have rectangular, triangular and other sections; it is important that these holes provide a substantially uniform distribution of the gas mixture flow over the catalyst bed.
    Ignition can occur in the channel of section 27, especially near the catalyst bed, however, the oxidation reaction occurs mainly within the catalyst bed. It is also possible to raise the temperature of the feed gas above the ignition temperature of the gas mixture. In this latter case, the gas flow rates in the 2k tubes are chosen so as to shorten the residence time of the gas in the channels of the 2k tubes to a duration that is not enough to guarantee the complete reaction of the gas mixture. It was found that if, prior to the moment the gases were introduced into the expanding sections 27, they were not fully mixed, then these gases tend to remain in this state, i.e. incompletely mixed, causing discrepancies and a decrease in gas flow rates. Nevertheless, it was found that within sections 26 in tubes 2k there is complete mixing of gases in a section of minimum distance h, which in this case is due to the high-speed turbulent flow. In addition, the introduction of flows through the openings 28 across the flow in the tubes 2 forms additional turbulence in the flows that descend down the tubes, which actually further enhances the mixing.
    In the embodiment of the invention shown in Fig. 7, the bottom or bottom part of the chamber 19 is closed by the wall 30. The tubes 2k pass through the bottom wall 30, in which they are fixed, for example, by welding. The lower ends of the tubes 2k protrude downward. In addition, element 25 will be open, which reduces the weight and the amount of starting material needed to obtain element 25.
    Figures 8-10 show another variant of the invention, in accordance with which an elongated uniform cross-section of the upper sections 26 of the channel, which are connected to the chamber 16, is formed by slit-shaped channels 31 between horizontal pipes 32 having an elongated cross-section and across the second chamber 19. Thus, the channels 30 with a constant cross-sectional area are slit-like. The pipes 32 are connected at opposite ends with an annular chamber 33, which receives a flow of gas through the inlets 18. The holes 3, arranged in horizontal rows, provide communication between the internal camera 35 of the pipes 32 with the channels 31. The vertical length of section 26, as well as the horizontal width of the chambers 35 in the pipes 32 are chosen so as to maintain a uniform pressure along the entire horizontal length of the pipes 32, and the number and diameter of the holes 3 are chosen so as to provide a significant first a pressure pad on. holes 3 and ensure a uniform flow of gas from the holes 3 into the slit-shaped channels 31. The width of channels-i 31, as well as their vertical size, are chosen so as to form a pressure drop from the upper chamber 16 with the final maintenance of uniform distribution through the inlets channels 31 and thereby ensure the formation of a uniform gas flow through the channels 31, which will ultimately allow the use of a flow rate that is higher than the rate of the gas mixture re-ignition, and the formation of turbulent th stream. The minimum distance at which the holes 3 are located above the bottom. The end of section 26 with a uniform cross section of the channels will be equal to or slightly larger than the minimum distance, which guarantees essentially complete mixing of the gas flows. The pipes 32 in the lower part are provided with wedge-shaped elements 36, which are mounted on or are integrally formed with the lower edges of the pipes 32 to form diverging lower sections 27 of the channels in order to reduce the flow rate and minimize or eliminate the formation of gas turbulence, or spiral flow at the entrance to the catalyst bed. Educated in
    elements 36 channels 37 can transmit coolant, for example water.
    Figure 11 shows a modified tube 3B, which can replace a tube or tubes 32. 8 of its lower part, the modified tube 38 may have the shape of the wedge-shaped elements of the Zb shown in figure 10
    The mixer works as follows. at once.
    In the construction 5 of the reaction apparatus shown in Fig. 1, the catalytic partial oxidation of, for example, natural gas containing 95 OBD of methane proceeds, the remainder is supplied to ethane, propane, nitrogen and -0.0-carbon oxide. The gas is mixed with
    steam and air with the final formation of a mixture containing about 20 vol.% natural gas, about 60 obD air and about 20 o6.% 5 steam. The steam is subdivided and introduced both into the natural gas stream and into the air stream before the inlet ports 15 and 18. A gaseous hydrocarbon with a temperature in the PFD C ndr-0 is given through the inlet 15 with a diameter of 0.25 m under a pressure of 2760 kPa An air flow with a temperature of 550 ° C is supplied through two inlet openings 18 with a diameter of 0.152 m under a pressure of 2 96 U k Pa and with a speed
    about 3 m / s; The diameter of the lower part of the chamber 19 is equal to 0.68 m, and the diameter of the upper part 22 is equal to 0.91 m. In this design, 261 tubes of L with an inner diameter of 12.7 mm and length of 0.51 are used. m each. In each tube, six holes 28 are formed with a diameter of 3.2 mm each, with four holes with 5 regular intervals around each tube at a distance of 0.102 m above it with the end of section 26, and the other two holes are opposite each other at a distance of 0.152 mm above the lower end of the tube. The bottom element 25 has a thickness of 0.127 m, and the channel sections 27 are tapered with a diameter in the upper part of 12.7 mm and with a diameter in the lower part of 4.5 mm. The pressures inside chambers 16 and 19 are maintained primarily at the pressure level at the inlet port. The flow rate of gas in tubes 2A above the top holes is equal to
    0
    approximately 52 m / s, and between the lower apertures and the lower end of the tubes it is approximately 107 m / s. At flow rates, from the channels, the gas flow rate decreases from 107 m / s at the upper end to 9 m / s at the lower end or at the entrance to the catalyst.
    The various sizes given above are intended for the reaction of some specific gaseous hydrocarbon and air supplied at some specific speeds. It should be borne in mind that these dimensions and speeds will be different for other gaseous hydrocarbons, oxygen or enriched air, for other catalysts and other feed rates.
    权利要求:
    Claims (7)
    [1]
    1. A gas blender with a distributor for supplying a gas reagent mixture to the reactor, containing successively placed a first chamber with an inlet for one gaseous agent, a second chamber with an inlet for the second gaseous agent, and a reaction chamber placed in the second chamber; forming a number of channels that communicate the first chamber with the reaction chamber and having a series of holes in the side walls that connect the channels with the cavity of the second chamber, characterized in that, in order to increase the productivity the mixer, the channels are made in two sections, with the first section, on the side of the first chamber, made with a straight through section, and the second, from the side of the reaction chamber, with a constantly increasing section through the gas.
    [2]
    2. Mixer pop. 1, the difference is Q Q y and with the fact that the upper part
    The pipes are fixed in the wall separating the first chamber from the second one.
    [3]
    3. A mixer according to claim 2, wherein the channels and tubes with a continuously increasing flow area are made in the bottom wall of the second chamber separating it from the reaction chamber
    [4]
    k. The mixer according to claim 2, jl and h aq and y, so that the pipe sections forming channels with an increasing flow area are placed under the bottom wall of the second chamber.
    [5]
    5. A mixer according to claim 1, about aphids h5 and 5 with the fact that the pipes in the second chamber have an oblong cross-section and are placed across the second chamber with the formation of channels in the form of slits.
    [6]
    o 6. The mixer according to claim 5, o. It means that the pipes are provided with wedge-shaped in cross section elements mounted on the lower edges of the pipes with an elongated cross section or made integral with them.
    [7]
    7. The mixer according to claim 6, of which is made with the fact that channels for coolant supply are made in the elements with wedge-shaped section.
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    同族专利:
    公开号 | 公开日
    DK453288A|1989-02-15|
    NO883606L|1989-02-15|
    CA1314129C|1993-03-09|
    EP0303439A2|1989-02-15|
    CN1014494B|1991-10-30|
    NZ225814A|1990-03-27|
    NO173127C|1993-11-03|
    NO883606D0|1988-08-12|
    MX165662B|1992-11-27|
    AT81490T|1992-10-15|
    DK453288D0|1988-08-12|
    ES2035301T3|1993-04-16|
    AU2098888A|1989-02-16|
    KR960009153B1|1996-07-16|
    AU604956B2|1991-01-03|
    DE3875305T2|1993-02-25|
    KR890003440A|1989-04-14|
    EP0303439B1|1992-10-14|
    CN1033753A|1989-07-12|
    UA5587A1|1994-12-28|
    GR3006155T3|1993-06-21|
    NO173127B|1993-07-26|
    ZA885993B|1990-04-25|
    DK174008B1|2002-04-08|
    JP2752383B2|1998-05-18|
    AR243404A1|1993-08-31|
    US4865820A|1989-09-12|
    JPH01159037A|1989-06-22|
    IN171676B|1992-12-05|
    DE3875305D1|1992-11-19|
    BR8804104A|1989-05-02|
    EP0303439A3|1990-07-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2446865C2|2007-03-29|2012-04-10|Полимери Эуропа С.П.А.|Mixer with low pressure differential and its application for mixing two gases/vapors|
    RU2465193C2|2007-11-23|2012-10-27|Эни С.П.А.|Method of producing synthesis gas from liquid and gaseous hydrocarbons|
    RU2474469C2|2007-06-06|2013-02-10|Уде Гмбх|Device and method for catalytic gas phase reactions and their application|
    US9592481B2|2007-07-30|2017-03-14|Jgc Corporation|Method of producing a gas mixing device|US2630461A|1953-03-03|Production of acetylene by incom |
    US433871A|1890-08-05|Hydrocarbon-burner |
    GB367747A|
    US2102152A|1933-01-25|1937-12-14|Joseph W Hays|Premixing device for fluid fuel burners|
    US2195227A|1936-03-06|1940-03-26|Ig Farbenindustrie Ag|Production of acetylene|
    US2701011A|1944-08-26|1955-02-01|Bonvillian Claude Albert|Apparatus for the combustion of fuel|
    US2559979A|1945-02-23|1951-07-10|Arthur E Martois|Multiple gas burner|
    US2493017A|1946-08-05|1950-01-03|Ervin J Nutter|Grid spray nozzle|
    US2700598A|1946-10-31|1955-01-25|Standard Oil Dev Co|Process for reforming hydrocarbons|
    US2656254A|1948-12-11|1953-10-20|Columbian Carbon|Carbon black|
    US2790838A|1952-01-16|1957-04-30|Eastman Kodak Co|Process for pyrolysis of hydrocarbons|
    US2827112A|1953-08-28|1958-03-18|Union Carbide Corp|Flame blasting and apparatus therefor|
    US2843592A|1954-09-01|1958-07-15|California Research Corp|Catalyst unit and gas distributor|
    US3473323A|1968-07-11|1969-10-21|Southwick W Briggs|Oxidation apparatus|
    FR2145089A5|1971-07-08|1973-02-16|Wendel Sidelor|
    GB1368352A|1972-01-26|1974-09-25|British Petroleum Co|Fluidised bed distributor plate|
    DE2232656B2|1972-07-03|1978-02-02|Siemens AG, 1000 Berlin und 8000 München|CLEARING GAS GENERATOR FOR GENERATING A COMBUSTION GAS|
    DE2301644C2|1973-01-13|1974-07-18|Friedrich Uhde Gmbh, 4600 Dortmund|Device for producing a homogeneous gas mixture|
    GB1459766A|1973-03-20|1976-12-31|British Petroleum Co|Combustor|
    US3927998A|1973-12-28|1975-12-23|Texaco Inc|Production of methane-rich gas stream|
    NL187622C|1975-04-14|1991-12-02|Stone & Webster Eng Corp|REFORM OVEN WITH CONVECTION HEATING OF PROCESS TUBES.|
    US4136015A|1977-06-07|1979-01-23|Union Carbide Corporation|Process for the thermal cracking of hydrocarbons|
    US4166834A|1977-09-27|1979-09-04|John Zink Company|Air injector nozzle for secondary reformer|
    US4409196A|1979-04-24|1983-10-11|Foster Wheeler Energy Corporation|Synthesis gas for ammonia production|
    US4522894A|1982-09-30|1985-06-11|Engelhard Corporation|Fuel cell electric power production|
    US4477262A|1983-05-16|1984-10-16|Victor Equipment Company|Mixer for cutting torch|
    DE3532413C2|1985-09-11|1990-02-08|Uhde Gmbh, 4600 Dortmund, De|
    FR2608581B1|1986-12-18|1989-04-28|Inst Francais Du Petrole|FLAME-OPERATING METHOD AND DEVICE FOR THE MANUFACTURE OF SYNTHESIS GAS|CA2004219A1|1988-11-30|1990-05-31|Michael Dunster|Production of hydrogen from hydrocarbonaceous feedstock|
    US5106590A|1990-05-11|1992-04-21|Davy MckeeLimited|Gas mixer and distributor with heat exchange between incoming gases|
    US5298226A|1992-10-02|1994-03-29|Praxair Technology, Inc.|Perforated plate fluid distributor and its associated fixed bed vessel|
    US5523063A|1992-12-02|1996-06-04|Applied Materials, Inc.|Apparatus for the turbulent mixing of gases|
    IT1283585B1|1996-04-11|1998-04-22|Snam Progetti|EQUIPMENT TO CARRY OUT PARTIAL OXIDATION REACTIONS|
    US5980596A|1997-04-25|1999-11-09|Exxon Research And Engineering Co.|Multi-injector autothermal reforming process and apparatus for producing synthesis gas .|
    US5883138A|1997-04-25|1999-03-16|Exxon Research And Engineering Company|Rapid injection catalytic partial oxidation process and apparatus for producing synthesis gas |
    US5935489A|1997-04-25|1999-08-10|Exxon Research And Engineering Co.|Distributed injection process and apparatus for producing synthesis gas|
    AU7251498A|1997-04-25|1998-11-24|Exxon Research And Engineering Company|Low temperature process for producing synthesis gas|
    US6267912B1|1997-04-25|2001-07-31|Exxon Research And Engineering Co.|Distributed injection catalytic partial oxidation process and apparatus for producing synthesis gas|
    US5886056A|1997-04-25|1999-03-23|Exxon Research And Engineering Company|Rapid injection process and apparatus for producing synthesis gas |
    US5980782A|1997-04-25|1999-11-09|Exxon Research And Engineering Co.|Face-mixing fluid bed process and apparatus for producing synthesis gas|
    DE19806427A1|1998-02-17|1999-08-19|Fleissner Maschf Gmbh Co|Air mixer for static mixing of two air flows|
    US6471937B1|1998-09-04|2002-10-29|Praxair Technology, Inc.|Hot gas reactor and process for using same|
    WO2000038826A1|1998-12-24|2000-07-06|Ruhrgas Aktiengesellschaft|Device for mixing two fluid components|
    EP1043271A1|1999-03-30|2000-10-11|Shell Internationale Researchmaatschappij B.V.|Apparatus for the catalytic partial oxidation of hydrocarbons|
    US6350427B1|1999-07-27|2002-02-26|Kerr-Mcgee Chemical Llc|Processes for reacting gaseous reactants containing solid particles|
    EP1222144A1|1999-10-05|2002-07-17|Ballard Power Systems Inc.|Autothermal reformer|
    AU3108201A|2000-01-24|2001-07-31|Int Fuel Cells Llc|Autothermal fuel gas reformer assemblage|
    US7018436B2|2000-08-08|2006-03-28|Shell Oil Company|Catalytic reactor with tangential flow distribution|
    DE10219747B4|2002-05-02|2005-06-23|Daimlerchrysler Ag|A method for preventing re-ignition in a mixture flowing to a reaction space and a reactor for carrying out the method|
    DE10262231B4|2002-07-04|2009-04-16|Sgl Carbon Ag|Process for the production of hydrogen|
    US7097787B2|2002-07-19|2006-08-29|Conocophillips Company|Utilization of micro-channel gas distributor to distribute unreacted feed gas into reactors|
    US7262334B2|2002-11-13|2007-08-28|Regents Of The University Of Minnesota|Catalytic partial oxidation of hydrocarbons|
    EP1419812B1|2002-11-15|2015-09-16|Haldor Topsoe A/S|High temperature fixed bed reactor and its use|
    DE10304155A1|2003-02-03|2004-08-05|Basf Ag|Process for the oxidative purification of an exhaust gas containing an combustible component|
    TW200422289A|2003-02-18|2004-11-01|Bp Chem Int Ltd|Auto thermal cracking reactor|
    GB2421246A|2003-08-21|2006-06-21|Syntroleum Corp|Two-stage auto thermal reforming process system|
    US7399329B2|2003-08-22|2008-07-15|Syntroleum Corporation|Process for production of synthesis gas using an oxygen-containing gas|
    US7108838B2|2003-10-30|2006-09-19|Conocophillips Company|Feed mixer for a partial oxidation reactor|
    DE10359744A1|2003-12-19|2005-07-14|Uhde Gmbh|Method and device for injecting oxygen into a synthesis reactor|
    AU2005206487A1|2004-01-08|2005-08-04|Syntroleum Corporation|Processes for starting up an autothermal reformer|
    DE102004024957A1|2004-05-22|2005-12-22|Uhde Gmbh|Device, useful for passing oxygen that is added in pure form into a reaction gas, comprises an oxygen distribution element from two tubes and a multitude of flow pipes before the arrangement for receiving catalyst filling|
    US7683232B2|2004-05-25|2010-03-23|Regents Of The University Of Minnesota|Production of olefins having a functional group|
    US7156193B2|2004-06-04|2007-01-02|Matt Swartout|Continuous positive flow backflash prevention system|
    US8517717B2|2004-08-13|2013-08-27|Velocys, Inc.|Detonation safety in microchannels|
    CN100349647C|2004-10-29|2007-11-21|中国石油化工股份有限公司|Multi-segment insulation fix bed reactor|
    AU2005316638A1|2004-12-14|2006-06-22|Syntroleum Corporation|Burnerless autothermal reformer mixer|
    US7416571B2|2005-03-09|2008-08-26|Conocophillips Company|Compact mixer for the mixing of gaseous hydrocarbon and gaseous oxidants|
    DE102005034941B4|2005-07-22|2008-12-18|J. Eberspächer GmbH & Co. KG|Reformer for the production of synthesis gas|
    US20080257147A1|2005-12-06|2008-10-23|Johnson Matthey Plc|Gas Distributor|
    US7547422B2|2006-03-13|2009-06-16|Praxair Technology, Inc.|Catalytic reactor|
    US7842846B2|2006-03-30|2010-11-30|Basf Aktiengesellschaft|Process for heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated|
    DE102006024038A1|2006-05-23|2007-11-29|Forschungszentrum Jülich GmbH|Apparatus for producing a fuel-oxidizer mixture|
    DE102006054415A1|2006-11-16|2008-05-21|Uhde Gmbh|Method and device for injecting oxygen into a reaction gas flowing through a synthesis reactor|
    FR2948296A1|2009-07-21|2011-01-28|Inst Francais Du Petrole|DEVICE FOR MIXING GAS AND DISPENSING THE MIXTURE RESULTING AT THE ENTRY OF A CATALYTIC REACTOR|
    US8808654B2|2009-09-29|2014-08-19|Praxair Technology, Inc.|Process for sulfur removal from refinery off gas|
    FR2960449B1|2010-05-25|2012-08-03|Inst Francais Du Petrole|REACTOR FOR AUTOTHERMAL REFORMING OF GASOIL|
    DE102011086321B4|2011-11-14|2013-07-25|Mtu Friedrichshafen Gmbh|Gas mixer and gas mixing system|
    CA2860773C|2012-01-13|2020-11-03|Siluria Technologies, Inc.|Process for separating hydrocarbon compounds|
    US9670113B2|2012-07-09|2017-06-06|Siluria Technologies, Inc.|Natural gas processing and systems|
    US9598328B2|2012-12-07|2017-03-21|Siluria Technologies, Inc.|Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products|
    WO2015081122A2|2013-11-27|2015-06-04|Siluria Technologies, Inc.|Reactors and systems for oxidative coupling of methane|
    CN106068323B|2014-01-08|2019-09-06|希路瑞亚技术公司|Ethylene at liquid system and method|
    US10377682B2|2014-01-09|2019-08-13|Siluria Technologies, Inc.|Reactors and systems for oxidative coupling of methane|
    US9701597B2|2014-01-09|2017-07-11|Siluria Technologies, Inc.|Oxidative coupling of methane implementations for olefin production|
    US20160289143A1|2015-04-01|2016-10-06|Siluria Technologies, Inc.|Advanced oxidative coupling of methane|
    WO2016181344A1|2015-05-14|2016-11-17|Sabic Global Technologies B.V.|Reactors and reactor-internal devices for dehydrogenation of hydrocarbons|
    RU2643967C2|2015-06-11|2018-02-06|Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Ухтинский государственный технический университет"|Method of fluid jet mixing and device for its implementation|
    EP3786138A1|2015-10-16|2021-03-03|Lummus Technology LLC|Oxidative coupling of methane|
    DE102015121037A1|2015-12-03|2017-06-08|Thyssenkrupp Ag|Device for the distribution of oxygen in an oxidation reactor, oxidation reactor and installation with such a device and method of operation|
    EP3554672A4|2016-12-19|2020-08-12|Siluria Technologies, Inc.|Methods and systems for performing chemical separations|
    AU2018273238B2|2017-05-23|2022-02-10|Lummus Technology Llc|Integration of oxidative coupling of methane processes|
    EP3441360B1|2017-08-10|2020-07-29|Sener Ingenieria Y Sistemas, S.A.|System for alcohol reforming and hydrogen production, units of the system and method thereof|
    RU187844U1|2018-11-29|2019-03-19|Федеральное государственное бюджетное образовательное учреждение высшего образования "Ярославский государственный технический университет" |The device for contacting gas with liquid|
    RU187523U1|2018-11-29|2019-03-11|Федеральное государственное бюджетное образовательное учреждение высшего образования "Ярославский государственный технический университет" ФГБОУВО "ЯГТУ"|Device for contacting gas with liquid|
    EP3693338B1|2019-02-07|2021-09-01|Sener Ingenieria Y Sistemas, S.A.|High-pressure auto-thermal system for reforming alcohol and producing hydrogen, and method therefor|
    CN111905645A|2020-07-29|2020-11-10|青海三四一九干燥设备有限公司|Hot air distributor for pressure spray drying equipment|
    法律状态:
    2005-05-10| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: MM4A Effective date: 20030813 |
    优先权:
    申请号 | 申请日 | 专利标题
    US07/085,159|US4865820A|1987-08-14|1987-08-14|Gas mixer and distributor for reactor|
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