WO2013008009A1 - Appareil pour oxydation adiabatique partielle de méthane - Google Patents

Appareil pour oxydation adiabatique partielle de méthane Download PDF

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Publication number
WO2013008009A1
WO2013008009A1 PCT/GB2012/051634 GB2012051634W WO2013008009A1 WO 2013008009 A1 WO2013008009 A1 WO 2013008009A1 GB 2012051634 W GB2012051634 W GB 2012051634W WO 2013008009 A1 WO2013008009 A1 WO 2013008009A1
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chamber
reactor
methane
porous
reactor according
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PCT/GB2012/051634
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English (en)
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James BANISTER
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Gas2 Limited
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—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
    • B01J15/00—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor
    • B01J15/005—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2425—Tubular reactors in parallel
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2475—Membrane reactors
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/004—Sparger-type elements
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature

Definitions

  • the present invention relates to a process and apparatus for hydrocarbon conversion. More particularly, the present invention relates to a process and apparatus for adiabatic methane conversion into synthetic gas (i.e. syngas).
  • synthetic gas i.e. syngas
  • Non-catalytic partial oxidation does not require the high levels of steam but the very high process temperatures (>1200degC) create energy efficiency challenges of their own.
  • Rhodium has been found to be highly selective in the oxidation with minimal coke formation allowing the partial oxidation process to be run at much lower temperatures. The process does not require steam to operate, although small quantities (10% vol% of the methane feed) are frequently described as a means of increasing the hydrogen to carbon monoxide ratio in the resultant syngas.
  • DE 101 14173 describes a system whereby the oxygen is transported from the heated air stream to the side of the reactor containing the hydrocarbon by ion-transport through a selective membrane that rejects nitrogen. The two sides are separated by a gas-tight wall that is non-porous but conducts oxygen ions and is therefore referred to as ion- transport membranes.
  • An alternative term is dense membrane. Ion transport membranes rely on high temperatures of operation to maintain the oxygen flux at sufficient levels for economic relevance.
  • the inlet air must be heated to the operating temperature of the membrane, typically around 800-900degC, however the partial oxidation reaction is exothermic and so the heat of reaction from the partial oxidation of methane would then result in a temperature rise of the reacting fluids to a temperature in excess of l OOOdegC.
  • the exchange of heat from one fluid to another is a means by which the process fluids surrounding ion-transport membranes and therefore the membrane itself can be maintained within the well defined temperature range in which it must be operated.
  • the catalyst is porous and no gas-tight barrier is provided.
  • ion-transport membrane that contain packed catalyst particles, e.g. Hoang et.al, Int. J. Hyd. Ener.
  • the length and diameter of the ion-exchange membrane influences the catalyst performance.
  • oxygen flux through the membrane wall to the catalyst pellets contained within is known to be the limiting rate, rather than the amount of catalyst that the tube can hold and so a longer, thinner membrane, which increases the surface area to volume ratio of the membrane, is preferred.
  • the partial oxidation of methane is a very rapid reaction that takes place at temperatures in excess of 600 degC.
  • the feed or catalyst is preheated to at least 400degC to achieve light off (Journal of catalysis, 249 (2007) pp380-393 Horn et al.) of the catalyst is achieved and good selectivity to carbon monoxide is achieved.
  • the temperature of the gases passing over the catalyst rapidly rises and under adiabatic conditions (no heat loss) the product gases leaving the reactor can be in excess of 900 degC. It is also beneficial if the reaction can be performed at elevated pressure since most of the processes that utilise syngas to form another chemical do so at raised pressure and the costs of compressing the component feed streams (comprising methane and oxygen) is less than compressing the resultant syngas. This is principally as a result of the increase in gas volumes that accompany the reaction.
  • the partial oxidation of methane as described in US 7,641 ,888 (Gobina) is found to have similar characteristics in that it is most beneficially carried out at elevated temperature and pressure.
  • the alternative to construction with an exotic alloy is to refractory line the inside of the vessel to reduce heat transfer to the pressure containing shell such that external heat losses results in the shell being maintained at a significantly lower temperature than the gases within the reactor.
  • the demands on the material of construction of the unit are therefore reduced and a cheaper lower specification material can be utilised.
  • the cheapest form of reactor for a high temperature reactor is a refractory lined pressure vessel with no heat transfer to a utility fluid (an adiabatic reactor). This is well known to an engineer who is skilled in the art of reactor design.
  • a reactor for the partial oxidation of methane where a first and second reactant gas react in a channel surrounded by a porous catalytic reaction zone where the hydraulic mean diameter of the channel is more than 5mm.
  • a reactor for the partial oxidation of methane comprising:
  • a first chamber forming a passageway for a first reactant gas (e.g. in the form of oxygen); a second chamber forming a passageway for a second reactant gas (e.g. in the form of methane);
  • a first reactant gas e.g. in the form of oxygen
  • a second chamber forming a passageway for a second reactant gas (e.g. in the form of methane);
  • a porous, non-gas-tight catalytic membrane separating the first and second chambers, said membrane being capable of allowing all the components of the first reactant gas (e.g. oxygen) to permeate, not by an ion-transport mechanism, from the first chamber through to the second chamber to react with the second reactant gas (e.g. methane) in a reaction zone of the apparatus;
  • the first reactant gas e.g. oxygen
  • the second reactant gas e.g. methane
  • the second chamber has a hydraulic mean diameter greater than 5mm and has a length greater than 500mm.
  • porous is meant non-dense.
  • the first reactant gas may be oxygen and the second reactant gas may be methane.
  • the hydraulic mean diameter in the second chamber may be selected from any of the following: greater than about 5mm; greater than about 10mm; or greater than about 15mm.
  • the hydraulic mean diameter in the second chamber may be from about 5mm to 20mm or about 10mm to 15mm.
  • the length of the second chamber may be selected from any of the following: longer than about 500 mm; longer than about 600 mm; longer than about 1 ,200 mm; longer than about 2,000 mm; or longer than about 5,000 mm.
  • the oxygen may be fed to the reactor through a porous zone that is separate from the porous catalyst containing zone where:
  • a fraction of the gas is allowed to pass from one chamber to another without passage through the catalytic membrane.
  • the reactor may be refractory lined. Therefore, a shell of the reactor may have an internal refractory material capable of self containing heat giving the reactor adiabatic features that will allow the recovery of heat after passing through the reactor.
  • the energy from the hot gases can then be used to generate energy or pre heat gases at the beginning.
  • the reaction may use air or any combination of oxygen enriched air.
  • the adiabatic reactor may also allow for cleaning in situ by means of Introduction of, for example, steam to improve gas inlet velocity, decrease carbon formation and improve hydrogen yields.
  • the adiabatic reactor may also allow introduction of nitrogen to enhance reactor performance and reduce the reaction temperature.
  • the adiabatic reactor may also allow gas product extraction on both sides of the membrane, in other words the adiabatic reactor enables recovery of the syngas produced through the middle of the reactor on the membrane side or through the shell of the adiabatic reactor.
  • the adiabatic reactor may also allow for in situ regeneration of catalyst.
  • the adiabatic reactor may be used for producing syngas in ratios of about 1 .8:1 H 2 /CO all the way to about 6:1 if desired.
  • the adiabatic reactor may therefore be used for handling; Natural gas, Coal Bed Methane and Biogas.
  • the adiabatic reactor may contain an extended membrane such that the seal between chambers is located outside of the reaction chamber in order to lower the temperature of operation of the seal.
  • the membrane may additionally contain an extended portion of more than 100 mm of non-porous section, created by the addition of a non-porous coating, which extends from the refractory lined cavity to the sealing section in order that the gases to not contact and react in the vicinity of the seal or outside the refractory lined section.
  • the membrane may additionally be free to move relative to the expansion and contraction of the reactor by locating one end of the membrane in a close fitting but non- sealing chamber that connects the two chambers.
  • a method for partially oxidizing methane comprising:
  • a first reactant gas e.g. in the form of oxygen
  • first reactant gas e.g. oxygen
  • second reactant gas e.g. methane
  • the second chamber has a length greater than 1 m and hydraulic mean diameter greater than 7mm.
  • the reactor may be as defined in the first, second, or third aspects.
  • Figure 1 shows this correlation between hydraulic mean diameter and Reynolds number for a series of catalyst channels with a fixed surface catalyst concentration and fixed pressure drop according to an embodiment of the present invention
  • Figure 2 is a schematic diagram of a porous membrane reactor according to an embodiment of the present invention.
  • Figure 3 is a representation of turbulence on reducing catalyst temperature in a cylindrical catalytic porous tube reactor according to an embodiment of the present invention
  • Figure 4 is a representation of the effect of increasing the mass transfer of oxygen by removal of a porous distributor according to an embodiment of the present invention
  • Figures 5a to 5d represent membranes for generating turbulence according to embodiments of the present invention
  • Figure 6 is a representation of a porous membrane reactor comprising a large central channel to allow insertion of a distributor and an external chamber designed to allow turbulence to develop according to an embodiment of the present invention without excessive residence time;
  • Figure 7 is a representation of a further porous membrane reactor comprising a porous oxygen distributor and large central chamber to allow turbulence to develop according to an embodiment of the present invention.
  • the present invention therefore relates to a reactor for the partial oxidation of methane using a porous walled channel capable of supporting turbulence for methane gas prior to reacting with oxygen gas.
  • the turbulence is created by forming the porous walled channel such that the flow of second gas has a Reynolds number of greater than 1000.
  • the Reynolds number Re is a dimensionless number that gives a measure of the ratio of inertial forces pV 2 /L to viscous forces ⁇ /L 2 and consequently quantifies the relative importance of these two types of forces for given flow conditions.
  • the concept was introduced by George Gabriel Stokes in 1851 , but the Reynolds number is named after Osborne Reynolds, who popularized its use in 1883.
  • reaction being sought in the present invention where the first reactant gas is methane and the second reactant gas is oxygen is the following partial oxidation reaction to form synthetic gas:
  • Figure 1 shows the correlation between hydraulic mean diameter and Reynolds number for a series of catalyst channels with a fixed surface catalyst concentration and fixed pressure drop. Figure 1 also illustrates the relationship between diameter and residence time.
  • the most beneficial diameter of catalyst channel is when turbulence is just achieved. Further increasing the diameter reduces the catalyst volume density unnecessarily increasing the reactor size.
  • the effect of the turbulence can be seen in the following CFD model of a porous catalyst channel.
  • the example shows a theoretical catalyst channel with a 37mm hydraulic mean diameter operating at low flow laminar regime and high flow turbulent regime.
  • One method of evaluating the performance of different reactor geometries is to model the reaction using accepted published kinetics.
  • the kinetics from Deutschmann and L.D. Schmidt Two-dimensional modeling of partial oxidation of methane on Rhodium in a short contact time reactor, Olaf Deutschmann and Lanny D. Schmidt, Twenty-Seventh Symposium (International) on Combustion/The Combustion Institute, 1998/pp. 2283-2291 ) undertaken in different reactor geometries has been cited worldwide by other authors can be used within a CFD model to determine the surface temperatures that would be present in different catalyst geometries.
  • FIG 2 is a schematic representation of an apparatus 8.
  • An oxygen (0 2 ) supply 18 is fed into the outer bore 22 at one end of the membrane apparatus 8, and a natural gas (which mainly comprises methane (CH 4 )) supply 20 is fed into the corresponding end of the inner bore 14.
  • the partial pressure of the oxygen 18 is maintained at a higher pressure than that of the methane supply 20, which results in the oxygen passing through the pores (not shown) of the modified membrane 10 from the outer bore 22 to the inner bore 14.
  • the oxygen molecules come into contact with the catalysts 12 present in the sidewall 13 of the modified membrane 10, which catalyses the reaction of the oxygen molecules with methane diffusing against the flow of gas in the membrane pores before oxygen reaches the bulk methane flow present in the inner bore of the modified membrane 10.
  • the catalyst lowers the activation energy of the reaction so that the reaction takes place at lower temperatures than the uncatalysed reaction and so as methane and oxygen contact in the presence of the catalyst syngas is instantly formed according to the following chemical reaction:
  • Pressure control of the oxygen supply 18 flow rate allows different flow rates of the methane supply 20 to be used, since an increase in the pressure of the oxygen supply will result in a greater flux of oxygen through the pores of the modified membrane 10.
  • a gas stream comprising the methane flows next to or through the catalyst impregnated layer 12.
  • the thermally stabilized gamma alumina layer 30 on the bore side 14 increases the specific surface area of the support and stabilizing a high surface area of metal catalyst which enhances the reaction between permeated oxygen and the methane.
  • the oxygen at point 18 may be fed at a rate of 5 - 500 L/min and the methane at point 20 may be fed at a rate of 10 - 1000 L/min.
  • the length and diameter of the inner bore 14 is selected to provide a Reynolds number of greater than 1000 such that turbulence within the inner bore will occur.
  • the unitless Reynolds number as defined by the ratio (rho x v x D/mu) (density x velocity x hydraulic mean diameter/viscosity) is an indication of whether turbulent or laminar flow is present in developed fluid flow.
  • a Reynolds number below 2000 for a smooth bore pipe, or below 1000 for a rough pipe is indicative that the fluid flow within the pipe will be in a laminar regime. At values higher than this then turbulence is sustained.
  • the Reynolds number can be determined using the hydraulic mean diameter, calculated from a ratio of the wetted perimeter and cross sectional area. Turbulence increases mass transfer by allowing local circulation of fluids and non- diffusion based transport of material. Similarly turbulence aids heat transfer by allowing convective as well as conduction mechanisms for heat transfer.
  • the temperature of the fluid (and catalyst) is controlled by transfer of the reaction heat away from the catalytic surface to a heat transfer surface and then into a secondary fluid. Turbulence again reduces the thickness of the boundary layer and enhances heat and mass transfer from the catalyst.
  • the surface temperature of the catalyst is not usually affected by the increased turbulence. Unlike with bulk well-mixed reactions where the reaction can continue in the absence of mass .transfer, with surface catalysed reactions the increase in heat transfer with turbulence also accompanies an increased mass transfer which can increase the reaction rate and the resultant rate of heating. The result of this is that the fluid in contact with the catalyst will remain at the temperature of the catalyst. This temperature will be no more than the adiabatic reaction temperature that can be calculated from a knowledge of the thermodynamic properties of the fluids and reactants.
  • the catalyst support is designed with a small channel size that enables a high volumetric concentration of catalyst to be used.
  • the channel size is only limited by the increasing pressure drop that results as the channel size is decreased. Increasing the channel size to more than the minimum required to avoid excessive pressure drop will result in a less effective reactor.
  • Figure 3 shows the effect of turbulence on reducing catalyst temperature in a cylindrical catalytic porous tube reactor.
  • Figure 4 shows the effect of removing the porous distributor on the catalyst temperature in the example described above at the high flow rate of 100 L/min. In particular, Figure 4 shows the effect of increasing the mass transfer of oxygen by removal of the porous distributor.
  • turbulence is achieved on the outside of the catalytic membrane without excessive residence time. This is most simply achieved by providing sufficient length of catalyst membrane such that the desired GHSV (gas hourly space velocity) results in turbulent flow. Typically this will require the chamber containing the methane to be at least 1 m in length surrounding a catalytic membrane of at least 25mm in diameter and for the outer chamber to have a hydraulic mean diameter of at least 5mm. It may be beneficial for the purposes of control and gas distribution for each membrane to be surrounded by a metal shroud that can control the direction of flow and aid turbulence.
  • a means of enhancing the turbulence and gas distribution such as a swirl device or other turbulence inducing device. While turbulence in the oxygen chamber may be beneficial where very high mass transfer in the methane chamber has already been achieved it is less necessary and generally a lower Reynolds number in the oxygen chamber should be maintained.
  • Figures 5a - 5d represent catalytic membranes for generating turbulence in a porous membrane reactor as previously described.
  • Figure 5a represents a membrane 100 made from ceramic with a diameter of about 25 mm.
  • the membrane 100 has a series of outer located channels 102.
  • This membrane configuration is only suitable for use with a reactor configuration as shown in figure 6 in which the oxygen containing stream passes down the channels 102 and the methane containing stream passes along the external surface of the membrane 100 unlike US 7,641 ,888.
  • the channels 102 are too small for turbulence to develop internally without causing a large pressure drop.
  • Figure 5b represents a membrane 120 which has a central channel 122 and a series of outer located channels 124.
  • the central channel has a large enough diameter to be used in either reactor configuration Figure 6 or Figure 7 as in the configuration shown in Figure 6and internal oxygen distributor can be fitted or in configuration shown in Figure 7 in which the methane flow passes through the central channel 122 turbulent methane flow can develop.
  • Figure 5c represents a membrane 130 with a simple large channel 132 which is similar in design and use as the configuration Figure 5b. In the configuration shown in Figure 5c thicker wall is utilised to enable a stable extrusion, whereas in Figure 5b the extrusion is made more stable through the use of a lighter but more complex and larger volume structure.
  • Figure 5d is a further membrane 140 where the number of spokes 142 has been minimised to achieve a balance between the hydraulic mean diameter of channels 144 and stability of the ceramic in the extrusion process.
  • the structure would typically have an external diameter in excess of 50mm and with individual channels 144 having hydraulic mean diameters in excess of 25mm. This structure is most suitable for use in reactor configuration Figure 7 in which the methane passes down the centre channels.
  • FIG. 6 is a further reactor of the present invention which specific component parts described below.
  • Reactant gas 21 1 contains methane and is fed into nozzle 208 entering the distribution chamber 214 that is bounded by the end plate 201 and the intermediate plate 202.
  • the reactant gas is at a temperature below 600 degC and the chamber 214 is protected from the high temperature chamber 218 by the refractory material 204 the principle metal of construction for the end plate and other items around chamber 214 can be 310 stainless materials.
  • the methane containing gas then passes through the plate 202 and refractory material 204 through an orifice 210, through a turbulence inducing device 215 such as a swirl generator into a chamber bounded by the sheath 205 and catalytic membrane 207.
  • the oxygen containing reactant gas 212 is fed via a manifold into each individual catalytic membrane through a cap 209.
  • the sealing cap 209 allows insertion of the membrane into the reactor and also forms a pressure seal against the plate 201.
  • Reactant gas 212 is prevented from mixing with reactant gas 21 1 by a metal sealing cylinder that surrounds the end of the catalytic porous membrane.
  • a porous distributor for the oxygen 216 is located down the centre of the catalytic membrane and sealed using a mineral seal such as a mica or exfoliated mica type of block seal around the end of the catalytic membrane.
  • the porous gas distributor and catalytic membrane are supported by structures 206 and 217.
  • the gap between the sheath 205 and the membrane 207 is typically about 25mm allowing turbulent flow to develop.
  • the sheath 205 and swirl device 215 work in conjunction to generate high local gas velocities particularly at the inlet of the methane where otherwise gas velocities and turbulence would be at a minimum. As the reaction proceeds there is an increase in the gas volume leading to higher velocities and higher levels of turbulence. At the chamber entrance where the velocities are lowest is also the location where turbulence is beneficial. Consequently, particularly where the Reynolds number of the flowing gas would be below 4000 it is beneficial at the chamber entrance to locally enhance methane gas velocities.
  • a swirl device 215 achieves this by imparting a rotational as well as linear velocity to the gas.
  • a flow guide or sheath 205 within the reactor can aid the onset of turbulence and with the addition of vanes could further increase gas velocities, while reducing dead volume and therefore reducing residence time within the reactor.
  • higher flow rates and with the largest diameter membranes, where the pitch of the tubes is no longer determined by the space requirement of the seal and sealing caps the sheaths may not be required.
  • the oxygen containing gas and methane containing gas contact in the porous catalytic membrane with bulk flow of gas from the centre of the porous catalytic membrane to the reaction chamber 218.
  • the syngas 213 produced by reaction of the oxygen and methane remains outside of the porous catalytic membrane and exits the shell of the reactor.
  • a geometry of membrane as shown in Figure 5b would be used with a membrane external diameter of approximately 50mm.
  • the porous catalytic membrane would be 207 approximately 3000mm long, manufactured from a thermally resistant alumina based ceramic containing 0.1 wt% rhodium as catalyst deposited onto a thermally stabilized alumina coating.
  • the main body of the reactor 201 can be manufactured from 310 stainless material as the refractory lining 204 protects the shell from excessive heat allowing use of a lower thickness material.
  • FIG. 7 is a further reactor of the present invention which specific component parts described below.
  • Oxygen containing gas 31 1 is fed into nozzle 308 and enters chamber 313 bounded by reactor end plates 301 and intermediate plate 302. Again the chamber 313 is maintained at a temperature below 600degC by the use of refractory lining 304.
  • the oxygen containing gas 31 1 is distributed into the main chamber 314 by passage along and through porous metallic or ceramic distributors 305. The distribution passage prevents stimulation of turbulence within the oxygen chamber as well as hindering the mass transfer of the oxygen to ensure good stoichiometry at the catalyst..
  • the methane containing gas 312 passes through the reactor sealing caps 312 into the centre of the porous catalytic membrane 307. The sealing caps 310 allows insertion of the membrane.
  • a device that enhances the turbulence within the central channel of the membrane may be a simple narrow tube to increase the local velocity, or a more complex injector with other fluids added e.g. water or device for turbulence induction (not shown).
  • a swirl device 215 achieves this by imparting a rotational as well as linear velocity to the gas.
  • the methane and oxygen are prevented from contacting within chamber 313 by a metal sleeve surrounding each catalytic membrane in this chamber.
  • the oxygen distribution tubes 305 and porous catalytic membrane 307 are supported by structure 306.
  • the syngas 313 produced travels down the centre of the membrane and exits into chamber 315.
  • Sealing is arranged around the membranes such that expansion and contraction of the membranes relative to the shell can occur without excessive mechanical stresses.
  • a sliding type of seal is suitable as a high degree of leak tightness is not required.
  • the seal allows a pressure differential to be maintained between the chamber 314 and chamber 315 driving the oxidant flow through the catalytic membrane.
  • a small amount of leakage is allowable as this does not affect the performance of the reactor and may be beneficial in moderating the pressure drop across the membrane at high flows.
  • a suitable membrane configuration for this reactor type would be Figure 5b or 5c with an internal diameter within the membrane of about 25mm and a length of membrane of approximately 3000mm.

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Abstract

La présente invention concerne un procédé et un appareil de conversion des hydrocarbures. Plus particulièrement, l'invention concerne un procédé et un appareil de conversion adiabatique du méthane en gaz synthétique (à savoir du gaz de synthèse).
PCT/GB2012/051634 2011-07-13 2012-07-11 Appareil pour oxydation adiabatique partielle de méthane WO2013008009A1 (fr)

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GB201112025A GB201112025D0 (en) 2011-07-13 2011-07-13 Improved apparatus for adiabatic methane partial oxidation

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112020392A (zh) * 2018-04-27 2020-12-01 林德有限责任公司 用于处理含硫化物的废碱液的方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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