WO2004047973A2 - Method for reducing the lightoff temperature of a catalyst - Google Patents

Method for reducing the lightoff temperature of a catalyst Download PDF

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Publication number
WO2004047973A2
WO2004047973A2 PCT/US2003/036983 US0336983W WO2004047973A2 WO 2004047973 A2 WO2004047973 A2 WO 2004047973A2 US 0336983 W US0336983 W US 0336983W WO 2004047973 A2 WO2004047973 A2 WO 2004047973A2
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WO
WIPO (PCT)
Prior art keywords
catalyst
fuel
temperature
working fluid
lightoff
Prior art date
Application number
PCT/US2003/036983
Other languages
French (fr)
Other versions
WO2004047973A3 (en
Inventor
Maxim Lyubovsky
Robert N. Carter
Original Assignee
Precision Combustion, Inc.
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Filing date
Publication date
Application filed by Precision Combustion, Inc. filed Critical Precision Combustion, Inc.
Priority to AU2003291099A priority Critical patent/AU2003291099A1/en
Publication of WO2004047973A2 publication Critical patent/WO2004047973A2/en
Publication of WO2004047973A3 publication Critical patent/WO2004047973A3/en

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Classifications

    • 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
    • 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
    • B01J8/0207—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 the fluid flow within the bed being predominantly horizontal
    • B01J8/0214—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 the fluid flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
    • 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
    • B01J2208/00008—Controlling the process
    • B01J2208/00716—Means for reactor start-up
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/63—Platinum group metals with rare earths or actinides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2430/00—Influencing exhaust purification, e.g. starting of catalytic reaction, filter regeneration, or the like, by controlling engine operating characteristics
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2430/00—Influencing exhaust purification, e.g. starting of catalytic reaction, filter regeneration, or the like, by controlling engine operating characteristics
    • F01N2430/04—Influencing exhaust purification, e.g. starting of catalytic reaction, filter regeneration, or the like, by controlling engine operating characteristics by adding non-fuel substances to combustion air or fuel, e.g. additives
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
    • F01N3/10—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust
    • F01N3/18—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operation; Control
    • F01N3/20—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operation; Control specially adapted for catalytic conversion ; Methods of operation or control of catalytic converters
    • F01N3/2006—Periodically heating or cooling catalytic reactors, e.g. at cold starting or overheating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
    • F01N3/10—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust
    • F01N3/24—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by constructional aspects of converting apparatus
    • F01N3/30—Arrangements for supply of additional air

Definitions

  • the present invention is generally directed to a method for the operation of a catalytic reactor, and, more specifically, to a method for reducing the lightoff temperature of a catalyst within the catalytic reactor.
  • Catalytic reactors are well known devices for supporting many chemical reactions, such as exothermic oxidative reactions.
  • a catalyst which is in a catalyst bed, in the reactor needs to reach threshold temperature, commonly referred to as lightoff temperature.
  • the chemical reaction proceeds at the desired rate generally at a temperature substantially higher than the lightoff temperature.
  • auxiliary fluid such as air
  • resistive heating of a substrate on which the catalyst is positioned e.g. passing an electrical current through the substrate
  • preheating with a homogenous flame e.g., fuel and oxidant in an oxidation reactor
  • the working fluid e.g., fuel and oxidant in an oxidation reactor, may also be pre-heated to raise the temperature of the catalyst to the lightoff temperature. All these methods require auxiliary systems such as heaters, burners, or electric power sources adding to the cost and complexity of the system.
  • a starter fuel/oxidant mixture is used to raise the temperature of the catalyst to the lightoff temperature. After the lightoff temperature is achieved, the starter fuel/oxidant mixture is gradually replaced with an operational fuel/oxidant mixture.
  • This substitution strategy requires storage of multiple fuel types, storage of significant amounts of a starter fuel, and precise flow control during the switching process to avoid catalyst or catalytic reactor damage.
  • a catalyst supports an exothermic reaction between constituents of a working fluid. Based on the working fluid, the catalyst has a baseline lightoff temperature it must achieve before the exothermic reaction proceeds at a desired rate.
  • the working fluid is supplemented with a starter fuel prior to associating the working fluid with the catalyst.
  • the working fluid in association with the starter fluid in the presence of the catalyst defines a supplemented lightoff temperature that is less than the baseline lightoff temperature. As a result, the temperature rise required to lightoff the catalyst is reduced.
  • the start fuel may be discontinued after the supplemented lightoff temperature is reached.
  • each working fluid which has fuel and oxidant components, interacts differently with a catalyst, or catalysts, within a catalytic reactor.
  • the selection of a starter fuel depends on the interaction characteristics of the working fluid, starter fuel and the catalyst(s).
  • the amount of starter fuel added to the working fluid need not be significant.
  • the amount added is not sufficient in and of itself to interact with the catalyst(s) within the catalytic reactor to raise the catalyst(s) to a temperature at or above the lightoff temperature. It, however, is preferred that the starter fuel be more reactive than the fuel, or fuels, within the working fluid as to the catalyst, or catalysts, within the catalytic reactor.
  • FIG. 1. is a graph illustrating the relationship between lightoff temperature and operational temperature of a catalyst.
  • FIG. 2 depicts a cross-sectional view of a catalytic reactor in which the method disclosed herein might be employed.
  • a catalyst therein lights off when the catalyst temperature rises dramatically from an initial catalyst temperature to an operational temperature.
  • FIG. 1 shows this relationship.
  • the auxiliary heating profile denoted by reference number 10, shows the temperature of the catalyst as a function of the heat applied thereto.
  • the catalyst is heated from, for example, ambient conditions to a lightoff temperature, say T ⁇ .
  • T ⁇ a lightoff temperature
  • the catalyst temperature jumps nearly instantaneously from the lightoff temperature to a considerably higher operational temperature designated A.
  • the working fluid is supplemented with a starter fluid.
  • the lightoff temperature of the catalyst is reduced.
  • the baseline lightoff temperature i.e., the catalyst temperature that is required to lightoff the catalyst if only the working fluid is considered, denoted T is reduced to a supplemented lightoff temperature denoted T 2 .
  • the auxiliary heating required for the catalyst is similarly reduced.
  • the operational temperature of the catalyst is a function of lightoff temperature of the catalyst, the operational temperature of the catalyst is reduced from point A to point B when the lightoff temperature is reduced from the baseline lightoff temperature Tj to the supplemented lightoff temperature T 2 .
  • the temperature increase of the catalyst above the lightoff temperature results from the exothermic reactions between the components of the working fluid.
  • the operational temperature of the catalyst after lightoff is approximately equal to the sum of lightoff temperature and the temperature rise due to the exothermic reactions.
  • a reduction in catalyst lightoff temperature equates to a similar reduction in catalyst operational temperature.
  • points A and B are on a line designated 12 that is generally parallel to the auxiliary heating profile 10.
  • the amount of starter fuel required is minimal as compared to the amount of fuel in the working fluid.
  • the heat release of the starter fuel when reacted with oxidant in the working fluid in the presence of the catalyst is sufficiently low that it is incapable in and of itself of raising the initial catalyst temperature of the catalyst to the baseline lightoff temperature T While the method reduces the lightoff temperature, it is still anticipated that some auxiliary heating of the catalyst may still be required. This auxiliary heating could be by conventional methods known to those skilled in the art.
  • the method of the present invention is shown in conjunction with a fixed geometric catalytic reactor suitable for performing the method. As shown in FIG. 2, the catalytic reactor, generally denoted by the reference number 50, is comprised of housing 52.
  • the housing 52 defines a chamber 54, an entrance 56, and an exit 58.
  • a plurality of conduits 60 each having a first opening 62, a second opening 64, and an exterior surface 66, penetrate the housing 52. The penetration is such that a portion of each conduit 60 is positioned within the chamber 54 with the first opening 62 outside the chamber 54 and the second opening 64 inside the chamber.
  • a catalyst 68 is positioned on a portion of an exterior surface 66 of at least one conduit 60 within the chamber 54 between the first opening 62 and the second opening 64.
  • a mixture, working fluid, with or without starter fuel, 70 enters through the entrance 56 and flows toward the exit 58.
  • the method was employed with a catalytic reactor similar to that depicted in FIG. 2 using methane and oxygen, as a constituent of air, as the working fluid.
  • the catalytic reactor had a platinum catalyst supported on a La-stabilized ⁇ -alumina washcoat.
  • the average flow rate of the working fluid with starter fluid, if present, was about 50 ft/ sec.
  • the working fluid with starter fluid, if present, had an initial temperature of about 200°C.
  • Auxiliary heating of the catalyst was accomplished by preheating the working fluid.
  • the tests were conducted at a pressure of 1 atm. The results are as follows:

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A method to reduce the lightoff temperature of a catalyst. In the method, the working fluid (the fuel and oxidant to be reacted in the presence of the catalyst) is supplemented with a starter fluid at least until the lightoff temperature of the catalyst is reached. Preferably, the amount of starter fuel added is sufficiently small such that a reaction of the starter fuel and oxidant in the presence of the catalyst does not have a sufficient heat release to raise the temperature of the catalyst to the lightoff temperature.

Description

METHOD FOR REDUCING THE
LIGHTOFF TEMPERATURE OF A CATALYST
Field of the Invention The present invention is generally directed to a method for the operation of a catalytic reactor, and, more specifically, to a method for reducing the lightoff temperature of a catalyst within the catalytic reactor.
Background of the Invention Catalytic reactors are well known devices for supporting many chemical reactions, such as exothermic oxidative reactions. However, in order for a catalytic reactor to support an exothermic oxidative reaction at a desired rate, a catalyst, which is in a catalyst bed, in the reactor needs to reach threshold temperature, commonly referred to as lightoff temperature. Upon reaching the lightoff temperature, the chemical reaction proceeds at the desired rate generally at a temperature substantially higher than the lightoff temperature.
Several methods for raising the temperature of the catalyst to the lightoff temperature are known in the art. Common methods of preheating the catalyst to the lightoff temperature include; passing an auxiliary fluid, such as air, that has been heated through the catalytic bed; resistive heating of a substrate on which the catalyst is positioned, e.g. passing an electrical current through the substrate; or preheating with a homogenous flame. The working fluid, e.g., fuel and oxidant in an oxidation reactor, may also be pre-heated to raise the temperature of the catalyst to the lightoff temperature. All these methods require auxiliary systems such as heaters, burners, or electric power sources adding to the cost and complexity of the system.
Efforts to lower the lightoff temperature of a catalyst to minimize the rise in temperature required to lightoff the catalyst have been concentrated on engineering various aspects of the catalyst. One such engineering effort has focused on catalyst structure. For example where the catalyst is positioned on a substrate, high area washcoats have been used in conjunction with the catalyst to increase catalyst surface area and dispersion. While achieving reduced catalyst lightoff temperatures, this technique tends to reduce the durability of the catalyst.
Other methods that do not lowered lightoff temperature can be used to lightoff a catalyst. In one such method, a starter fuel/oxidant mixture is used to raise the temperature of the catalyst to the lightoff temperature. After the lightoff temperature is achieved, the starter fuel/oxidant mixture is gradually replaced with an operational fuel/oxidant mixture. This substitution strategy requires storage of multiple fuel types, storage of significant amounts of a starter fuel, and precise flow control during the switching process to avoid catalyst or catalytic reactor damage.
Based on the foregoing it is the general object of the present invention to overcome or improve upon the problems and drawbacks of the prior art.
Summary of the Invention
A catalyst supports an exothermic reaction between constituents of a working fluid. Based on the working fluid, the catalyst has a baseline lightoff temperature it must achieve before the exothermic reaction proceeds at a desired rate. In the method of the present invention, the working fluid is supplemented with a starter fuel prior to associating the working fluid with the catalyst. The working fluid in association with the starter fluid in the presence of the catalyst defines a supplemented lightoff temperature that is less than the baseline lightoff temperature. As a result, the temperature rise required to lightoff the catalyst is reduced. As an option, the start fuel may be discontinued after the supplemented lightoff temperature is reached.
The precise starter fuel is application dependent. For example, each working fluid, which has fuel and oxidant components, interacts differently with a catalyst, or catalysts, within a catalytic reactor. As a result, the selection of a starter fuel depends on the interaction characteristics of the working fluid, starter fuel and the catalyst(s).
The amount of starter fuel added to the working fluid need not be significant. Preferably, the amount added is not sufficient in and of itself to interact with the catalyst(s) within the catalytic reactor to raise the catalyst(s) to a temperature at or above the lightoff temperature. It, however, is preferred that the starter fuel be more reactive than the fuel, or fuels, within the working fluid as to the catalyst, or catalysts, within the catalytic reactor. Brief Description of the Drawings
FIG. 1. is a graph illustrating the relationship between lightoff temperature and operational temperature of a catalyst.
FIG. 2 depicts a cross-sectional view of a catalytic reactor in which the method disclosed herein might be employed.
Detailed Description of the Invention
In exothermic oxidative reactors, a catalyst therein lights off when the catalyst temperature rises dramatically from an initial catalyst temperature to an operational temperature. FIG. 1 shows this relationship. The auxiliary heating profile, denoted by reference number 10, shows the temperature of the catalyst as a function of the heat applied thereto. As depicted in FIG. 1, the catalyst is heated from, for example, ambient conditions to a lightoff temperature, say Tα. Upon reaching the lightoff temperature Tu the catalyst temperature jumps nearly instantaneously from the lightoff temperature to a considerably higher operational temperature designated A.
In FIG. 1, it has been assumed that the catalyst temperature results directly from the auxiliary heat applied to the catalyst. This assumption is based on the further assumption that if the working fluid is flowing over the catalyst before the catalyst is at the lightoff temperature, the exothermic reactions occurring in the presence of the catalyst are minimal. Thus for all practical purposes, these reactions do not significantly increase the temperature of the catalyst. In the event the exothermic reactions are more than minimal, the catalyst temperature before lightoff will be equal to the sum of the catalyst temperature resulting form the auxiliary heat applied thereto and the temperature rise resulting from the exothermic reactions. Therefore, the auxiliary heating profile 10 will have to be adjusted accordingly.
In the present method, the working fluid is supplemented with a starter fluid. As a result, the lightoff temperature of the catalyst is reduced. Referring to FIG. 1, the baseline lightoff temperature, i.e., the catalyst temperature that is required to lightoff the catalyst if only the working fluid is considered, denoted T is reduced to a supplemented lightoff temperature denoted T2. As a result of the addition of the starter fluid, the auxiliary heating required for the catalyst is similarly reduced. As the operational temperature of the catalyst is a function of lightoff temperature of the catalyst, the operational temperature of the catalyst is reduced from point A to point B when the lightoff temperature is reduced from the baseline lightoff temperature Tj to the supplemented lightoff temperature T2. After lightoff, the temperature increase of the catalyst above the lightoff temperature results from the exothermic reactions between the components of the working fluid. Thus, the operational temperature of the catalyst after lightoff is approximately equal to the sum of lightoff temperature and the temperature rise due to the exothermic reactions. Thus, a reduction in catalyst lightoff temperature equates to a similar reduction in catalyst operational temperature. As a result, points A and B are on a line designated 12 that is generally parallel to the auxiliary heating profile 10.
The amount of starter fuel required is minimal as compared to the amount of fuel in the working fluid. Preferably, the heat release of the starter fuel when reacted with oxidant in the working fluid in the presence of the catalyst is sufficiently low that it is incapable in and of itself of raising the initial catalyst temperature of the catalyst to the baseline lightoff temperature T While the method reduces the lightoff temperature, it is still anticipated that some auxiliary heating of the catalyst may still be required. This auxiliary heating could be by conventional methods known to those skilled in the art. The method of the present invention is shown in conjunction with a fixed geometric catalytic reactor suitable for performing the method. As shown in FIG. 2, the catalytic reactor, generally denoted by the reference number 50, is comprised of housing 52. The housing 52 defines a chamber 54, an entrance 56, and an exit 58. A plurality of conduits 60, each having a first opening 62, a second opening 64, and an exterior surface 66, penetrate the housing 52. The penetration is such that a portion of each conduit 60 is positioned within the chamber 54 with the first opening 62 outside the chamber 54 and the second opening 64 inside the chamber. A catalyst 68 is positioned on a portion of an exterior surface 66 of at least one conduit 60 within the chamber 54 between the first opening 62 and the second opening 64. In this fixed geometry catalytic reactor, a mixture, working fluid, with or without starter fuel, 70 enters through the entrance 56 and flows toward the exit 58. Additional air 72 flows into the entrances 62 of the conduits 60 passing through the conduits and exiting through the conduit exits 64. The mixture 70 contacts the additional oxidant 72 as the additional oxidant exits into the chamber 54. Mixing of the mixture 70 and additional oxidant 72 begins almost immediately. Example 1
The method was employed with a catalytic reactor similar to that depicted in FIG. 2 using methane and oxygen, as a constituent of air, as the working fluid. The catalytic reactor had a platinum catalyst supported on a La-stabilized γ-alumina washcoat. The average flow rate of the working fluid with starter fluid, if present, was about 50 ft/ sec. The working fluid with starter fluid, if present, had an initial temperature of about 200°C. Auxiliary heating of the catalyst was accomplished by preheating the working fluid. The tests were conducted at a pressure of 1 atm. The results are as follows:
Starter Fuel - Propane (LPG)
Fuel/Air Equivalence Ratio* - 3.0 (working fluid plus starter fuel)
*the actual fuel/oxidant ratio divided by the stoichiometric fuel/oxidant ratio based on a com lete combustion reaction.
Figure imgf000007_0001
Starter Fuel - Hydrogen
Fuel/Air Equivalence Ratio - 3.0 (working fluid only)
Figure imgf000007_0002
Starter Fuel - Hydrogen Sulfide
Fuel/ Air Equivalence Ratio - 3.0 (working fluid only)
Figure imgf000007_0003
The before and after temperatures provided under the condition of zero starter fuel indicate the minor hysteresis effects associated with the operation of catalytic reactors. Based on the above data, it is clear that the lightoff temperature for the catalyst was reduced in all cases with a minor addition of a starter fuel to the working fluid.
Example 2
Same conditions as Example 1, except a rhodium catalyst was used instead of a platinum catalyst. The results are as follows:
Starter Fuel - Propane (LPG)
Fuel/ Air Equivalence Ratio - 3.0 (working fluid plus starter fuel)
Figure imgf000008_0001
Starter Fuel - Hydrogen
Fuel/Air Equivalence Ratio - 3.0 (working fluid only)
Figure imgf000008_0002
Starter Fuel - Hydrogen Sulfide
Fuel/Air Equivalence Ratio - 3.0 (working fluid only)
Figure imgf000008_0003
As shown in the data above, H2 reduced the lightoff temperature over a rhodium catalyst, but propane did not. Hydrogen sulfide, on the other hand, increased the lightoff temperature. This illustrates that the starter fuel is dependent upon the catalyst.
Although the present invention has been described in considerable detail with reference to certain preferred versions thereof, other versions are possible. Therefore, the spirit and scope of the invention should not be limited to the description of the preferred versions contained herein.

Claims

What we claim is:
1. A method for reducing a baseline lightoff temperature of a catalyst intended to support an exothermic reaction between constituents of a working fluid, the method comprising the steps of: supplementing the working fluid with a starter fuel prior to associating the working fluid with the catalyst, the working fluid in association with the starter fluid in the presence of the catalyst defining a supplemented lightoff temperature less than the baseline lightoff temperature.
2. The method of claim 1 wherein the working fluid comprises fuel and oxidant in fuel rich proportions.
3. The method of claim 1 wherein the working fluid comprises fuel and oxidant, and the catalyst in cooperation with the starter fuel and oxidant is capable of generating a heat of reaction, the heat of reaction being insufficient to raise the catalyst to the baseline lightoff temperature.
4. The method of claim 1 including the further step of discontinuing the starter fuel after the catalyst lights off.
5. The method of claim 1 wherein the working fluid comprises fuel and oxidant and the fuel has a reactivity, and the starter fuel has a reactivity, and the working fluid fuel reactivity is less than the starter fuel reactivity.
PCT/US2003/036983 2002-11-21 2003-11-19 Method for reducing the lightoff temperature of a catalyst WO2004047973A2 (en)

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US7976594B2 (en) 2003-07-31 2011-07-12 Precision Combustion, Inc. Method and system for vaporization of liquid fuels

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5867982A (en) * 1995-06-02 1999-02-09 Tengblad; Roger System for reducing emissions in catalytic converter exhaust systems
US6272849B1 (en) * 2000-01-13 2001-08-14 Ford Global Technologies, Inc. Apparatus and method for heating an automotive catalyst to an emission reactive condition

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5867982A (en) * 1995-06-02 1999-02-09 Tengblad; Roger System for reducing emissions in catalytic converter exhaust systems
US6272849B1 (en) * 2000-01-13 2001-08-14 Ford Global Technologies, Inc. Apparatus and method for heating an automotive catalyst to an emission reactive condition

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US20040098969A1 (en) 2004-05-27
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