EP4321242A1 - Système de mélange de deux fluides - Google Patents

Système de mélange de deux fluides Download PDF

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Publication number
EP4321242A1
EP4321242A1 EP22020382.2A EP22020382A EP4321242A1 EP 4321242 A1 EP4321242 A1 EP 4321242A1 EP 22020382 A EP22020382 A EP 22020382A EP 4321242 A1 EP4321242 A1 EP 4321242A1
Authority
EP
European Patent Office
Prior art keywords
opening diameter
openings
tube
fluid
main pipe
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.)
Pending
Application number
EP22020382.2A
Other languages
German (de)
English (en)
Inventor
Anton Wellenhofer
Desislava TOTA
Florian Habla
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP22020382.2A priority Critical patent/EP4321242A1/fr
Publication of EP4321242A1 publication Critical patent/EP4321242A1/fr
Pending legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3133—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit characterised by the specific design of the injector
    • B01F25/31331—Perforated, multi-opening, with a plurality of holes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/314—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit
    • B01F25/3142—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction
    • B01F25/31425—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction with a plurality of perforations in the axial and circumferential direction covering the whole surface

Definitions

  • the invention relates to a system for mixing two fluids, in particular for mixing two different gases, for example the mixing of oxygen into a hydrocarbon stream, and to a use of this system in particular for oxidative dehydrogenation processes.
  • the mixing of two gases within pipelines is usually achieved using a gas distributor and optionally subsequently using static mixing elements.
  • the gas distributor is typically designed as a T-piece, as an inserted, perforated pipe or as a lance.
  • a high mixing quality is usually only achieved further downstream through the additional use of static mixing elements.
  • the gas injector sold by the applicant as OXYMIX this is introduced into the interior of a main pipe through which a first gas flows and through this a second gas is injected into the interior of the main pipe, the second gas being injected in particular counter to the flow direction of the first gas via an injector head which has circularly arranged openings for the gas to exit.
  • Static mixing elements are, for example, spiral-shaped elements for deflecting a gas flow, whereby the static mixing elements can also include other shapes such as squares, grids, etc.
  • ODH oxidative dehydrogenation
  • paraffins with two to four carbon atoms
  • ODH these paraffins are reacted with oxygen, producing, among other things, the corresponding olefins and water.
  • ODH refers in particular to the oxidative dehydrogenation of ethane to ethylene, hereinafter also referred to as ODHE.
  • ODH may be advantageous over more established processes for producing olefins such as steam cracking or catalytic dehydrogenation.
  • steam cracking or catalytic dehydrogenation there is no thermodynamic equilibrium constraint due to the exothermic nature of the reactions involved and due to the virtually irreversible formation of water.
  • the ODH can be carried out at comparatively low reaction temperatures. In principle, regeneration of the catalysts used is not necessary since the presence of oxygen enables or effects regeneration in situ. Finally, in contrast to steam cracking, smaller amounts of worthless by-products such as coke are produced.
  • Catalysts based on MoVNbOx and MoVNbTeOx can be used in ODH. Under industrially relevant reaction conditions, significant amounts of the respective carboxylic acids of the paraffins used are formed as by-products, especially acetic acid in the case of ODHE. Processes that involve the targeted formation of ethylene and acetic acid are also referred to as “EDHOX”. Such processes are considered a superior option for ethylene producers and an advantageous choice for processes that require both ethylene and acetic acid, such as: B. VAM (vinyl acetate monomer), EVA (ethylene vinyl acetate) copolymer, PVOH (polyvinyl alcohol) products, PET (polyethylene terephthalate), ethyl acetate and similar derivatives.
  • VAM vinyl acetate monomer
  • EVA ethylene vinyl acetate copolymer
  • PVOH polyvinyl alcohol
  • PET polyethylene terephthalate
  • the typical EDHOX system consists of a reaction section, a separation/purification stage and a closed circuit for ethane recycling.
  • EDHOX supplies downstream processes directly with ethylene and acetic acid.
  • the combined ethylene and acetic acid yield is remarkably high, with an overall selectivity of over 93%.
  • This ODH process also recovers a significant portion of the carbon dioxide produced as a pure byproduct (for carbon capture, utilization and storage, CCUS).
  • the reaction in ODH is preferably carried out in fixed bed reactors, in particular in cooled tube bundle reactors, e.g. B. carried out with salt molten cooling.
  • the volume of the mixer or the mixing section (distributor including optional static mixing elements), especially when mixing in oxygen for oxidation processes in refineries or chemical production.
  • Another aim is to keep the pressure loss across the distributor and optional mixing elements as low as possible. Areas with high oxygen concentrations should be avoided as much as possible because of the resulting possible high-temperature spots and the resulting uncontrolled reactions and the risk of explosion. The same applies to mixing oxygen into a hydrocarbon stream.
  • the distributor should not create any recirculation areas or dead zones, which are associated with increased local residence times, which in turn can be questionable from a safety perspective.
  • the distributor should also be suitable for oxidative dehydrogenation (ODH), especially of ethane to ethylene, also called ODHE.
  • ODH oxidative dehydrogenation
  • the present invention proposes a system for mixing two fluids and a use of such a system according to the independent claims.
  • fluid is to be understood as meaning a liquid or a gas, but also a liquid-gas mixture.
  • Each of the fluids mentioned can be mixed with another of the fluids mentioned, for example a gas in a liquid, a gas in a gas or a gas in a liquid-gas mixture, etc.
  • the two fluids can be different or the same. Without limiting the generality, the example of a mixture of a gas in a main gas stream of another gas will be considered below.
  • the system according to the invention for mixing two fluids has a main pipe for transporting a first fluid in a downstream direction of the main pipe.
  • Downstream direction is to be understood as meaning a flow essentially parallel to the longitudinal axis of the main pipe, in particular in front of the distributor and optional static mixing elements. After the distributor, turbulent flow areas can arise, with the resulting mixture continuing overall flows downstream.
  • the system according to the invention further has a distribution device for supplying and distributing a second fluid inside the main tube, this distribution device having a plurality of radial tubes extending in the radial direction of the main tube, one end of which is arranged along a circumference of the main tube and which is located in extend the interior of the main pipe.
  • each radial tube has openings in its tube jacket, which are designed for the supply of the second fluid into the interior of the main tube.
  • “Arranged along a circumference of the main tube” means here that the radial tubes are arranged at certain points on the main tube in the circumferential direction of the main tube. These protrude into the interior of the main pipe.
  • a radial tube can extend over the entire cross section of the main tube. It is also possible for a radial tube to extend up to the longitudinal axis of the main tube, so that two or more radial tubes meet on the longitudinal axis of the main tube. Finally, it is also possible for a radial tube to only extend up to a predetermined distance from the longitudinal axis of the main tube. These possibilities will be discussed below.
  • an optimal mixing of the second fluid into the main flow of the first fluid can be achieved.
  • a very high mixing quality is achieved after the distribution device or the distributor. This allows the total length of the mixer (including optional static mixing elements) and thus the volume of the mixer to be significantly reduced.
  • a reduction in the volume of the mixer is advantageous in terms of safety, especially if mixing is to be carried out in the explosion area.
  • the mixer according to the invention or the mixing system according to the invention also does not produce any recirculation areas or dead zones, which are associated with increased local residence times, which should also be avoided, particularly in the mixture of oxygen and hydrocarbon mentioned.
  • the radial tubes extend with their other ends, i.e. with their ends protruding into the interior of the main tube, up to a predefined distance from the longitudinal axis of the main tube. Said end of each radial tube can be completely closed so that the second fluid is supplied via the mentioned openings in the tube jacket of a radial tube, or the end of the radial tube can be closed except for at least one opening, so that the second fluid is additionally supplied through this at least one opening at the end of a radial tube.
  • the respective other ends i.e. the ends of the radial tubes projecting into the interior of the main tube, are connected to a central tube section arranged axially inside the main tube.
  • This can improve the stability of the radial tubes and also have a positive effect on the flow properties.
  • the connection between said other end of the radial tube and the central tube section can have at least one opening which is designed for the supply of the second fluid into the interior of the main tube.
  • the openings in the tube jacket of a radial tube either have the same opening diameter or two, three or more different opening diameters. In this way it is possible to supply different areas inside the main pipe with second fluid through the different opening diameters. In this way, the entire cross-sectional area of the main pipe can be supplied with the second fluid as evenly as possible.
  • an opening with a first opening diameter is surrounded by two openings with a second opening diameter along a first arrangement direction.
  • openings with a first opening diameter and openings with a second opening diameter can alternate along a first arrangement direction.
  • exactly one opening located as centrally as possible in the radial tube along the first arrangement direction with a first, in particular larger opening diameter can be surrounded by two openings with a second, in particular smaller opening diameter at equal distances, so that a central area within the cross-sectional area is supplied with second fluid as evenly as possible can.
  • openings with a third along a second arrangement direction on the radial tube circumference which runs in particular parallel to the first arrangement direction Opening diameters are arranged.
  • the openings with the third opening diameter are arranged in greater density along the second arrangement direction compared to the openings with the first or second opening diameter.
  • the first opening diameter is larger than the second opening diameter and the second opening diameter is larger than the third opening diameter.
  • other arrangements can be selected in order to achieve the most uniform possible distribution over the cross section with this second fluid.
  • the openings in the tube jacket of a radial tube are arranged such that the second fluid flows into the downstream direction of the main tube and/or at an angle of at most 45° to the downstream direction, the downstream direction being parallel to the longitudinal axis of the main tube Inside the main pipe flows in.
  • the openings in the tube jacket of a radial tube in such a way that the second fluid flows in an upstream direction of the main tube and/or at an angle of at most 45° to the upstream direction, the upstream direction running parallel to the longitudinal axis of the main tube , flows into the interior of the main pipe.
  • the second fluid flows counter to the first fluid as it exits the radial tube.
  • the openings in the tube jacket of a radial tube are arranged such that the second fluid flows in a direction perpendicular to the downstream direction of the main tube and/or at an angle of at most 45° to the direction perpendicular to the downstream direction, the downstream direction being parallel to the longitudinal axis of the main pipe, flows into the interior of the main pipe.
  • the second fluid exits at a substantially right angle to the flow direction of the first fluid. This can also achieve good mixing. It has been shown that a combination of all three, but especially also the first and last-mentioned options, can deliver a good mixing result.
  • the distributor device comprises an annular space which at least partially surrounds the circumference of the main tube, along which the radial tubes are attached, one end of which is connected to the annular space in order to supply second fluid introduced into the annular space into the radial tubes transport.
  • the annular space in particular has a feed connection for supplying the second fluid.
  • Second fluid introduced into the annular space in this way is consequently distributed within the annular space, which is arranged in the circumferential direction and at least part of the circumference of the main pipe. From this annular space, the second fluid can flow into the radial tubes.
  • One end of the radial tubes is open and its circumference is connected to the casing of the main tube.
  • the second fluid that flows into a radial pipe then passes through the openings in the pipe jacket of the radial pipe into the interior of the main pipe.
  • the main pipe can have openings in its pipe jacket in the area of the annular space surrounding it, which allow the second fluid to be fed from the annular space into the interior of the main pipe. In this way, second fluid can flow into the interior of the main pipe directly on the inside of the main pipe.
  • the openings in the tube jacket of the main tube can be arranged in such a way that an opening with a fourth opening diameter is surrounded by two openings with a fifth opening diameter along a third arrangement direction, in particular Openings with a sixth opening diameter are arranged along a fourth arrangement direction, which runs in particular parallel to the third arrangement direction.
  • the fourth opening diameter is larger than the fifth opening diameter and the fifth opening diameter is larger than the sixth opening diameter, with the openings with the sixth opening diameter in particular being arranged in a closer order than the openings along the third arrangement direction, so the openings with the fourth or fifth opening diameter.
  • the fourth opening diameter is equal to the first opening diameter
  • the fifth opening diameter is equal to the second opening diameter
  • the sixth opening diameter is equal to the third opening diameter.
  • the present mixing system according to the invention is particularly, but not exclusively, suitable for mixing oxygen or an oxygen-containing gas as the second fluid in a hydrocarbon or a gas comprising a hydrocarbon as the first fluid.
  • An example of this is the oxidative dehydrogenation of ethane to ethylene (ODHE).
  • the second aspect of the invention relates to the use of the system explained above for feeding oxygen or an oxygen-containing gas as a second fluid into hydrocarbon or a hydrocarbon such as ethane-containing gas as a first fluid, in particular in an ODHE process, at an operating pressure of 2 to 20 bar or in particular 2 to 10 bar or more in particular 3 to 6 bar, the second fluid being fed to the radial tubes at 10 to 40 degrees Celsius or in particular at 20 to 30 degrees Celsius or further in particular at about 25 degrees Celsius.
  • the flow ratio in the main pipe of the second fluid (e.g. oxygen or oxygen-containing gas) to the first fluid e.g.
  • ethane or fluid containing ethane) flowing in the main pipe is 0.1 to 0.8 kg/kg or in particular 0.15 to 0.5 kg/kg or more particularly 0.3 to 0.4 kg/kg, the temperature of the mixture being in particular 150 to 350 degrees Celsius or in particular 200 to 300 degrees Celsius or more particularly 240 to 260 degrees Celsius.
  • FIG. 1 shows a schematic perspective view of an embodiment of a system 100 for mixing two fluids.
  • the illustrated system 100 is cut in a horizontal and a vertical direction to facilitate understanding.
  • the system 100 includes a main pipe 110 for transporting a first fluid in a downstream direction of the main pipe 110 and a manifold 120 for supplying and distributing a second fluid within the interior of the main pipe 110.
  • the distributor device 120 has a plurality of radial tubes 130 (in this example six radial tubes 130) extending in the radial direction of the main tube 110, one end 132 of which is arranged along a circumference of the main tube 110, the radial tubes 130 extending into the interior of the main tube 110 extend.
  • Each radial tube 130 has openings 134, 136, 138 in its tube jacket, which are designed for the supply of the second fluid into the interior of the main tube 110.
  • an oxygen stream is used as the first fluid, which is mixed into a second fluid, here a hydrocarbon stream.
  • a second fluid here a hydrocarbon stream.
  • gases and/or liquids and/or liquid-gas mixtures can be used as first and second fluids.
  • the radial tubes 130 extend with their other ends 133, i.e. with their ends 133 extending into the interior of the main tube 110, up to a predefined distance from the longitudinal axis 112 of the main tube 110.
  • the ends 133 can in principle be closed.
  • the second fluid (for example the oxygen stream) can be added to the radial tubes 130 by suitable feed devices.
  • the distributor device 120 includes an annular space 150 for this purpose, which at least partially surrounds a circumference of the main tube 110, along which the radial tubes 130 are attached, one end 132 of which is connected to the annular space 150 in order to accommodate second fluid introduced into the annular space 150 to be transported into the radial tubes 130.
  • the annular space 150 for its part has a feed connection 160 for supplying the second fluid into the annular space 150.
  • the openings in the tube jacket of a radial tube 130 are equipped with different, flow-optimized hole diameters in order to achieve the most uniform possible mixing over a respective open cross section inside the main tube 110.
  • the openings 134, 136, 138 in the tube jacket of a radial tube 130 have three different opening diameters. Visible in Figure 1 is an opening 134 with a first opening diameter, an opening 136 with a second opening diameter and an opening 138 with a third opening diameter, the first opening diameter being larger than the second and the second opening diameter being larger than the third.
  • a particularly uniform mixing of second fluid into the respective open cross section inside the main pipe 110 can be achieved by a special arrangement of these openings 134, 136, 138, as described further below in connection with Figure 2 is explained.
  • the openings 134, 136, 138 in the tube jacket of a radial tube 130 are in the exemplary embodiment Figure 1 arranged such that the second fluid flows through openings 138 with smaller opening diameter in the downstream direction of the main pipe as well (to a lesser extent, as shown in Figure 3 can be seen) flows into the interior of the main pipe 110 in the opposite upstream direction of the main pipe and through openings 134, 136 with a larger opening diameter in a direction substantially perpendicular to the downstream direction of the main pipe. This also allows the interference to be designed to be flow-optimized.
  • FIG. 1 In the exemplary embodiment according to Figure 1 is along a first arrangement direction 311 (see Fig. 3 ) an opening 134 with a first opening diameter surrounded by two openings 136 with a second opening diameter.
  • a second arrangement direction 312 (see Fig. 3 ) openings 138 are arranged with a third opening diameter. It is advantageous if the second arrangement direction runs parallel to the first arrangement direction and if the openings 138 along the second arrangement direction are arranged closer than the openings along the first arrangement direction.
  • the opening 134 has a larger opening diameter than the openings 136.
  • the opening 134 is surrounded by two openings 136.
  • the smaller openings are arranged along a second arrangement direction which is substantially parallel to the first arrangement direction.
  • the openings 138 with the third opening diameter are arranged closer than the openings 134,136 along the first arrangement direction.
  • the openings 134, 136 transport second fluid in a direction that is substantially perpendicular to the downstream direction of the main tube 110.
  • the openings 138 transport second fluid at a small angle thereto due to the curvature of the jacket surface of the radial tube 130, this angle being at most 45°.
  • the subsequent series of openings with the smallest diameter transport the fluid in a direction downstream of the main pipe 110.
  • FIG. 1 Also shown are further openings 114, 116, 118 in the tube jacket of the main tube 110 in the area of the annular space 150. More precisely, these openings 114, 116, 118 are attached between one end 132 of the radial tubes 130. These openings 114, 116, 118 are arranged in an analogous manner to the openings 134, 136, 138.
  • a third arrangement direction 313 see Fig. 3
  • an opening 114 with a fourth opening diameter is surrounded by two openings 116 with a fifth opening diameter.
  • a fourth arrangement direction 314 which runs parallel to the third arrangement direction, openings 118 with a sixth opening diameter are arranged in a denser arrangement.
  • the fourth opening diameter is equal to the first
  • the fifth opening diameter is equal to the second
  • the sixth opening diameter is equal to the third.
  • FIG. 2 The fluidic effect of this arrangement of the openings 114, 116, 118 and 134, 136, 138 is in Figure 2 to see.
  • a section of a cross section of the main pipe 110 can be seen, this section being essentially delimited by two radial pipes 130 following one another in the circumferential direction and the corresponding section of the pipe jacket of the main pipe 110.
  • the cross-sectional section is to be understood here less as a plane, but rather as a region of finite Thickness to represent the corresponding second fluid mixing areas of both openings 134, 136 and 116, 114 as well as the second fluid mixing areas across the adjacent rows of openings 138 and 118, respectively.
  • FIG. 2 Shown are the mixing areas 210 for the second fluid via the large openings 134, 114. These mixing areas 210 overlap and are to be located in the center of the cross-sectional section (“central area”). Furthermore Shown are mixing areas 220 for second fluid via the central openings 136, 116. These mixing areas also overlap and are located in the corner areas.
  • the openings 138, 118 are present, i.e. the small openings that lead to mixing areas 230.
  • the mixing areas are in turn superimposed, so that the edge area is essentially continuously supplied with second fluid. Overall, the arrangement of the openings shown results in optimal coverage of the cross-sectional section with second fluid.
  • the embodiment according to Figure 1 for an EDHOX process for example, at an operating pressure of 2 to 10 bar, preferably at 3 to 6 bar, for example at about 5 bar.
  • Oxygen can be added via the feed port 160 at, for example, 20 to 30 degrees Celsius, in particular 22 to 28 degrees Celsius, for example at approximately 25 degrees Celsius.
  • the ratio of the flow rates of the oxygen (or the oxygen-containing gas) and the hydrocarbon flowing in the main pipe 110 is preferably 0.1 to 0.8 kg / kg, in particular 0.15 to 0.5 kg / kg and particularly preferably between 0.3 and 0.4 kg/kg at a mixing temperature of, for example, 220 to 280 degrees Celsius, in particular 240 to 260 degrees Celsius, for example about 250 degrees Celsius.
  • the opening diameter of the openings 134 with a large opening diameter can be, for example, 20 to 24 mm, in particular approximately 22 mm
  • the opening diameter of the medium-sized openings 136 can be, for example, 14 to 18 mm, in particular 16 mm
  • the opening diameter of the small openings 138 can, for example 4 to 8 mm, in particular 6 mm.
  • the opening diameter of the opening 142 in the central tube section 140 can be, for example, between 6 and 10 mm, in particular 8 mm.
  • Figure 3 shows schematically in another perspective view the system 100 for mixing two fluids Figure 1 . Only the type of perspective view is changed here, whereby Figure 1 the system 100 from the downstream side and Figure 3 the system 100 shows from the upstream side. It can be seen that no openings with the smallest opening diameter 138 are arranged in the radial tubes 130, which release second fluid in an upstream direction of the main tube 110. Only the ones in Figure 3 Openings 138 shown along the arrangement direction 312 (and the corresponding further openings 138) release second fluid in this direction at a small angle (at most 45 °) to the upstream direction. The arrangement directions 311 and 312 are easier to see due to the larger view.
  • the openings 114 and 116 are arranged in the pipe jacket of the main pipe 110 along a third arrangement direction 313 and the openings 118 are arranged in a fourth arrangement direction 314.
  • the distribution device 120 and the system 100 for mixing two fluids full reference is made to the explanations of the exemplary embodiment Figure 1 referred.
  • FIG 4 shows schematically another embodiment of a system 100 for mixing two fluids in a perspective view.
  • the annular space 150 can be clearly seen, which surrounds the main tube 110 on the part of the circumference shown, as well as the various openings 134, 136 and 138 in the tube jacket of each radial tube 130 and the openings 114, 116 and 118 in the tube jacket of the Main tube 110 in the areas between the radial tubes 130.
  • the arrangement of these openings corresponds to that of the exemplary embodiment Figure 1 .
  • the radial tubes 130 are arranged with their ends 133 projecting into the interior of the main tube 110 in such a way that the ends 133 are connected to one another.
  • the respective ends 133 can be closed or opened, so that second fluid can spread between two opposite radial tubes 130.
  • FIG. 5 schematically shows another embodiment of a system 100 for mixing two fluids in a perspective view.
  • the embodiment is similar to that of Figure 3 , so that full reference is made to the above explanations in connection with Figure 3 is referred.
  • a flow body 540 is arranged in the central tube section 140.
  • the flow body 540 includes a hemispherical geometry in the front upstream part and a conical geometry in the rear downstream part.
  • flow bodies 540 can also have a teardrop shape. It is also possible to create a flow body 540 by rotating the upper part of a cross section of an airfoil profile about the corresponding chord. The use of such a flow body 540 arranged axially inside the main pipe improves mixing and homogenizes the flow of the mixture through the main pipe 110.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
EP22020382.2A 2022-08-10 2022-08-10 Système de mélange de deux fluides Pending EP4321242A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP22020382.2A EP4321242A1 (fr) 2022-08-10 2022-08-10 Système de mélange de deux fluides

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP22020382.2A EP4321242A1 (fr) 2022-08-10 2022-08-10 Système de mélange de deux fluides

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Publication Number Publication Date
EP4321242A1 true EP4321242A1 (fr) 2024-02-14

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050056313A1 (en) * 2003-09-12 2005-03-17 Hagen David L. Method and apparatus for mixing fluids
DE102011078181A1 (de) * 2011-06-28 2013-01-03 Robert Bosch Gmbh Vorrichtung und Verfahren zum Einbringen eines Reduktionsmittels in einen Abgasstrang
EP2680957A1 (fr) * 2011-03-01 2014-01-08 Basf Se Procédé et dispositif de mélange de deux courants de fluide
CN105214528A (zh) * 2015-09-11 2016-01-06 中国石油化工股份有限公司 一种烯烃与氧气的混合器

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050056313A1 (en) * 2003-09-12 2005-03-17 Hagen David L. Method and apparatus for mixing fluids
EP2680957A1 (fr) * 2011-03-01 2014-01-08 Basf Se Procédé et dispositif de mélange de deux courants de fluide
DE102011078181A1 (de) * 2011-06-28 2013-01-03 Robert Bosch Gmbh Vorrichtung und Verfahren zum Einbringen eines Reduktionsmittels in einen Abgasstrang
CN105214528A (zh) * 2015-09-11 2016-01-06 中国石油化工股份有限公司 一种烯烃与氧气的混合器

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
BEISPIEL IVARS, F.LOPEZ NIETO, J. M.: "Handbook of Advanced Methods and Processes in Oxidation Catalysis: From Laboratory to Industry", 2014, IMPERIAL COLLEGE PRESS, article "Light Alkanes Oxidation: Targets Reached and Current Challenges", pages: 767 - 834
GÄRTNER, C.A. ET AL.: "Oxidative Dehydrogenation of Ethane: Common Principles and Mechanistic Aspects", CHEMCATCHEM, vol. 5, no. 11, 2013, pages 3196 - 3217, XP055533676, DOI: 10.1002/cctc.201200966
X. LIE. IGLESIA: "Kinetics and Mechanism of Ethane Oxidation to Acetic Acid on Catalysts Based on Mo-V-Nb Oxides", J. PHYS. CHEM. C, vol. 112, 2008, pages 15001 - 15008, XP002771194

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