WO2007045457A1 - Fluid mixing device inserted in or combined with a reactor - Google Patents

Fluid mixing device inserted in or combined with a reactor Download PDF

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Publication number
WO2007045457A1
WO2007045457A1 PCT/EP2006/010049 EP2006010049W WO2007045457A1 WO 2007045457 A1 WO2007045457 A1 WO 2007045457A1 EP 2006010049 W EP2006010049 W EP 2006010049W WO 2007045457 A1 WO2007045457 A1 WO 2007045457A1
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WO
WIPO (PCT)
Prior art keywords
zone
mixing
pipes
fluid
pipe
Prior art date
Application number
PCT/EP2006/010049
Other languages
French (fr)
Inventor
Andrea Bartolini
Luca Basini
Alessandra Guarinoni
Antonio Bennardo
Nicola Onorati
Original Assignee
Eni S.P.A.
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 Eni S.P.A. filed Critical Eni S.P.A.
Priority to EP06806365A priority Critical patent/EP1954386A1/en
Priority to US12/090,363 priority patent/US7815700B2/en
Priority to BRPI0617475-2A priority patent/BRPI0617475A2/en
Priority to CA2626481A priority patent/CA2626481C/en
Priority to JP2008535964A priority patent/JP5436859B2/en
Priority to CN2006800416650A priority patent/CN101304804B/en
Priority to EA200800841A priority patent/EA013043B1/en
Publication of WO2007045457A1 publication Critical patent/WO2007045457A1/en

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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
    • B01F25/3132—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices
    • 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
    • B01F25/3132—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices
    • B01F25/31322—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices used simultaneously
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00259—Preventing runaway of the chemical reaction
    • B01J2219/00265—Preventing flame propagation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/8593—Systems
    • Y10T137/87571—Multiple inlet with single outlet
    • Y10T137/87652—With means to promote mixing or combining of plural fluids

Definitions

  • the present invention relates to a device for mixing two fluids, preferably a hydrocarbon fuel and an oxidizing stream, such as air, enriched air or oxygen, which can be used, inserted in or combined with a reactor, also in catalytic partial oxidation processes with a short contact time .
  • a hydrocarbon fuel preferably a hydrocarbon fuel and an oxidizing stream, such as air, enriched air or oxygen, which can be used, inserted in or combined with a reactor, also in catalytic partial oxidation processes with a short contact time .
  • Short contact time - catalytic partial oxidation is a process used for the production of synthesis gas (syngas) .
  • synthesis gas syngas
  • pre-mixed streams of a hydrocarbon fuel, an oxidant (Air, enriched air or oxygen) and optionally vapour are fed at pressures ranging from 1 to 80 ATM and at a low temperature (T ⁇ 400°C) on a catalytic surface which becomes incandescent .
  • the reagent mixtures used in short contact time catalytic partial oxidation processes can be flammable. In order to avoid the triggering and propagation of flames, it is therefore advisable to effect the mixing in a limited volume, at temperatures lower than the triggering temperature of the flames and for times shorter than the flame- retarding times.
  • catalytic partial oxidation as the "cold" gas of the pre-mixed stream reaches a catalyst which is at a high temperature, it is also appropriate for the reagent gases to have high linear rates, so as to limit heat back-propagation phenomena from the catalytic surface to the stream of gaseous reagents. Furthermore, if the linear rates of the gases also exceed propagation rate of the flames, this extinguishes them.
  • the characteristics of the mixing system are therefore crucial in this type of process, as, in general, in all processes in which it is necessary to mix a fuel stream and an oxidant stream, avoiding flame reactions.
  • Various literature documents describe equipment for mixing hydrocarbon and oxidant streams .
  • US 2004/0133057 describes a method for producing a mixer capable of mixing an oxidant and a fuel stream in safe conditions, as the mixing is effected in a fluid kept under turbulent motion and consequently only micro- quantities of reagents enter into close contact, thus preventing possible flame reactions from spreading to the whole mixture.
  • this apparatus not easy to produce and run, but it also does not guarantee that the two streams, at the outlet of the mixer, have been perfectly mixed.
  • US 6,726,850 claims a CPO process wherein the total oxygen is incrementally fed during several reaction steps.
  • the patent discloses nothing with respect to the geometry of the injection apparatus, but indicates short contact times of the hydrocarbon mix/oxygen (less then 10 msec in the first step and 1 msec in the subsequent steps) .
  • US 5,883,138 claims an apparatus from which the pressurized and pre-heated reagents are injected with a comparable momentum through a mixer consisting of a series of channels and holes which are open towards the catalytic area.
  • the patent discloses that if the residence time of the HC/O 2 mix is longer than 9 msec, the methane and oxygen mixtures can start undesired non-catalytic reactions in the gas phase.
  • the same considerations made for US 2004/0067180 are also valid for this patent.
  • a device has now been found, using the principle of the partialized outlet of one of the two feeding streams, which allows the technological limits of the known art to be overcome, satisfying the above-mentioned requirements.
  • the device, object of the present invention, for mixing two fluids, inserted in, or combined with a reactor substantially comprises the following zones:
  • a mixing zone separated from the distribution zone by a pipe-plate supporting said pipes, preferably parallel, said pipe-plate having slits or openings in order to uniformly discharge the second fluid in an axial direction into the mixing area, and said parallel pipes extending beyond said pipe-plate into the mixing zone.
  • the final portion of the parallel pipes is preferably equipped with means suitable for partializing the outlet of the fluid axially and/or radially and/or transversally distributed therein in the mixing zone.
  • Said parallel pipes which extend beyond the pipe- plate, can also be of different lengths.
  • Suitable elements can be positioned in the mixing area, close to the pipe-plate, in order to stop the return of any possible flames.
  • a porous element can be placed in the mixing zone, im- mediately under the pipe-plate, which can extend beyond the pipes .
  • the device, object of the invention can be situated at the inlet of the reactor.
  • the diameter of the pipes of the gaseous fluid (oxi- dant) and of the "slits" is calculated so that the linear rates of the two streams prevent recirculating areas of the streams themselves, which, even if, on the one hand, can be useful for the mixing, on the other they increase the residence time of the gas in the mixing zones, thus increasing the chances of triggering phenomena and flame reaction propagation.
  • the distance between the elements for blocking possible flame-returns and the ends of the bundle of pipes, is such as to minimize the formation of vortexes which could generate the recycling of a portion of fuel inside the oxidizing stream, thus increasing the chances of flame formation.
  • the device, object of the invention can be preferably inserted at the inlet of the reactor, or combined with a reactor: in particular, the reactor described in patent application IT-MI96A000690 can be used.
  • Said device can also be part of the reactor itself and in this case the equipment including said device is a further object of the present invention.
  • the apparatus for effecting the catalytic partial oxidation of hydrocarbons is characterized in that it comprises the mixing device as described above, and in that it also comprises a reaction zone (R) , consisting of a catalytic bed, with a constant or increasing section along the axis of the apparatus.
  • R reaction zone
  • a further object of the present invention relates to the catalytic oxidation process of gaseous or liquid fuels, effected by means of equipment having the device described above .
  • This catalytic partial oxidation process of gaseous fuels selected from hydrocarbon compounds, natural gas and/or LPG is effected by means of suitable catalytic system using the apparatus described above and through the following steps : • premixing and possibly heating the reagents consisting of said fuels and oxygen or air or oxygen-enriched air, to temperatures ranging from 25 to 400 0 C, possibly in the presence of vapour and/or CO 2 ;
  • the process according to the invention can be effected for obtaining syngas or unsaturated hydrocarbons (ethylene, styrene, etc..) starting from liquid or gaseous fuels .
  • syngas or unsaturated hydrocarbons ethylene, styrene, etc..
  • the catalysts can consist of oxide carriers on which noble metals are deposited, such as Rh, Ru, Ir, Pt and/or other transition metals such as Ni, Fe, Co.
  • the oxide car- riers can consist of metal sponges with different geometries, or metal fibrous carriers on which the same metals are deposited.
  • the catalysts can consist of nitrides or oxy-nitrides containing noble metals and other transition metals such as Rh, Ru, Ir, Pt, Ni, Fe, Co. These metals can be supported on nitride species as metal aggregates, but they can also be inserted in the chemical formula of the nitride or oxy- nitride (A more detailed description of these catalysts can be found in patent application IT-MI2002A000214) .
  • the catalysts used in the process of the present invention can be in any form, preferably in the form of a fixed bed permeable to a fluid, in particular to a gas.
  • the fixed bed can have any form, and preferably a vacuum degree rang- ing from 0.4 to 0.95, more preferably from 0.6 to 0.9.
  • the device shown in figure 1 is equipped with two different inlets, for the fuel and for the oxidant. More spe- cifically, the oxidizing stream enters from the top of the mixer and is distributed in a series of pipes having a reduced diameter. The fuel enters from the side (several inlets can also be present) and is radially distributed in the mixing chamber which envelops the pipes in which the oxygen circulates, finally entering the mixing chamber by means of "slits" present in the pipe-plate.
  • the pipes of the oxidant i.e. air, enriched air or preferably oxygen, extend in length beyond the pipe-plate, so that the oxidant is released in an atmosphere “rich” in fuel (the opposite is potentially dangerous) .
  • the final portion of the oxidant pipes is equipped with suitable restriction elements, such as, for example, metal alloys or sintered ceramics, or a series of openings having suitable dimensions, so as to effect partialization along the outlet axis of the feeding.
  • suitable restriction elements such as, for example, metal alloys or sintered ceramics, or a series of openings having suitable dimensions, so as to effect partialization along the outlet axis of the feeding.
  • the advantage of said par- tialized outlet consists in the fact that the formation of mixtures is reduced within the flammability ranges.
  • the inlets of the oxidant and fuel shown in figure 1 are only illustrative and should not be interpreted as being a limita- tion of the invention; other inlets are possible, for example fuel from above, there still being an oxidant/fuel phase separation inside the mixer and the relative positioning of the outlets (oxidant in downstream with respect to the fuel) .
  • the stream containing oxygen at the outlet from the relative ducts (1) , flows through suitable elements (2) capable of partializing the charge into a series of streams which intersect the hydrocarbon phase (3) according to both perpendicular and parallel trajectories, or vector combinations of the same.
  • suitable elements (2) capable of partializing the charge into a series of streams which intersect the hydrocarbon phase (3) according to both perpendicular and parallel trajectories, or vector combinations of the same.
  • the rapid mixing of the streams prevents the local formation of compositions inside the flammability region.
  • An alternative scheme for the mixer envisages oxidant pipes with different lengths, so as to further partialize the oxygen release, with all the consequent advantages .
  • Figure 4 includes suitable elements, within the appara- tus of figure 2, capable of stopping possible flame- returns .
  • a porous element (5) is positioned at the outlet of the hydrocarbon stream; the outlets of the oxidant stream are also situated inside the porous element, possibly at various heights and downstream of the inlet of the hydrocarbon stream.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Catalysts (AREA)

Abstract

A device is described for mixing two fluids, inserted in or combined with a reactor, which can also be used for catalytic partial oxidation, substantially consisting of the following zones : - a first feeding zone equipped with means for allowing a first fluid, possibly gaseous under the operating conditions, to enter in an axial direction; - an underlying distribution zone containing a bundle of pipes preferably parallel to the axis inside which said fluid is uniformly distributed; - a second feeding zone equipped with means for allowing a second fluid to enter the distribution zone containing the bundle of preferably parallel pipes and to be uniformly distributed outside said parallel pipes; - a mixing zone separated from the distribution zone by a pipe-plate supporting said parallel pipes, said pipe-plate having slits or openings in order to uniformly discharge the second fluid in an axial direction into the mixing area, and said parallel pipes extending beyond said pipe -plate into the mixing zone.

Description

FLUID MIXING DEVICE INSERTED IN OR COMBINED WITH A REACTOR
The present invention relates to a device for mixing two fluids, preferably a hydrocarbon fuel and an oxidizing stream, such as air, enriched air or oxygen, which can be used, inserted in or combined with a reactor, also in catalytic partial oxidation processes with a short contact time .
Short contact time - catalytic partial oxidation (SCT- CPO) is a process used for the production of synthesis gas (syngas) . In catalytic partial oxidation with a short contact time, pre-mixed streams of a hydrocarbon fuel, an oxidant (Air, enriched air or oxygen) and optionally vapour, are fed at pressures ranging from 1 to 80 ATM and at a low temperature (T<400°C) on a catalytic surface which becomes incandescent .
The reagent mixtures used in short contact time catalytic partial oxidation processes can be flammable. In order to avoid the triggering and propagation of flames, it is therefore advisable to effect the mixing in a limited volume, at temperatures lower than the triggering temperature of the flames and for times shorter than the flame- retarding times. In catalytic partial oxidation, as the "cold" gas of the pre-mixed stream reaches a catalyst which is at a high temperature, it is also appropriate for the reagent gases to have high linear rates, so as to limit heat back-propagation phenomena from the catalytic surface to the stream of gaseous reagents. Furthermore, if the linear rates of the gases also exceed propagation rate of the flames, this extinguishes them.
The characteristics of the mixing system are therefore crucial in this type of process, as, in general, in all processes in which it is necessary to mix a fuel stream and an oxidant stream, avoiding flame reactions. Various literature documents describe equipment for mixing hydrocarbon and oxidant streams .
US 2005/0095186 claims an apparatus in which the fuel and oxidant are mixed thanks to the tangential motion of the fuel. In our opinion, this method does not prevent the local generation of oxygen concentration gradients, which are potentially harmful as they are capable of causing flame reactions.
US 2004/0133057 describes a method for producing a mixer capable of mixing an oxidant and a fuel stream in safe conditions, as the mixing is effected in a fluid kept under turbulent motion and consequently only micro- quantities of reagents enter into close contact, thus preventing possible flame reactions from spreading to the whole mixture. In our opinion, not only is this apparatus not easy to produce and run, but it also does not guarantee that the two streams, at the outlet of the mixer, have been perfectly mixed.
US 2004/0067180 describes a mixer consisting of micro- channels into which the oxidant and fuel are fed sepa- rately. It is advisable however for its positioning to be close to the catalytic area, which, in our opinion, can give considerable heat back-propagation problems, with the possibility of triggering flame reactions.
US 6,726,850 claims a CPO process wherein the total oxygen is incrementally fed during several reaction steps. The patent discloses nothing with respect to the geometry of the injection apparatus, but indicates short contact times of the hydrocarbon mix/oxygen (less then 10 msec in the first step and 1 msec in the subsequent steps) . US 5,883,138 claims an apparatus from which the pressurized and pre-heated reagents are injected with a comparable momentum through a mixer consisting of a series of channels and holes which are open towards the catalytic area. The patent discloses that if the residence time of the HC/O2 mix is longer than 9 msec, the methane and oxygen mixtures can start undesired non-catalytic reactions in the gas phase. The same considerations made for US 2004/0067180 are also valid for this patent.
US 6,863,867 claims the use of diffusive mixer groups arranged so as to introduce the charge both radially and tangentially. Each mixer consists of a series of ducts which receive the charge from one end and release it at the opposite end. Also in this case the patent does not disclose how to minimize the formation of regions in which the oxygen/hydrocarbon ratio falls within the flammability ranges .
A device has now been found, using the principle of the partialized outlet of one of the two feeding streams, which allows the technological limits of the known art to be overcome, satisfying the above-mentioned requirements.
The device, object of the present invention, for mixing two fluids, inserted in, or combined with a reactor, substantially comprises the following zones:
* a first feeding zone equipped with means for allowing a first fluid, possibly gaseous under the operating conditions, to enter in an axial direction;
* an underlying distribution zone containing a bundle of pipes preferably parallel to the axis inside which said fluid is uniformly distributed; * a second feeding zone equipped with means for allowing a second fluid to enter the distribution zone containing the bundle of preferably parallel pipes and to be uniformly- distributed outside said parallel pipes;
* a mixing zone separated from the distribution zone by a pipe-plate supporting said pipes, preferably parallel, said pipe-plate having slits or openings in order to uniformly discharge the second fluid in an axial direction into the mixing area, and said parallel pipes extending beyond said pipe-plate into the mixing zone. The final portion of the parallel pipes is preferably equipped with means suitable for partializing the outlet of the fluid axially and/or radially and/or transversally distributed therein in the mixing zone.
Said parallel pipes, which extend beyond the pipe- plate, can also be of different lengths.
Suitable elements can be positioned in the mixing area, close to the pipe-plate, in order to stop the return of any possible flames.
A porous element can be placed in the mixing zone, im- mediately under the pipe-plate, which can extend beyond the pipes .
The device, object of the invention, can be situated at the inlet of the reactor.
The diameter of the pipes of the gaseous fluid (oxi- dant) and of the "slits" is calculated so that the linear rates of the two streams prevent recirculating areas of the streams themselves, which, even if, on the one hand, can be useful for the mixing, on the other they increase the residence time of the gas in the mixing zones, thus increasing the chances of triggering phenomena and flame reaction propagation.
The distance between the elements for blocking possible flame-returns and the ends of the bundle of pipes, is such as to minimize the formation of vortexes which could generate the recycling of a portion of fuel inside the oxidizing stream, thus increasing the chances of flame formation.
The device, object of the invention, can be preferably inserted at the inlet of the reactor, or combined with a reactor: in particular, the reactor described in patent application IT-MI96A000690 can be used.
Said device can also be part of the reactor itself and in this case the equipment including said device is a further object of the present invention. The apparatus for effecting the catalytic partial oxidation of hydrocarbons is characterized in that it comprises the mixing device as described above, and in that it also comprises a reaction zone (R) , consisting of a catalytic bed, with a constant or increasing section along the axis of the apparatus. A further object of the present invention relates to the catalytic oxidation process of gaseous or liquid fuels, effected by means of equipment having the device described above . This catalytic partial oxidation process of gaseous fuels selected from hydrocarbon compounds, natural gas and/or LPG, is effected by means of suitable catalytic system using the apparatus described above and through the following steps : • premixing and possibly heating the reagents consisting of said fuels and oxygen or air or oxygen-enriched air, to temperatures ranging from 25 to 4000C, possibly in the presence of vapour and/or CO2;
• reacting the reagents in the catalytic zone, at inlet temperatures ranging from 5 to 5000C, at space velocity rates ranging from 1,000 to 1,000,000 Nl re- agents/L cat. x h, reaching temperatures ranging from 450 to 1,5000C.
In particular, the process according to the invention can be effected for obtaining syngas or unsaturated hydrocarbons (ethylene, styrene, etc..) starting from liquid or gaseous fuels .
The catalysts can consist of oxide carriers on which noble metals are deposited, such as Rh, Ru, Ir, Pt and/or other transition metals such as Ni, Fe, Co. The oxide car- riers can consist of metal sponges with different geometries, or metal fibrous carriers on which the same metals are deposited.
The catalysts can consist of nitrides or oxy-nitrides containing noble metals and other transition metals such as Rh, Ru, Ir, Pt, Ni, Fe, Co. These metals can be supported on nitride species as metal aggregates, but they can also be inserted in the chemical formula of the nitride or oxy- nitride (A more detailed description of these catalysts can be found in patent application IT-MI2002A000214) .
The catalysts used in the process of the present invention can be in any form, preferably in the form of a fixed bed permeable to a fluid, in particular to a gas. The fixed bed can have any form, and preferably a vacuum degree rang- ing from 0.4 to 0.95, more preferably from 0.6 to 0.9.
Some preferred embodiments of the present invention are provided with the help of figures 1-5.
The device shown in figure 1 is equipped with two different inlets, for the fuel and for the oxidant. More spe- cifically, the oxidizing stream enters from the top of the mixer and is distributed in a series of pipes having a reduced diameter. The fuel enters from the side (several inlets can also be present) and is radially distributed in the mixing chamber which envelops the pipes in which the oxygen circulates, finally entering the mixing chamber by means of "slits" present in the pipe-plate.
The pipes of the oxidant, i.e. air, enriched air or preferably oxygen, extend in length beyond the pipe-plate, so that the oxidant is released in an atmosphere "rich" in fuel (the opposite is potentially dangerous) .
The final portion of the oxidant pipes is equipped with suitable restriction elements, such as, for example, metal alloys or sintered ceramics, or a series of openings having suitable dimensions, so as to effect partialization along the outlet axis of the feeding. The advantage of said par- tialized outlet consists in the fact that the formation of mixtures is reduced within the flammability ranges. The inlets of the oxidant and fuel shown in figure 1 are only illustrative and should not be interpreted as being a limita- tion of the invention; other inlets are possible, for example fuel from above, there still being an oxidant/fuel phase separation inside the mixer and the relative positioning of the outlets (oxidant in downstream with respect to the fuel) . As shown in figure 2, the stream containing oxygen, at the outlet from the relative ducts (1) , flows through suitable elements (2) capable of partializing the charge into a series of streams which intersect the hydrocarbon phase (3) according to both perpendicular and parallel trajectories, or vector combinations of the same. The rapid mixing of the streams prevents the local formation of compositions inside the flammability region.
The crossing of the two streams further facilitates the rapid mixing of the phases. An alternative scheme for the mixer, shown in figure 3, envisages oxidant pipes with different lengths, so as to further partialize the oxygen release, with all the consequent advantages .
Figure 4 includes suitable elements, within the appara- tus of figure 2, capable of stopping possible flame- returns .
In a further configuration shown in figure 5, a porous element (5) is positioned at the outlet of the hydrocarbon stream; the outlets of the oxidant stream are also situated inside the porous element, possibly at various heights and downstream of the inlet of the hydrocarbon stream.

Claims

1. A device for mixing two fluids, inserted in or combined with a reactor, substantially consisting of the following zones : * a first feeding zone equipped with means for allowing a first fluid, gaseous under the operating conditions, to enter in an axial direction;
* an underlying distribution zone containing a bundle of pipes parallel to the axis inside which said fluid is uni- formly distributed;
* a second feeding zone equipped with means for allowing a second fluid to enter the distribution zone containing the bundle of parallel pipes and to be uniformly distributed outside said parallel pipes; * a mixing zone separated from the distribution zone by a pipe-plate supporting said parallel pipes, said pipe-plate having slits or openings in order to uniformly discharge the second fluid in an axial direction into the mixing area, and said parallel pipes extending beyond said pipe-plate into the mixing zone .
2. The device according to claim 1, wherein the terminal portion of the pipes is equipped with means for partializ- ing the outlet of the fluid distributed therein, axially, radially and/or transversally in the mixing zone.
3. The device according to claim 1, wherein the pipes extending beyond the pipe-plate are of different lengths.
4. The device according to claim 1, wherein suitable elements are positioned in the mixing zone, close to the pipe- plate to stop any possible flame-returns .
5. The device according to claim 1, wherein a porous element is positioned in the mixing zone, immediately behind the pipe-plate, which extends beyond the pipes themselves.
6. An apparatus for effecting the catalytic partial oxi- dations of hydrocarbons, characterized in that it comprises the mixing device as claimed in at least one of the claims from 1 to 6 and in that it also comprises a reaction zone (R) , consisting of a catalytic bed, with a constant or increasing section, along the axis of the apparatus.
7. A catalytic partial oxidation process of gaseous fuels, selected from hydrocarbon compounds, natural gas and/or LPG, by means of a suitable catalytic system effected with the equipment according to claim 6 and the following steps : • premixing and possibly heating the reagents consisting of said fuels and oxygen or air or oxygen-enriched air, to temperatures ranging from 25 to 4000C, possibly in the presence of vapour and/or CO2;
• reacting the reagents in the catalytic zone, at inlet temperatures ranging from 5 to 5000C, at space veloc- ity rates ranging from 1,000 to 1,000,000 Nl re- agents/L cat. x h, reaching temperatures ranging from 450 to 1,5000C.
PCT/EP2006/010049 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor WO2007045457A1 (en)

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EP06806365A EP1954386A1 (en) 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor
US12/090,363 US7815700B2 (en) 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor
BRPI0617475-2A BRPI0617475A2 (en) 2005-10-21 2006-10-18 device for mixing two fluids, apparatus for performing partial catalytic oxidation of hydrocarbons, and partial catalytic oxidation process of gaseous fuels
CA2626481A CA2626481C (en) 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor
JP2008535964A JP5436859B2 (en) 2005-10-21 2006-10-18 Liquid mixing device that is inserted into or combined with the reactor
CN2006800416650A CN101304804B (en) 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor
EA200800841A EA013043B1 (en) 2005-10-21 2006-10-18 Fluid mixing device inserted in or combined with a reactor

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ITMI20052002 ITMI20052002A1 (en) 2005-10-21 2005-10-21 DEVICE FOR MIXING FLUIDS INSERTED OR COMBINED WITH A REACTOR

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WO2008058646A1 (en) 2006-11-16 2008-05-22 Uhde Gmbh Process and apparatus for injecting oxygen into a reaction gas flowing through a synthesis reactor
DE102006054415A1 (en) * 2006-11-16 2008-05-21 Uhde Gmbh Method and device for injecting oxygen into a reaction gas flowing through a synthesis reactor
US8529117B2 (en) 2007-10-02 2013-09-10 Ineos Europe Limited Mixing apparatus for gases
US8500894B2 (en) 2007-12-14 2013-08-06 Dow Technology Investments Llc Wet scrubbing for removing particulate solids from oxygen supply line
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US8404189B2 (en) 2007-12-14 2013-03-26 Dow Technology Investments Llc Oxygen/hydrocarbon rapid (high shear) gas mixer, particularly for the production of ethylene oxide
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ZA200803415B (en) 2009-06-24
BRPI0617475A2 (en) 2011-07-26
US20080244974A1 (en) 2008-10-09
MA29927B1 (en) 2008-11-03
CN101304804A (en) 2008-11-12
CN101304804B (en) 2011-01-19
US7815700B2 (en) 2010-10-19
EA013043B1 (en) 2010-02-26
EA200800841A1 (en) 2008-10-30
EP1954386A1 (en) 2008-08-13
CA2626481C (en) 2014-03-11
ITMI20052002A1 (en) 2007-04-22
JP5436859B2 (en) 2014-03-05
JP2009512544A (en) 2009-03-26

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