WO2012064628A1 - In-situ vaporizer and recuperator for alternating flow device - Google Patents
In-situ vaporizer and recuperator for alternating flow device Download PDFInfo
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- WO2012064628A1 WO2012064628A1 PCT/US2011/059520 US2011059520W WO2012064628A1 WO 2012064628 A1 WO2012064628 A1 WO 2012064628A1 US 2011059520 W US2011059520 W US 2011059520W WO 2012064628 A1 WO2012064628 A1 WO 2012064628A1
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- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
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- B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
- B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
- B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
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- 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
- C01B3/46—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 discontinuously preheated non-moving solid materials, e.g. blast and run
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D3/00—Burners using capillary action
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K5/00—Feeding or distributing other fuel to combustion apparatus
- F23K5/02—Liquid fuel
- F23K5/14—Details thereof
- F23K5/22—Vaporising devices
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
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- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
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- C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
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- 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
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to an in situ vaporizer and heat recover ⁇ 7 apparatus for an alternating flow system that can be located on-board a transportation vehicle.
- hydrocarbons, or water to vapor streams prior to chemical conversion.
- the current invention describes a novel in-situ. vaporizer and heat recovery device particularly suitable for alternating flow reactor systems where the flow through the device alternates between a liquid vaporization mode and a reheating mode.
- it is part of a pressure-swing reformer ("PSR") system as described in US Patent 7,491,250 for example. It enables the design of compact syngas generation systems, which may he deployed, for example, in transportation vehicles.
- PSR pressure-swing reformer
- the present inventors have discovered particular design criteria of such an in-situ vaporizer and heat recovery device that are required for it to achieve the above described advantages. These features include specifications on geometry, heat capacity and heat transfer, flow channel dimensions, and void fraction and void fraction gradient to minimize the size and weight of the de vice. A unique combination of these design criteria produce a high efficiency vaporizer/recuperator as demonstrated in an application to pressure swing reforming as taught in the above referenced patent.
- the present invention relates to a device for converting a liquid feed stream to a gaseous vapor stream comprising: (a) channel means having a first and second end, said channel means having a plurali ty of channels connecting said first and second end, said channel means having a substantially solid region and a void region, (b) inlet means for directing the liquid feed stream to the first end of the plurality of channels, and (c) outlet means for directing the gaseous vapor stream from said plurality of channels, where said channels have, at any distance x between the inlet and outlet, a geometric configuration, perpendicular to the feed flow direction characterized by (1 ) a void area A'(x), and (2) a total cross-sectional area A(x), where the void area AYx) as a fraction of the total area A(x) is
- A(x) and an average void fraction along a length of device L is L
- the void fraction varies along the length of the device.
- the average variation in void volume, as projected over the total length of the device ranges from about 0.01 to about 0.5.
- the device has sequential constant void volume regions, which regions vary along the device length.
- Figure 1 hereof is a schematic representation of an embodiment of the present invention.
- the present invention is directed to a device for converting a supplied liquid stream(s) to a gaseous vapor stream. More particularly, the invention relates to a device operating in a cyclic process whereby a liquid hydrocarbon and, optionally, a water mixture is converted into a mixture of hydrocarbon vapor and optionally steam.
- a liquid hydrocarbon and, optionally, a water mixture is converted into a mixture of hydrocarbon vapor and optionally steam.
- One particular application is for vaporization of a liquid hydrocarbon and water stream for use in a pressure swin steam reforming process.
- the device is designed for continuous operation through a cyclic two- stage process.
- the first stage is a vaporization mode
- the second stage is a reheating mode.
- design criteria or features that produce an in-situ vaporizer and heat recovery device capable of large dynamic ranges of operation, minimal pressure drop, corrosion resistance, and be sufficiently compact and light weight for mobile applications. These features include specifications on geometry, heat capacity and heat transfer capability, flow channel dimensions, and the void fraction and gradient of the void fraction within the vaporizer,
- the device of the present invention is comprised of a partially porous media with void passages comprising a set of characteristic sizes and shapes.
- the void regions within the device form a set of connected pathways by which fluid (in either the liquid or gaseous state) can pass through the device.
- a simplified conceptual device geometry is shown in Figure 1 for illustration.
- the void fraction, or fractional porosity is the open fraction of the volume of the de vice at a given point in space. Fluid may enter either end of the device, and exit at the opposite end.
- a first purpose of the de vice is to vaporize a supplied liquid stream to vapor. As illustrated in Figure 1 , the surface by which the liquid stream to be vaporized enters the device (1 1) will be defined as the inlet surface here identified as (10).
- the surface through which the vaporized stream exits is defined as the outlet surface (12).
- a high temperature re-heat stream may enter through either the inlet or outlet surface, and exit the correspondin opposite end.
- the reheat stream is shown flowing counterflow to the vaporization flow (16).
- the reheat stream (14) is illustrated in Figure 1 as entering the outlet surface stream (12) and exiting at the inlet surface (10) as stream (15).
- the device is illustrated as a cylindrical device having constant cross-sectional area.
- the device cross-sectional shape is not limited to cylindrical, but may be rectangular, square, triangular, or otherwise.
- the cross-sectional area may also vary as a function of axial position.
- a liquid or mixture of liquids or liquid- containing stream (16) enters the device at inlet (10) at a given volumetric liquid flow rate Q liq .
- This liquid flow is vaporized to a gas-phase stream that can be characterized in terms of a Normal gaseous volumetric flow rate, Q vap , with knowledge of the density and molecular weight of its components.
- the liquid phase may alternatively be supplied through a pre-atomized liquid stream forming a liquid droplet spray.
- the liquid or liquid spray enters, impacts the pre-heated surfaces within (11), and changes from the liquid to vapor phase, which exits the device as a vaporized stream (17).
- a gaseous stream either as vapor of liquid stream (16) or as diluent, may enter the device along with the liquid stream (16) and exit alongside vaporized stream (17). Any material that is already gaseous before entering the device during the vaporization period is not considered to be part of Qj lq or Q vap , although it must be considered in calculation of dew points.
- a heated stream (14) is passed through the device for a period of time t regan with a volumetric flow rate Qrege entering one end of the device and exiting the opposite end as a cooled stream (15).
- This is the re -heating or regeneration step.
- this stream enters the device (1 1) at the outlet end (12) and exits at the inlet end (10).
- the stream may enter the device (1 1) at the inlet end (10) and exits at the outlet end (12).
- An element of the invention is that both vaporization and reheat periods of operation of the device share the same flow paths.
- the regenerative flow heats the device from an initial temperature (in one embodiment approximately around the dew point of the liquid feeds) to a final higher temperature which is higher than the dew point of the liquid streams at the prescribed operating pressure.
- the dew point identified herein as T DEW is known in the art as the temperature at which a vapor just begins to condense, and is dependent on stream composition and pressure.
- the flows are varied in a periodic manner, alternating between the endothermic vaporization phase (energy transfer to the fluid phase from the solid material) and exothermic regenerative heat transfer phase (energy transfer from the fluid flow to the solid material).
- the initial and final temperature of the device are determined from the coupling of the flow conditions (such as flow rate and velocity), geometric considerations such as device size and design, and the diemiophysical properties of both the fluid and the device.
- the present invention provides the specification for the geometric channels that conduct flow through the vaporizer. Such channels are defined as open or "void" spaces separated by solid wails.
- the walls themselves may include some porosity, typically with pore diameters well below 0.1 mm. Such porosit is not counted as "void” as used in the present specification, and is counted only as a reduction of the apparent densit of the solid walls.
- the geometric features of the device of the present invention are related to the magnitude of void fraction, the spatial variation of the void fracti on, and the size and shapes of the small channel features which comprise the void fraction.
- 0 X is the void fraction at a given spatial location is denoted by the subscript x
- the total cross-sectional area of the device at this plane is A(x)
- the "open” or "void area” which contains no solid material in that plane is given by A'(x).
- x follows the direction of vaporizing flow (16), and has a value of zero at the device inlet (10 ⁇ and a value of L to tai at the device outlet ( 12), where L to tai is the length of the device from inlet to outlet along the axis of fluid flow.
- plane (19) is perpendicular to this axis of flow.
- planes are also known in the art as "axial planes”.
- the average porosity, or average void fraction, along a certain length of the device L is defined b :
- the average void fraction 0 a of the device is a parameter that leads to successful operation of the device.
- W T e have discovered that acceptable average void fraction for the device of the present inventi on ranges between 0.3 and 0.95.
- the device average void fraction ranges from 0.4 to 0,7.
- the void fraction varies axially along the length of the device.
- length of the device we mean the dimension along which the vapor flow predominantly occurs.
- this dimension or direction is axial, here indicated by dimension or direction "x.”
- the surface void fraction at the inlet surface (10) of the device has been found to preferably be between 0.5 and 0.995. A most preferred range at this location ranges from 0.65 and 0.995.
- the void fraction at the outlet surface (12) of the device is preferred to range from 0.2 and 0.7. A most preferred range of outlet void fractions ranges from 0.35 and 0.6.
- the variation may be generated either through a continuous change of void fraction or through a sequential series of constant void fraction regions.
- the void fraction is varied, tha t variation of void fraction can be characterized as an a verage variation over the length of the device.
- the set of 0 X values from inlet (10) to outlet (12) can be analyzed by least squares methods that are known in the art to compute a least- squares linear slope of 0 X versus x. This average variation can be expressed as a slope or gradient (i.e.
- the average total void fraction change is between 0.01 and 0.5.
- the preferred average total void fraction change is 0.15 to 0.35.
- the acceptable ranges of the axialiy device-averaged void fraction gradient vary between 0.01 and 0.5 void fraction decrease per linear inch of length.
- the preferred variation of the average void fraction gradient is 0.15 to 0.35 void fraction decrease per linear inch length.
- the number of preferred regions is greater than one and less tha twenty. The more preferred number of regions is between two and ten, and a most preferred number between two and five.
- the void volume is comprised of a large number of structured, small scale void regions denoted in the following as channels or channel regions.
- channels are made of simple shapes and in a range of sizes.
- Preferred shapes for the cross-sections of the channel size void regions are highly structured, regular shapes, such as circular, semi-circular, annular, periodic wavy-walled corrugation, or rectangular channels and slots.
- One embodiment of the device is to have the channels geometries nearly identical in size and shape throughout the device volume.
- a preferred embodiment of the device is to have nearly identical channel shapes within the device, with varying sizes at different axial locations (i.e. sets of circular channels with different diameters).
- An even more preferred embodiment of the device is to have an axial variation of both the channel shapes and sizes. Stated otherwise, changing the shape and/or size may increase the surface area available for heat transfer and thereby vaporization.
- An alternative embodiment utilizes chaotic channels of wormhoie networks comprised of mil lions of irregular channel shapes, such as a material characteristic of ceramic or metal foams.
- An additional embodiment utilizes the structures passages created by the interwoven networks of wire materials, such as made from stacking or weaving of metallic w ires.
- the channel shapes that make up the void regions of the device can be characterized by a set of spatial dimensions.
- One dimension is referred to as hydraulic diameter.
- a channel hydraulic diameter can be defined in terms of the axial plane (19) described in connection with Figure 1.
- d h '(x) 4 A'(x)/P'(x), where A'(x) represents the total void area of the device at a given axial location, and P'(x) is the total length of the intersecting surface between the solid and void region.
- a characteristic horizontal size of the device h cliar is approximated by taking the square root of the device volume to the total axial length, or
- the inlet region is preferably between about 5% and about 40% of the device length.
- the inlet region is between 10% and 30% of the device length.
- the orientation of the channels within the inlet region are preferably arranged such that movement of the incoming inlet flow stream is possible perpendicular to its average direction of flow. This allows a dispersive mixing component and a distribution component to the flow.
- a preferred design has a. flow pathway perpendicular to flow axis that is in proportion to the characteristic horizontal size(h j ia3 .) concurrent with the flow in the axial direction.
- a preferred design has, within the inlet region, a
- perpendicular to flo axis continuous flow pathway that is at least 10%, to as much as 50% of the characteristic horizontal size(h c ii av ). of the device.
- Other preferred designs have a continuous flow pathway of at least ⁇ ., ⁇ 3
- the acceptable characteristic channel hydraul ic diameter sizes, d ⁇ i ' x), in the inlet region of the device range from 0.1 to 1 0 mm, with a preferred range of 0.3 to 5 mm, and an even more preferred range of 0.7 to 2 mm.
- the characteristic channel sizes at the outlet of the devi ce range from 0.2 to 5 mm, with a preferred range of 0.4 to 2 mm, and an even more preferred range of 0.5 to 1.5 mm.
- the ratio of the channel hydraulic diameter to channel length is between 0.5 and 10,000, with a preferred ratio between 10 and 5000, and an even more preferred ratio between 40 and 200.
- An additional characteristic parameter of the device is the internal surface area available for vaporization of the incoming stream, and for reheating of the recuperator volume.
- S v S / V
- S the interior surface area
- V void + solid volume
- S V)avg 8 ⁇ 3 ⁇ / V tota i ⁇
- a preferred value of the average range of internal surface area per unit volume is between 20 inVhr and 1000 in7hr .
- An even more preferred value of the average range of internal surface area per unit volume is between 50 in 2 / in 1 and 250 inVin 3 .
- composition of the materials which comprise the device are such that the thermal heat capacity have a value at least 100 J kg-K, with a preferred value greater than 500 J/kg, and an even more preferred heat capacity value greater than 1000 J/kg.
- thermal contact between various regions of the device should be maximized.
- acceptabl e values of the thermal conductivity of the materials be at least 10 W/m-K, with a prefeiTed value greater than 50 WVm-K, and an even preferred value greater than 200 W/m-K.
- the composition of the materials which comprise the device are such that the density of the solid materials should be at least 2500 kg/m 3 , with a preferred value greater than 5000 kg/ m " , and an even more preferred value greater than 7000
- m liq is the mass flow rate of the liquid
- A, !q is the latent heat of vaporization of the liquid in mass units
- z vaB is the time period of injection
- Q vao is the Normal volumetric gaseous flow rate of vaporized liquid
- ⁇ ⁇ is the latent heat of vaporization of the liquid in Normal gas volume units.
- the amount of energy required is proportional to the rate of liquid supply, the vaporization energy per unit mass (or volume) of the fluid, and the length of time of the process.
- both the liquid basis and converted gaseous basis expressions are shown includin their conversion factors. Normal gas conditions are known in the art and are typically taken as 0°C and 1 atm absolute.
- the vaporization capacity of the device is directly proportional to its available energy storage.
- the highest temperature of the device will be at the time of the beginning of the liquid injection step.
- the average temperature of the device at this time is T DV i-
- T D y F final average temperature
- we define ATDBVICE to be the average temperature difference in the device from the beginning to the end of the liquid injecti on process (T DVi - T DVF ).
- the absolute values of the high and low temperatures will depend on the device properties, and the heat balance and operating conditions of the process.
- the maximum vaporization capacity of the device H' is given by
- p device is the a verage density of the solid material of the device
- ⁇ is the average porosity of the device
- C derke is the average specific heat capacity of the device is mass units
- the vaporization capacity is proportional to the specific heat capacity, solid material volume, and material density of the device, and also directly proportional to the temperature
- the space velocity of a. system can be expressed as the Normal volumetric hourly gas flow rate of feed divided by the volume of the device, called the gaseous hourly space velocity, or GHSV.
- the gaseous feed rate is calculated as a molar rate of feed, and the Normal volume rate calculated as if the substances are gaseous species.
- a liquid water feed flowing at rate of 1 g/sec entering a 0.5 liter device has a gaseous hourly space velocity for the liquid injection step given by
- Q vm is the Normal volumetric gas flo rate (in units of NL/hr) and ⁇ ,.. ! ⁇ is the total device volume.
- the compactness and resulting efficiency of the device in terms of rate of vaporization capacity per unit volume is directly proportional to the space velocity.
- the overall space velocity of the system is proportional to the productivity of the system. It is desirable for the space velocity to have as high a value as possible.
- the space velocity GHSV is preferably greater than 500, and even more preferably greater than 1000.
- the amount of heat consumed in the vaporization step is balanced by the amount of heat deposited in the device during the reheat (regeneration) portion of the cycle.
- I f the l iquid feed is fed at a high rate (high G HSV), then the heat is used up rapidly and the cycle time must be short. If the liquid feed is fed at a low rate (low GHSV ), then the heat is used up slowly and the cycle time is longer.
- the heat transfer requirements of the device can be expressed as a product of the volumetric heat of vaporization of the liquid feeds and the GHSV of the feed streams.
- the volumetric heat transfer requirement for vaporization is:
- porous media comprised of solid materials with characteristic channel passage shapes can be characterized by a heat transfer coefficient (h) and a characteristic heat transfer surface area. (A). Preferred values for the surface area per unit volume characteristics were defined above. Correlations for the heat transfer coefficient based on gas and solid properties are also known in the art. These heat transfer coefficients are a.
- volumetric heat transfer coefficient can be defined and given in units of
- volumetric heat transfer requirement for vaporization rewritten in consistent time units can be written as
- the present invention has a characteristic heat transfer temperature change as the ratio of the volumetric vaporization requirement to volumetric heat transfer coefficient for regeneration of the device. This characteristic
- This temperature differential describes the balance between the heat transfer supply and demand during the cyclic operation of the device. As used here, this is based on heat transfer coefficients used in the reheat portion of the cycle, which is typically the lower heat transfer coefficient portion of the cycle and serves as a limiting design condition. This temperature difference is a basic design parameter for the device. The device design and material properties chosen to satisfy the requirements of the invention.
- the characteristic AT Hr is preferably be between about 0.1 ° C and 600 ° C. More preferably, the characteristic AT Hr should be between 0.5 ° C and 300 " C.
- An additional feature of the device is a low axial resistance to flow in order to minimize pressure drop during both vapor production and reheat regeneration processes.
- An axial flow resistance can be defined for orthotropic resistance such as laminar flow through small channels:
- ⁇ is the pressure drop from factional resistance
- L is the averaging spatial length
- dx is the local incremental axial distance
- ⁇ ⁇ is the local void fraction
- GHSV is the gaseous hourly space velocity (in units ofhr "1 )
- ⁇ is the fluid viscosity
- p c is the cell number density per unit area (number of channels per unit cross sectional area of the device). All values are taken to be functions of the local coordinate, such that the overall pressure drop is the integral contribution from all axial sections of the device.
- the pressure drop is constrained by the channel size, the number density of cells per unit area, the porosity , and the GHSV (flow per unit volume) of the device.
- the porosity is related to the channel size by the expression
- the physical parameters of the device are selected in a manner to meet the design constraints of the system for operation.
- the design condition is selected based on maximum flow conditions in the regions of the device with the smallest flow passageways.
- a feature of the de vice for successful operation is that it operate with a low axial resistance to flow, such that the overall average ⁇ per unit length of the device is less that 5 psi/inch.
- a range of parameters which is acceptable for the device allow a pressure drop between 0.01 and 5 psi/inch, with a preferred range between 0.03 and 1 psi/inch pressure drop.
- the device may be constructed using an arrangement of thin, corrugated sheets of various metallic composition rolled into a tight concentric rings or stacked into closely spaced layers.
- the corrugation geometry generates a series of small annular cells.
- the diameter of the cells may be varied by changing the thickness of the rolled material sheets and the density of the corrugated concentric rings or sheets, and by varying the tightness of packing along its axial length.
- the material is comprised of sheets of Fecralloy® metal. The corrugation and sheet thicknesses for this design are selected to result in an overall porosity (open volume) of
- a high porosity inlet region has a. porosity of approximately 80%. This high porosity enables a significantly higher degree of liquid penetration into the interior volume of the device.
- the interior of the device comprises a monoli th having an intermediate value of porosity of about 60%, which is utilized as a transition between the low porosity inlet and high porosity outl et regions of the de vice.
- the sheets are made of continuous pieces of material in the axial direction, but of varying lengths.
- the cellular design of the device is such as to provide minimal pressure drop from the supplied fluid streams in either direction. Low pressure drop operation is particularly useful for applications invol vin reheating of the device by high velocity, high temperature gaseous streams which would incur substantial pressure drop losses.
- This device is particularly useful with a cyclic endothermic steam reforming process with an exothermic regeneration process to produce synthesis gas.
- a mixture of liquid hydrocarbon fuel and liquid water are injected using electronic fuel injectors onto the top (inlet) surface and into the internal volume of the vaporizer.
- the vaporized mixed stream then flows downward through a Gas Mixer and subsequently into the Reaction Zone where the feed is steam reformed into synthesis gas, using energy in the bed previously deposited from the reheat portion of the cycle.
- This synthesis gas passes out of the device at the bottom and can be utilized externally.
- a carbon monoxide, hydrogen, and possibly also fuel mixture is combusted.
- This high temperature stream is then used to reheat the catalyst bed of the Reaction Zone.
- the cycle returns to liquid injection mode.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
- Exhaust Gas After Treatment (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Hydrogen, Water And Hydrids (AREA)
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Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201180054061.0A CN103201002B (zh) | 2010-11-09 | 2011-11-07 | 用于交替流装置的原位汽化器和同流换热器 |
EP11781980.5A EP2637757A1 (en) | 2010-11-09 | 2011-11-07 | In-situ vaporizer and recuperator for alternating flow device |
AU2011326221A AU2011326221B2 (en) | 2010-11-09 | 2011-11-07 | In-situ vaporizer and recuperator for alternating flow device |
JP2013538802A JP2014504199A (ja) | 2010-11-09 | 2011-11-07 | 交液流デバイス用のインサイチュでの蒸発器および復熱器 |
KR1020137014843A KR20140041392A (ko) | 2010-11-09 | 2011-11-07 | 교번 유동 장치용 동일 반응계 내 기화기 및 폐열 회수기 |
SG2013034657A SG190166A1 (en) | 2010-11-09 | 2011-11-07 | In-situ vaporizer and recuperator for alternating flow device |
CA2817381A CA2817381A1 (en) | 2010-11-09 | 2011-11-07 | In-situ vaporizer and recuperator for alternating flow device |
MX2013005231A MX2013005231A (es) | 2010-11-09 | 2011-11-07 | Vaporizador y recuperador in situ para dispositivo de flujo alterno. |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
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US41151210P | 2010-11-09 | 2010-11-09 | |
US61/411,512 | 2010-11-09 | ||
US13/289,215 | 2011-11-04 | ||
US13/289,215 US20120111315A1 (en) | 2010-11-09 | 2011-11-04 | In-situ vaporizer and recuperator for alternating flow device |
Publications (1)
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WO2012064628A1 true WO2012064628A1 (en) | 2012-05-18 |
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PCT/US2011/059520 WO2012064628A1 (en) | 2010-11-09 | 2011-11-07 | In-situ vaporizer and recuperator for alternating flow device |
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US (1) | US20120111315A1 (ja) |
EP (1) | EP2637757A1 (ja) |
JP (1) | JP2014504199A (ja) |
KR (1) | KR20140041392A (ja) |
CN (1) | CN103201002B (ja) |
AU (1) | AU2011326221B2 (ja) |
CA (1) | CA2817381A1 (ja) |
MX (1) | MX2013005231A (ja) |
SG (1) | SG190166A1 (ja) |
WO (1) | WO2012064628A1 (ja) |
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US9315430B2 (en) | 2011-12-08 | 2016-04-19 | Exxonmobil Chemical Patents Inc. | Reactor components |
CN105214568B (zh) * | 2014-06-10 | 2018-04-20 | 万华化学集团股份有限公司 | 一种加热器、该加热器的用途和应用该加热器制备异氰酸酯的方法 |
WO2020206158A1 (en) | 2019-04-05 | 2020-10-08 | Exxonmobil Research And Engineering Company | Hydrogen production with integrated co2 capture |
EP3959171A1 (en) | 2019-04-24 | 2022-03-02 | ExxonMobil Research and Engineering Company | Reverse flow reactors with selective flue gas cascade |
EP3959170A2 (en) | 2019-04-24 | 2022-03-02 | ExxonMobil Research and Engineering Company | Reverse flow reactors with selective flue gas management |
JP2022545711A (ja) | 2019-08-26 | 2022-10-28 | エクソンモービル・テクノロジー・アンド・エンジニアリング・カンパニー | 逆流反応器中のco2水素化 |
JP2022545712A (ja) | 2019-08-26 | 2022-10-28 | エクソンモービル・テクノロジー・アンド・エンジニアリング・カンパニー | 逆流反応器のためのプロセス強化 |
JP2023541942A (ja) | 2020-09-16 | 2023-10-04 | エクソンモービル テクノロジー アンド エンジニアリング カンパニー | リバース・フローリアクタにおけるアンモニアおよび尿素の製造 |
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US20090238751A1 (en) * | 2007-11-02 | 2009-09-24 | University Of Connecticut | Process Intensification In Microreactors |
EP2123618A1 (en) * | 2008-05-13 | 2009-11-25 | L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Ceramic foam with gradient of porosity in heterogeneous catalysis |
DE102008031083A1 (de) * | 2008-07-01 | 2010-01-07 | J. Eberspächer GmbH & Co. KG | Verdampferbaugruppe für einen Verdampferbrenner eines Heizgerätes, insbesondere für ein Fahrzeug |
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US6634864B1 (en) * | 2002-02-19 | 2003-10-21 | Vapore, Inc. | High fluid flow and pressure in a capillary pump for vaporization of liquid |
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JP3913624B2 (ja) * | 2002-07-11 | 2007-05-09 | 本田技研工業株式会社 | 蒸発器 |
JP3889328B2 (ja) * | 2002-07-11 | 2007-03-07 | 本田技研工業株式会社 | 蒸発器 |
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US8899020B2 (en) * | 2006-08-21 | 2014-12-02 | Southwest Research Institute | Apparatus and method for assisting selective catalytic reduction |
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JP2010132482A (ja) * | 2008-12-03 | 2010-06-17 | Ngk Insulators Ltd | リアクタ |
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2011
- 2011-11-04 US US13/289,215 patent/US20120111315A1/en not_active Abandoned
- 2011-11-07 CN CN201180054061.0A patent/CN103201002B/zh not_active Expired - Fee Related
- 2011-11-07 WO PCT/US2011/059520 patent/WO2012064628A1/en active Application Filing
- 2011-11-07 CA CA2817381A patent/CA2817381A1/en not_active Abandoned
- 2011-11-07 EP EP11781980.5A patent/EP2637757A1/en not_active Withdrawn
- 2011-11-07 SG SG2013034657A patent/SG190166A1/en unknown
- 2011-11-07 KR KR1020137014843A patent/KR20140041392A/ko not_active Application Discontinuation
- 2011-11-07 MX MX2013005231A patent/MX2013005231A/es unknown
- 2011-11-07 AU AU2011326221A patent/AU2011326221B2/en not_active Expired - Fee Related
- 2011-11-07 JP JP2013538802A patent/JP2014504199A/ja active Pending
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US7491250B2 (en) | 2002-06-25 | 2009-02-17 | Exxonmobil Research And Engineering Company | Pressure swing reforming |
US20040175326A1 (en) * | 2003-02-28 | 2004-09-09 | Frank Hershkowitz | Pressure swing reforming for fuel cell systems |
US20090238751A1 (en) * | 2007-11-02 | 2009-09-24 | University Of Connecticut | Process Intensification In Microreactors |
EP2123618A1 (en) * | 2008-05-13 | 2009-11-25 | L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Ceramic foam with gradient of porosity in heterogeneous catalysis |
DE102008031083A1 (de) * | 2008-07-01 | 2010-01-07 | J. Eberspächer GmbH & Co. KG | Verdampferbaugruppe für einen Verdampferbrenner eines Heizgerätes, insbesondere für ein Fahrzeug |
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MX2013005231A (es) | 2013-08-01 |
CA2817381A1 (en) | 2012-05-18 |
SG190166A1 (en) | 2013-06-28 |
CN103201002B (zh) | 2015-04-22 |
KR20140041392A (ko) | 2014-04-04 |
US20120111315A1 (en) | 2012-05-10 |
JP2014504199A (ja) | 2014-02-20 |
AU2011326221A1 (en) | 2013-05-30 |
EP2637757A1 (en) | 2013-09-18 |
AU2011326221B2 (en) | 2016-12-22 |
CN103201002A (zh) | 2013-07-10 |
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