KR20190118681A - Gradual oxidation with heat transfer - Google Patents

Abstract

Embodiments of systems and methods for oxidizing a gas are described herein. In some embodiments, the reaction chamber is structured to receive flue gas and maintain the gas at a temperature in the reaction chamber that is above the autoignition temperature of the gas. In addition, the reaction chamber is structured to maintain the reaction temperature in the reaction chamber below the combustion stop temperature. In some embodiments, heat and product gases from the oxidation process are used to drive a turbine, reciprocating engine, for example, and injected back into the reaction chamber.

Description

Gradual oxidation with heat transfer {GRADUAL OXIDATION WITH HEAT TRANSFER}

The present invention relates to gradual oxidation with heat transfer.

In some industrial processes, such as power generation, steam generation and thermally driven chemical treatment, heat is provided directly or indirectly by combustion of high-energy-content (HEC) fuels such as propane or natural gas. Can be.

Emissions from landfill and other sources of gases containing volatile organic compounds (VOCs) are considered contaminants. These waste streams often contain little fuel and thus do not sustain combustion on their own. Some of the methods for disposing of VOC-containing waste streams use the following types of thermal oxidizers: (1) fired- or supplemental fired-thermal oxidizers, (2) Catalytic thermal oxidizer, (3) oxidizer with heat recovery, and (4) Regenerative thermal oxidizer (RTO).

The fired- or supplemental fired-thermal oxidizer may comprise a burner, a retention chamber, a mixing chamber and an exhaust stack. 1 aa, an air-fuel mixture 6 is provided to the burner 2 to produce continuous combustion, waste stream 7 is introduced into the combustion and hot gases are introduced to the mixing chamber 3 and the retention chamber 4. Illustrates a batch structure that continuously oxidizes as it passes. If the waste stream 7 is within flammability limits, it can be burned directly in the burner 2 instead of the air-fuel mixture 6. The mixing chamber 3 is required to be supplied with waste streams and burners separately. The retention chamber 4 provides enough time to complete the oxidative chemical reactions. The exhaust vessel 5 carries the products of oxidation to the atmosphere.

Catalytic oxidizers avoid the production of thermal NOx by keeping the oxidation reaction temperature low, as shown in FIG. 1ab. Waste stream 7 containing VOCs is provided in a catalytic reaction chamber 8 having a large inner surface area coated with a catalyst. Catalytic materials include rare metals such as platinum, palladium and iridium, as well as certain VOCs, copper oxides, vanadium and cobalt. The concentration of VOCs in the waste stream 7 should be low enough that the reaction temperature does not exceed the catalyst maximum service temperature. Waste stream 7 typically must be heated to a specific temperature range suitable for catalytic reactivity.

The use of a recuperator can reduce the operating costs of fired thermal oxidizers and catalytic oxidizers, as shown in FIG. 1A. Exhaust from the reaction chamber 1 which may be present by the example of the system of FIG. 1aa or FIG. When supplied, it is fed to a high temperature recuperator 9 to heat a separate combustion air-fuel mixture. The use of the recuperator 9 can reduce or eliminate the need for supplemental fuel to heat the reactants to their oxidation temperature.

Finally, RTO can be used to oxidize VOC. In RTO, heat is stored on an intermediate heat sink material, typically a ceramic solid, for recovery during alternate cycles. The cycle uses heat from the preheated flow to preheat the VOC-loaded waste stream to a higher temperature. If the temperature is high enough, oxidation will occur due to autoignition, as discussed in more detail later in the present disclosure. If the temperature is not high enough, supplemental ignition from other fuel and air sources may be required. The higher temperature exhaust is then sent through the cooler heat sink to capture energy.

There are several approaches to achieving cycling of heat exchange materials. 1ad illustrates a system using two regenerative oxidizers. In the arrangement pointed out, the waste stream 7 is introduced into the first high temperature regenerative oxidizer. The waste stream is heated as it passes through the first regenerative oxidizer, thereby incrementally cooling the heat sink material with the first oxidizer starting at the inlet. After the waste stream 7 self-ignites, the hot exhaust gas is withdrawn from the first oxidizer and provided to the inlet of the second oxidizer, thereby saving the stored thermal energy in the heat sink material in the second oxidizer. Play ". The oxidized waste stream cools as it passes through the second oxidizer. If the second oxidizer is sufficiently heated, the system is restructured such that the flow from the waste stream 7 is provided at the inlet of the second oxidizer and the exhaust from the second oxidizer is provided at the inlet of the first oxidizer. do. The process circulates between the two arrangements such that the precooled oxidizer is heated while heating the waste stream 7 and vice versa. Some RTO designs allow the use of rotating hardware to vary the flow streams between cycles or to move regenerative oxidizers between cycles. Another approach is to use a single regenerative oxidizer, but to reverse the flow direction for each cycle. One end of the oxidizer is preheated while the other end captures heat after the oxidative reaction. The reversal of the flow direction is necessary because the end of the oxidizer close to the inlet cools to the point where it can no longer heat the inlet waste stream 7 to the temperature at which it starts the reaction.

U.S. Patent Application 13 / 289,996 U.S. Patent Application 13 / 289,989 U.S. Patent Application 13 / 048,796 U.S. Patent Application 13 / 115,910 U.S. Patent Application 13 / 115,902

In some circumstances, it is advantageous to dispose of methane released from low energy-content (LEC) fuels such as some landfills while minimizing unwanted components such as carbon monoxide (CO) and NOx in the exhaust. In other circumstances, it is desirable to provide heat from HEC fuels, such as propane, to drive or power industrial processes without producing these same unwanted components. In order to achieve these operations, air-fuel mixtures formed from one or both of LEC and HEC fuels maintain the maximum temperature of the air-fuel mixture below the temperature at which thermal NOx forms, while the VOCs and hydrocarbons in the fuels CO ₂ ) and water (H ₂ O) must be reached at a temperature high enough. Any conventional open-flame combustion process is a candidate group that is replaced by a process that reduces the formation of NOx compounds through a reduced pressure oxidation process.

It is also desirable to utilize energy otherwise discarded when LEC fuel is disposed of by simply oxidizing it to convert VOCs to CO ₂ and H ₂ O. One of the disadvantages of existing power-generating systems driven by gas turbines is that the HEC fuel is burned to provide heat to drive the turbine. This would essentially benefit from using "free" LEC fuel to provide this heat and to avoid or reduce the cost of purchasing the fuel.

The processes described above in FIGS. 1A-1AD have various disadvantages. For the thermal oxidizer of FIG. 1 aa, for example, if a supplemental fuel is required to provide the air-fuel mixture 6, the cost of the fuel is added to the cost of the process. In addition, the reaction temperatures at burner 2 are high enough to form thermal NOx, which is discussed in more detail later in the present disclosure.

Catalysts can have challenges associated with their use. Precious metal catalysts are rare and expensive. In a process, the waste stream is required to be heated to a certain range using any of a variety of means including heat recovery, as described below, and often adds to the cost of the process. The catalyst may be chemically inert due to processes such as sintering, fouling or volatilization. Waste fuels, such as landfill gas, often contain contaminants that can significantly shorten the life of the catalyst. In order to control the reaction temperature to avoid volatilization, fuel composition and process variables are maintained within pre-limited limits, which adds cost to monitor and adjust these variables.

Recuperators have some disadvantages. Recuperators are an additional investment in thermal oxidation systems. The recuperator also adds a pressure drop to the system, which increases the power requirements for the flow conveying device, ie the fan, which moves the waste stream 7 and the air-fuel mixture 6 through the system. . If the recuperators contain small passages, they can be contaminated and corroded from various exhaust gas components. If the temperature of the exhaust gas from the reaction chamber is above the maximum service temperature for the material of the recuperator, additional process equipment is required to cool and exhaust the exhaust before introducing it into the recuperator.

Regenerative oxidizers have the disadvantage that the repositioning of the flow path between cycles requires significant complexity in hot valve actuation and pipe actuation or in physically moving the hot regenerative oxidizers. The relocation structure also stops the process, which requires some system to accumulate waste stream 7 during the relocation structure operation.

The gradual oxidation (GO) process disclosed herein avoids the drawbacks associated with conventional systems for treating waste streams containing VOCs. The GO process runs LEC fuel once through a start-up process and does not require additional HEC fuel to continue the oxidation process. The GO process does not require the use of expensive catalysts, which reduces the required investment and avoids the operational risk of toxicization of the catalyst. The disclosed GO process transfers heat generated by oxidation of the waste stream into the inlet flow, thereby avoiding the problem of incrementally cooling the medium as observed in regenerative oxidizers, and requiring expensive and potentially unwanted valves. Not only is eliminated, but the regeneration system is restructured between cycles, eliminating the need for an accumulator to handle the incoming waste stream.

In addition, there are circumstances that require the use of HEC fuel while minimizing the formation of unwanted NOx compounds and CO as well as reducing unburned hydrocarbons in the exhaust. One of the drawbacks of existing power-generating systems driven by gas turbines using HEC fuel is that some levels of residual hydrocarbons, where NOx can be formed, and the mixture falls below the lower flammability limit during the combustion process. The combustion process takes place at a temperature that may be present.

The disclosed systems use GO processes that occur in oxidizers (also referred to herein as gradual oxidizers, GO chambers and GO reaction chambers) instead of conventional combustion chambers to generate heat to drive the system. In certain arrangements, the oxidizer contains a material such as a ceramic, which is structured to be porous to gas flow and maintains its structure at temperatures above 1200 ° F.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber having a reaction chamber structured to receive a gas comprising an oxidizable fuel through the inlet. An oxidizer structured to maintain gradual oxidation of the fuel in the reaction chamber; And for attracting heat from the reaction chamber such that the adiabatic reaction temperature in the reaction chamber is close to the flameout temperature and heat is withdrawn from the reaction chamber to reduce the actual temperature in the reaction chamber to a temperature that does not exceed the burnout temperature. Means;

In certain embodiments, the means for attracting heat from the reaction chamber comprises a heat exchanger. In certain embodiments, the means for attracting heat from the reaction chamber comprises a fluid. In certain embodiments, the means for attracting heat from the reaction chamber includes means for generating steam. In certain embodiments, the means for attracting heat is configured to attract heat from the reaction chamber when the actual temperature in the reaction chamber increases to the stoppage temperature. In certain embodiments, the system further comprises means for raising the temperature of the gas above the autoignition temperature of the fuel at the inlet of the reaction chamber. In certain embodiments, the means comprises a heat exchanger in the oxidizer. In certain embodiments, the reaction chamber is structured to maintain gradual oxidation of the oxidizable fuel without a catalyst. In certain embodiments, the means is configured to attract heat from the reaction chamber when the temperature in the reaction chamber exceeds 2300 ° F. In certain embodiments, the system further includes a turbine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber having a reaction chamber structured to receive a gas comprising an oxidizable fuel through the inlet. An oxidizer structured to maintain a gradual oxidation process in the reaction chamber; And a heat exchanger configured to attract heat from the reaction chamber such that when the adiabatic reaction temperature in the reaction chamber approaches the burnout temperature, the actual temperature in the reaction chamber is reduced to a level not exceeding the burnout temperature.

In certain embodiments, the heat exchanger is configured to attract heat from the reaction chamber when the actual temperature in the reaction chamber increases to the stoppage temperature. In certain embodiments, the system further includes a turbine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the heat exchanger is configured to raise the temperature of the gas above the autoignition temperature of the fuel, at the inlet of the reaction chamber. In certain embodiments, the heat exchanger comprises a fluid introduced into the reaction chamber. In certain embodiments, the heat exchanger is configured to evacuate the fluid from the reaction chamber. In certain embodiments, the heat exchanger comprises means for generating steam. In certain embodiments, the reaction chamber is structured to maintain gradual oxidation of the oxidizable fuel without a catalyst. In certain embodiments, the heat exchanger is configured to attract heat from the reaction chamber when the temperature in the reaction chamber exceeds 2300 ° F. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing fuel described herein is an oxidizer having a reaction chamber having an inlet and an outlet, the oxidizer having a reaction chamber structured to maintain a gradual oxidation process of fuel in the reaction chamber. Receiving a gas within the oxidizable fuel; And if the adiabatic reaction temperature in the reaction chamber approaches the burnout temperature, drawing heat from the reaction chamber so that the actual temperature in the reaction chamber does not exceed the burnout temperature.

In certain embodiments, the method further comprises expanding the gas from the reaction chamber in the turbine. In certain embodiments, the method further comprises compressing the fuel with a compressor before introducing the fuel mixture into the reaction chamber. In certain embodiments, the method includes attracting heat from the reaction chamber comprises introducing a fluid into the reaction chamber. In certain embodiments, the method further comprises draining the fluid from the reaction chamber. In certain embodiments, the fluid is withdrawn from the reaction chamber in the form of steam. In certain embodiments, the reaction chamber maintains gradual oxidation of the oxidizable fuel without a catalyst. In certain embodiments, when the temperature in the reaction chamber exceeds 2300 ° F., heat is drawn from the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing fuel described herein is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction being structured to maintain a temperature in the reaction chamber to gradually oxidize the fuel in the reaction chamber. Receiving a gas containing an oxidizable fuel in an oxidizer having a chamber; And reducing the temperature in the reaction chamber such that the actual temperature in the reaction chamber remains below the burnout temperature.

In certain embodiments, the method includes reducing the temperature attracting heat from the reaction chamber. In certain embodiments, the method further includes expanding the gas from the reaction chamber in the turbine. In certain embodiments, the method further comprises compressing the fuel with a compressor before introducing the fuel mixture into the reaction chamber. In certain embodiments, the method includes introducing a fluid into the reaction chamber to reduce the temperature. In certain embodiments, the method further comprises draining the fluid from the reaction chamber. In certain embodiments, the method drains the fluid from the reaction chamber in the form of steam. In certain embodiments, the reaction chamber maintains gradual oxidation of the oxidizable fuel without a catalyst. In certain embodiments, the method reduces the temperature so that the temperature in the reaction chamber does not exceed 2300 ° F. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel described herein includes determining a temperature in a reaction chamber of an oxidizer having an inlet and an outlet and structured to maintain gradual oxidation of the oxidizable fuel; And outputting a signal to decrease the temperature in the reaction chamber so that when the temperature in the reaction chamber approaches the burnout temperature, the temperature remains below the burnout temperature.

In certain embodiments, the signal includes instructions to attract heat from the reaction chamber by introducing a liquid into the reaction chamber. In certain embodiments, the signal includes instructions to drain the fluid from the reaction chamber. In certain embodiments, the instructions to drain the fluid from the reaction chamber include instructions to drain the fluid in the form of steam. In certain embodiments, a signal that attracts heat from the reaction chamber is output when the temperature in the reaction chamber exceeds 2300 ° F. In certain embodiments, the temperature is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso-phen When approaching the burnout temperature of at least one of tainne, n-pentane, acetylene, hexane and carbon monoxide, a signal is drawn to attract heat from the reaction chamber.

In certain embodiments, a method for oxidizing a fuel described herein includes determining a temperature in a reaction chamber of an oxidizer having an inlet and an outlet and structured to maintain gradual oxidation of the oxidizable fuel; And outputting a signal to the heat exchanger to attract heat from the reaction chamber when the temperature in the reaction chamber is close to the combustion stop temperature.

In certain embodiments, the signal includes instructions for removing heat from the reaction chamber. In certain embodiments, the signal includes instructions to reduce the temperature by introducing a fluid into the reaction chamber. In certain embodiments, the signal includes instructions to drain the fluid from the reaction chamber. In certain embodiments, the instructions for evacuating the fluid from the reaction chamber include evacuating the fluid in the form of steam. In certain embodiments, further comprising repeatedly calculating the adiabatic reaction temperature in the reaction chamber based on the data of the oxidizable fuel. In certain embodiments, a signal that decreases the temperature in the reaction chamber is output when the temperature in the reaction chamber exceeds 2300 ° F. In certain embodiments, the temperature is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso-phen When approaching the burnout temperature of at least one of tainne, n-pentane, acetylene, hexane and carbon monoxide, a signal is drawn to attract heat from the reaction chamber. In certain embodiments, when the temperature increases to the burnout temperature, a signal is drawn that attracts heat from the reaction chamber.

In certain embodiments, a method for oxidizing a fuel described herein includes determining a temperature in a reaction chamber of an oxidizer having an inlet and an outlet and structured to maintain gradual oxidation of the oxidizable fuel; And determining, by the sensor, when the temperature in the reaction chamber is close to the combustion stop temperature of the fuel in the reaction chamber.

In certain embodiments, the method includes outputting a signal to reduce the temperature in the reaction chamber when the calculated adiabatic reaction temperature in the reaction chamber exceeds the burnout temperature. In certain embodiments, the calculated adiabatic reaction temperature is based on oxidizable fuel and oxidant in the reaction chamber. In certain embodiments, the signal includes instructions for removing heat from the reaction chamber. In certain embodiments, the signal includes instructions to reduce the temperature by introducing a liquid into the reaction chamber. In certain embodiments, a signal that decreases the temperature in the reaction chamber is output when the temperature in the reaction chamber exceeds 2300 ° F. In certain embodiments, the temperature is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso-phen If the burnout temperature of at least one of tain, n-pentane, acetylene, hexane and carbon monoxide is exceeded, a signal is drawn to attract heat from the reaction chamber.

In certain embodiments, a system for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber having a reaction chamber configured to receive a gas comprising an oxidizable fuel through the inlet. An oxidizer structured to maintain the oxidation process without a catalyst; A detection module for detecting when the reaction temperature in the reaction chamber is close to the combustion stop temperature of the fuel in the reaction chamber or when the reaction chamber inlet temperature is close to the autoignition threshold; And a correction module, based on the detection module, for outputting instructions for changing at least one of the removal of heat from the reaction chamber or the inlet temperature of the reaction chamber, wherein the correction module burns down the actual temperature in the reaction chamber. It is structured for at least one of maintaining below the temperature and maintaining the inlet temperature above the autoignition threshold of the fuel.

In certain embodiments, the calibration module outputs instructions for removing heat from the reaction chamber by a heat exchanger. In certain embodiments, the calibration module outputs instructions for removing heat from the reaction chamber by the fluid. In certain embodiments, the calibration module outputs instructions for raising the inlet temperature. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is structured to maintain oxidation of the oxidizable fuel below the shutdown temperature. In certain embodiments, when the temperature in the reaction chamber exceeds 2300 ° F., the calibration module outputs instructions to remove heat from the reaction chamber. In certain embodiments, the turbine receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a system for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber having a reaction chamber configured to receive a gas comprising an oxidizable fuel through the inlet. An oxidizer structured to maintain the oxidation process without a catalyst; A detection module for detecting when the reaction temperature in the reaction chamber is close to the combustion stop temperature of the fuel in the reaction chamber or when the reaction chamber inlet temperature is close to the autoignition threshold; And based on the detection module, a calibration module that outputs instructions for at least one of maintaining an actual temperature within the reaction chamber below the combustion stop temperature, or maintaining an inlet temperature above the fuel's self-ignition threshold. Include.

In certain embodiments, the calibration module outputs instructions to the heat exchanger to remove heat from the reaction chamber. In certain embodiments, the calibration module outputs instructions for removing heat from the reaction chamber by the fluid. In certain embodiments, the calibration module outputs instructions for raising the inlet temperature. In certain embodiments, the system further comprises a heat exchanger disposed within the reaction chamber. In certain embodiments, the reaction chamber is structured to maintain oxidation of the oxidizable fuel below the shutdown temperature. In certain embodiments, when the temperature in the reaction chamber exceeds 2300 ° F., the calibration module outputs instructions to remove heat from the reaction chamber.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber having a reaction chamber structured to receive a gas comprising an oxidizable fuel through the inlet. An oxidizer structured to maintain an oxidation process without a catalyst; And a processor for detecting a case where the reaction temperature in the reaction chamber is close to the combustion stop temperature of the fuel in the reaction chamber and the case where the reaction chamber inlet temperature falls to the self-ignition threshold.

In certain embodiments, based on the processor, the calibration module reduces the actual temperature in the reaction chamber to remain below the burnout temperature of the fuel by removing heat from the reaction chamber. In certain embodiments, the calibration module, based on the processor, raises the inlet temperature above the fuel's self-ignition threshold by increasing the residence time of the oxidizable fuel in the reaction chamber.

In certain embodiments, a method for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, in an oxidizer having a reaction chamber structured to maintain an oxidation process of a gas. Receiving a gas comprising fuel; And if at least one of the actual temperature in the reaction chamber approaches or increases to or near the combustion stop temperature of the fuel, and the reaction chamber inlet temperature approaches or falls below the autoignition threshold of the fuel. Changing at least one of the removal of heat from the chamber and the inlet temperature of the reaction chamber.

In certain embodiments, the actual temperature of the reaction chamber is maintained below the stoppage temperature. In certain embodiments, the inlet temperature of the reaction chamber is increased to a level that supports oxidation of the fuel without a catalyst. In certain embodiments, the inlet temperature is increased above the autoignition threshold. In certain embodiments, the temperature of the gas is increased by a heat exchanger disposed in the reaction chamber. In certain embodiments, the method further comprises expanding gas from the reaction chamber outlet in the turbine or piston engine. In certain embodiments, the method further comprises compressing the fuel with a compressor before introducing the fuel mixture into the reaction chamber. In certain embodiments, removal of heat from the reaction chamber includes introducing a liquid into the reaction chamber. In certain embodiments, the method further comprises draining the liquid from the reaction chamber. In certain embodiments, the liquid exits the reaction chamber in the form of steam. In certain embodiments, the reaction chamber maintains gradual oxidation of the oxidizable fuel without a catalyst. In certain embodiments, when the temperature in the reaction chamber exceeds 2300 ° F., heat is removed from the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, in an oxidizer having a reaction chamber structured to maintain a gradual oxidation process. Receiving a gas comprising; And removal of heat from the reaction chamber when the adiabatic reaction temperature in the reaction chamber is close to the combustion stop temperature of the fuel; And increasing at least one of the inlet temperature of the reaction chamber when the reaction chamber inlet temperature falls below the autoignition threshold of the fuel.

In certain embodiments, the actual temperature of the reaction chamber is maintained below the stoppage temperature. In certain embodiments, the inlet temperature of the reaction chamber is increased to a level that supports oxidation of the fuel without a catalyst. In certain embodiments, the inlet temperature is increased above the autoignition threshold. In certain embodiments, the gas temperature is increased by a heat exchanger disposed outside the reaction chamber, and the gas passes through the heat exchanger before introducing into the reaction chamber.

In certain embodiments, a method for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, in an oxidizer having a reaction chamber structured to maintain a gradual oxidation process without a catalyst. Receiving a gas comprising a possible fuel; And removal of heat from the reaction chamber such that when the reaction temperature in the reaction chamber is close to the burnout temperature of the fuel, the actual temperature of the reaction chamber is maintained below the burnout temperature; And when the reaction chamber inlet temperature falls below the autoignition threshold of the fuel, increasing at least one of the inlet temperatures of the reaction chamber such that the inlet temperature of the reaction chamber is maintained above a level that supports oxidation of the fuel without catalyst. Include. In certain embodiments, the inlet temperature is maintained above the autoignition temperature.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the gas containing the oxidizable fuel through the inlet and the oxidation process within the reaction chamber. An oxidizer having a reaction chamber structured to hold; A detection module for detecting the case where the reaction chamber inlet temperature of the gas falls below or below the autoignition threshold of the gas entering the first reaction chamber; And based on the detection module, a calibration module that outputs instructions to vary the inlet temperature of the reaction chamber to maintain the inlet temperature above the autoignition threshold, such that the gas in the reaction chamber is oxidized without catalyst.

In certain embodiments, the calibration module outputs instructions to the heat exchanger to raise the inlet temperature. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is configured to maintain oxidation of the gas below the stoppage temperature of the fuel in the reaction chamber. In certain embodiments, the system further includes a turbine or piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the gas containing the oxidizable fuel through the inlet and the oxidation process within the reaction chamber. An oxidizer having a reaction chamber structured to hold; A detection module for detecting the case where the reaction chamber inlet temperature of the gas falls toward the autoignition threshold of the fuel; And a calibration module based on the detection module to maintain the inlet temperature above the autoignition threshold.

In certain embodiments, the calibration module outputs instructions to the heat exchanger to maintain the inlet temperature. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is configured to maintain the actual temperature within the reaction chamber below the stoppage temperature of the fuel. In certain embodiments, the system further includes a turbine or piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the gas into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a system for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the structure being configured to receive a gas comprising an oxidizable fuel through the inlet and maintain an oxidation process An oxidizer having a reaction chamber; And a heat exchanger that maintains the reaction chamber inlet temperature above the fuel's autoignition threshold, such that the fuel oxidizes above the autoignition threshold and below the fuel's burnout temperature in the reaction chamber.

In certain embodiments, the detection module detects when the reaction chamber inlet temperature is close to the autoignition threshold. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the system further includes a turbine or piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, in a reaction chamber structured to maintain an oxidation process of an oxidizable fuel. Determining at least one of an actual reaction temperature of the reaction chamber and an inlet temperature of the reaction chamber; Determining by the sensor at least one of an actual reaction temperature approaching or exceeding a fuel stop temperature of the fuel and an inlet temperature approaching or falling below the autoignition threshold of the fuel; And determining at least one of a decrease in the actual reaction temperature in the reaction chamber to remain below the burnout temperature and an increase in the inlet temperature to maintain the inlet temperature above the autoignition threshold.

In certain embodiments, the reduction in the actual reaction temperature includes the removal of heat from the reaction chamber. In certain embodiments, the removal of heat from the reaction chamber includes introducing a fluid into the reaction chamber. In certain embodiments, removing heat further comprises draining the fluid from the reaction chamber. In certain embodiments, the reaction chamber is structured to drain the fluid in the form of steam. In certain embodiments, the increase in inlet temperature comprises adding fuel through a heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the burnout temperature is about 2300 ° F. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, in a reaction chamber structured to maintain an oxidation process of an oxidizable fuel. Determining at least one of an actual reaction temperature of the reaction chamber and an inlet temperature of the reaction chamber; Determining at least one of an actual reaction temperature approaching or exceeding a fuel stop temperature of the fuel and a reaction chamber inlet temperature approaching or falling below the autoignition threshold of the fuel; And outputting instructions of at least one of reducing the actual temperature or reducing the increase in the actual temperature in the reaction chamber to remain below the burnout temperature and increasing the inlet temperature above the fuel's self-ignition threshold. It includes.

In certain embodiments, the output includes instructions to remove heat from the reaction chamber. In certain embodiments, the method further includes removing heat from the reaction chamber by introducing a fluid into the reaction chamber. In certain embodiments, removing heat further comprises draining the fluid from the reaction chamber. In certain embodiments, the fluid exits the reaction chamber in the form of steam. In certain embodiments, the output includes increasing the inlet temperature by applying fuel through a heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the burnout temperature is about 2300 ° F. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing fuel described herein includes an oxidizer having a reaction chamber having an inlet and an outlet, wherein the oxidizable fuel is contained within an oxidizer having a reaction chamber structured to maintain an oxidation process. Receiving a gas comprising; And if the reaction chamber inlet temperature of the gas approaches or drops below the autoignition threshold of the fuel, the inlet temperature remains above the autoignition threshold and the reaction chamber maintains oxidation of the fuel in the reaction chamber without catalyst, Introducing additional heat into the gas.

In certain embodiments, additional heat is introduced by the heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber maintains oxidation of the oxidizable fuel below the stoppage temperature of the fuel. In certain embodiments, the method further includes a turbine or piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the compressor receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, includes an oxidizer having a reaction chamber having an inlet and an outlet, in an oxidizer having a first reaction chamber configured to maintain an oxidation process of the fuel, Receiving a gas comprising an oxidizable fuel; And when the reaction chamber inlet temperature of the gas approaches or falls below the autoignition threshold of the fuel, increasing the inlet temperature to a level above the autoignition threshold.

In certain embodiments, the reaction chamber maintains gradual oxidation of the fuel in the reaction chamber without catalyst. In certain embodiments, the inlet temperature is increased by the heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is configured to maintain oxidation of the fuel below the stoppage temperature of the fuel. In certain embodiments, the method further comprises a turbine or piston engine receiving gas from the reaction chamber and expanding the gas. In certain embodiments, the method further includes the step of a compressor to receive and compress the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel described herein includes an inlet temperature of a gas comprising an oxidizable fuel at the inlet in the reaction chamber having an inlet and an outlet and configured to maintain the oxidation process. Determining when to approach or fall below an ignition threshold; And outputting a signal that increases the inlet temperature of the gas such that the inlet temperature remains above the autoignition threshold.

In certain embodiments, the signal includes instructions for heating the gas with a heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is configured to maintain oxidation of the fuel below the stoppage temperature of the fuel. In certain embodiments, the reaction chamber is structured to maintain oxidation of the fuel below about 2300 ° F. In certain embodiments, the method further comprises a turbine or piston engine receiving gas from the reaction chamber and expanding the gas. In certain embodiments, the method further includes the step of a compressor to receive and compress the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing fuel described herein is an oxidizer having a reaction chamber having an inlet and an outlet, in an oxidizer having a reaction chamber structured to maintain gradual oxidation of the fuel without a catalyst, CLAIMS 1. A method of oxidizing fuel in a system containing a gas comprising an oxidizable fuel, the method comprising: detecting when the reaction chamber inlet temperature of the gas approaches or falls below the autoignition threshold of the gas; And outputting instructions for increasing the inlet temperature such that the gas inlet temperature remains above the autoignition temperature while the temperature in the reaction chamber remains below the burnout temperature.

In certain embodiments, the instructions increase the heat transfer to the gas by a heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is configured to maintain oxidation of the fuel below the stoppage temperature of the fuel. In certain embodiments, the reaction chamber is structured to maintain oxidation of the fuel at less than about 2300 ° F. In certain embodiments, the method further comprises a turbine or piston engine receiving gas from the reaction chamber and expanding the gas. In certain embodiments, the method further comprises the step of a compressor to receive and compress the gas comprising the fuel mixture prior to introducing the gas into the reaction chamber.

In certain embodiments, a method for oxidizing a fuel, as described herein, includes an inlet temperature of a gas comprising an oxidizable fuel at the inlet in a reaction chamber having an inlet and an outlet and configured to maintain an oxidation process. Determining with the sensor a case of approaching an ignition threshold, wherein the actual temperature in the reaction chamber is maintained at a level below the burnout temperature and above the autoignition threshold so that gradual oxidation of the fuel is maintained in the reaction chamber.

In certain embodiments, the signal increases the inlet temperature of the gas to remain above the autoignition threshold. In certain embodiments, the signal includes instructions for increasing heat transfer to the gas by a heat exchanger. In certain embodiments, the heat exchanger is disposed in the reaction chamber.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the gas containing the oxidizable fuel through the inlet and maintaining the oxidation process of the gas. An oxidizer having a reaction chamber that is structured to be; And a heat exchange medium disposed within the reaction chamber, the heat exchange medium being structured to maintain the internal temperature of the reaction chamber below the burnout temperature and to maintain the reaction chamber inlet temperature of the fuel above the autoignition temperature of the fuel. Circulates in the furnace, which attracts heat from the reaction chamber, keeping the internal temperature below the burnout temperature.

In certain embodiments, the circulation of the medium is structured to heat the gas at the inlet and maintain the inlet temperature of the fuel above the autoignition temperature. In certain embodiments, the circulation of the medium is structured to attract heat from the gas in the reaction chamber to maintain the internal temperature of the gas below the stoppage temperature of the gas. In certain embodiments, the medium comprises a number of steel structures circulated through the reaction chamber. In certain embodiments, the medium comprises a fluid circulated through the reaction chamber. In certain embodiments, the rate at which the medium circulates is based on at least one of an internal temperature and an inlet temperature. In certain embodiments, heat is drawn from the medium when the medium circulates outside the reaction chamber.

In certain embodiments, a system for oxidizing a fuel described herein is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber being structured to receive a gas comprising an oxidizable fuel through the inlet, The oxidizer may be an oxidizer structured to maintain an oxidation process of a gas in the reaction chamber; And a recirculation path that directs at least a portion of the product gas towards the inlet of the reaction chamber after oxidation in the reaction chamber and introduces the product gas into the reaction chamber at the inlet, the introduction of the product gas comprising the autoignition temperature of the gas. Increase in excess.

In certain embodiments, recycling of the product gas reduces the oxygen content level in the reaction chamber. In certain embodiments, the amount of product gas recycled is based on the inlet temperature. In certain embodiments, the amount of product gas recycled is based on the internal temperature of the reaction chamber.

In certain embodiments, a system for oxidizing a fuel described herein is an oxidizer having a reaction chamber having an inlet and an outlet, the reaction chamber being structured to receive a gas comprising an oxidizable fuel through the inlet, The oxidizer may be an oxidizer structured to maintain an oxidation process of a gas in the reaction chamber; And a heat exchange medium disposed in the reaction chamber, the heat exchange medium being structured to maintain the internal temperature of the reaction chamber below the burnout temperature and the reaction chamber inlet temperature of the fuel above the autoignition temperature of the fuel.

In certain embodiments, the heat exchange medium comprises a fluid. In certain embodiments, the fluid is circulated and the circulation of the medium is structured to heat the gas at the inlet and maintain the inlet temperature of the gas above the autoignition temperature of the gas. In certain embodiments, the heat exchange medium comprises sand. In certain embodiments, the heat exchange medium comprises a plurality of uniformly stacked structures. In certain embodiments, the heat exchange medium comprises a plurality of stacked disks, each having a plurality of perforations in which gas is allowed to flow. In certain embodiments, the heat exchange medium is configured to conduct heat in the reaction chamber towards the inlet, whereby the gas received through the inlet is heated above the autoignition temperature.

In certain embodiments, the split cycle reciprocating engine described herein includes an intake containing an air-fuel mixture comprising a mixture of air and gaseous fuel; A compression chamber, coupled to the reciprocating engine, for compressing the mixture in the reciprocating piston chamber; An oxidation chamber configured to receive the mixture from the compression chamber through the first inlet and maintain oxidation of the mixture at an internal temperature below the stoppage temperature of the mixture and sufficient to oxidize the mixture without a catalyst; And an expansion chamber that receives the oxidizing product gas from the oxidation chamber and expands the product gas in the expansion chamber through the reciprocating piston.

In certain embodiments, the oxidation chamber is structured to maintain the inlet temperature of the mixture above the autoignition temperature of the mixture. In certain embodiments, the system further includes a heat exchanger configured to draw heat from the product gas and heat the mixture prior to introducing the mixture into the oxidation chamber. In certain embodiments, the heat exchanger comprises a tube-in-tube heat exchanger. In certain embodiments, the system further comprises a heat exchange medium disposed in the oxidation chamber. In certain embodiments, the medium is configured to maintain the internal temperature of the oxidation chamber below the burnout temperature by conducting heat towards the inlet of the oxidation chamber, where the medium is introduced into the mixture introduced into the oxidation chamber. By cooling. In certain embodiments, the fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso-phen At least one of ethane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a split cycle reciprocating engine described herein includes a reciprocating cycle comprising at least one compression chamber having a reciprocating piston therein and at least one expansion chamber having a reciprocating piston therein; And an intake containing an air-fuel mixture comprising a mixture of air and gaseous fuel, the intake configured to apply the mixture to a compression chamber; A heating cycle comprising a reaction chamber configured to receive the mixture from the compression chamber and maintain the oxidation of the mixture at an internal reaction chamber temperature sufficient to oxidize the mixture without the catalyst, wherein the expansion chamber includes an oxidation product gas from the reaction chamber. And is configured to expand the product gas in the expansion chamber through the reciprocating piston.

In certain embodiments, the reaction chamber comprises an inlet and the reaction chamber is configured to maintain the inlet temperature of the mixture at the inlet above the autoignition temperature of the mixture. In certain embodiments, the system further includes a heat exchanger configured to draw heat from the product gas of the reaction chamber and to heat the mixture prior to introducing the mixture into the reaction chamber. In certain embodiments, the heat exchanger comprises a tube-in-tube heat exchanger. In certain embodiments, the product gas is applied back into the reaction chamber and combined with the air-fuel mixture introduced into the reaction chamber. In certain embodiments, the system further comprises a heat exchange medium disposed in the reaction chamber. In certain embodiments, the medium is configured to maintain the internal temperature of the reaction chamber below the stoppage temperature of the mixture by conducting heat towards the inlet of the reaction chamber, where the medium is introduced into the oxidation chamber. Cooled by the mixture. In certain embodiments, the fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso-phen At least one of ethane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, includes receiving a gaseous air-fuel mixture, including a mixture of air and gaseous fuel, via intake; Compressing the mixture into a compression chamber coupled to the reciprocating engine and compressing the mixture in the reciprocating piston chamber; Receiving the mixture from the compression chamber through the inlet and oxidizing the mixture in an oxidation chamber structured to maintain oxidation of the fuel without catalyst at the internal temperature of the reaction chamber; And expanding the heated product gas from the reaction chamber in the reciprocating piston chamber coupled to the reciprocating piston chamber, thereby driving the reciprocating engine.

In certain embodiments, the internal temperature of the reaction chamber is maintained below the stoppage temperature of the fuel. In certain embodiments, the steps further comprise removing heat from the reaction chamber when the temperature in the reaction chamber approaches or rises to or near the stoppage temperature. In certain embodiments, the temperature of the mixture at the inlet is maintained above the autoignition temperature of the mixture. In certain embodiments, the steps further comprise heating the mixture by a heat exchanger before oxidizing the mixture in the reaction chamber. In certain embodiments, a heat exchanger is disposed in the reaction chamber. In certain embodiments, the inlet temperature of the mixture at the inlet of the reaction chamber is below the autoignition temperature of the mixture. In certain embodiments, the mixture is heated to a temperature above the autoignition temperature in a heat exchanger.

In certain embodiments, a method for oxidizing a fuel described herein includes compressing an air-fuel mixture comprising a mixture of air and gaseous fuel in a reciprocating piston compression chamber coupled to a reciprocating engine; In a reaction chamber configured to receive the mixture from the compression chamber through the inlet, oxidizing the mixture above the autoignition temperature of the fuel and below the stoppage temperature of the fuel; And expanding the product gas from the reaction chamber in the reciprocating piston chamber coupled to the reciprocating engine, thereby driving the reciprocating engine.

In certain embodiments, the internal temperature of the reaction chamber is maintained below the stoppage temperature of the fuel. In certain embodiments, the method further comprises removing heat from the reaction chamber when the adiabatic temperature in the reaction chamber approaches or rises above the stoppage temperature. In certain embodiments, the temperature of the mixture at the inlet is maintained above the autoignition temperature of the mixture. In certain embodiments, the method further comprises heating the mixture by a heat exchanger before oxidizing the fuel in the reaction chamber. In certain embodiments, a heat exchanger is disposed in the reaction chamber. In certain embodiments, the inlet temperature of the mixture at the inlet of the reaction chamber is below the autoignition temperature of the mixture. In certain embodiments, the mixture is heated to a temperature above the autoignition temperature in a heat exchanger.

In certain embodiments, a method for oxidizing a fuel described herein includes: applying an air-fuel mixture comprising a mixture of air and gaseous fuel to compression in a reciprocating compression piston coupled to a reciprocating engine; Applying the mixture from the compression piston to the reaction chamber structured to gradually oxidize the mixture in the reaction chamber above the autoignition temperature of the mixture and below the burnout temperature of the mixture; And applying the product gas from the reaction chamber to expansion in the reciprocating expansion piston coupled to the reciprocating engine, thereby driving the reciprocating engine.

In certain embodiments, the method further includes determining with the sensor if the temperature of the reaction chamber is at or near the burnout temperature. In certain embodiments, the method further includes applying removal of heat from the reaction chamber when the temperature in the reaction chamber is close to the burnout temperature such that the temperature in the reaction chamber is maintained below the burnout temperature. . In certain embodiments, the method further includes maintaining an internal temperature within the reaction chamber below about 2300 ° F.

In certain embodiments, a method for oxidizing a fuel described herein includes determining an oxygen content level in a reaction chamber having an inlet and an outlet and configured to gradually oxidize the fuel in a gas mixture without a catalyst; And outputting instructions for introducing a flue gas received from an outlet of the reaction chamber and containing a flue gas from oxidation of fuel in the reaction chamber based on the determined oxygen content level. .

In certain embodiments, introducing the flue gas comprises mixing the flue gas with a gas mixture. In certain embodiments, the method further includes determining that the internal temperature in the reaction chamber is close to the stoppage temperature of the fuel. In certain embodiments, the method further includes outputting instructions to reduce the internal temperature in the reaction chamber when the adiabatic temperature in the reaction chamber approaches the stoppage temperature of the fuel. In certain embodiments, the instructions further comprise removing heat from the reaction chamber. In certain embodiments, outputting the instructions is structured to change the burnout temperature of the fuel in the reaction chamber. In certain embodiments, the method further comprises determining an inlet temperature of the gas mixture at the reaction chamber inlet. In certain embodiments, the method further includes increasing the temperature of the gas mixture at the inlet when the inlet temperature is close to the autoignition temperature of the fuel such that the inlet temperature is maintained above the autoignition temperature. In certain embodiments, increasing the temperature comprises mixing the flue gas with the gas mixture at or near the reaction chamber inlet.

In certain embodiments, a method for oxidizing a fuel, as described herein, has a gas mixture at the reaction chamber inlet and an oxygen content level in the reaction chamber having an inlet and an outlet and configured to gradually oxidize the fuel in the gas mixture without a catalyst. Determining at least one of the inlet temperatures of; Based on at least one of the determined oxygen content level and the inlet temperature, the flue gas received from the outlet of the reaction chamber and containing heated product gas from oxidation of the fuel in the reaction chamber, the determined oxygen content level is close to a predetermined threshold. Or introducing it into the reaction chamber when at least one of it is at least one of being close to or below the autoignition temperature of the fuel.

In certain embodiments, introducing the flue gas includes mixing the flue gas with a gas mixture. In certain embodiments, the method further includes determining that the internal temperature in the reaction chamber is close to the stoppage temperature of the fuel. In certain embodiments, the method further includes reducing the internal temperature in the reaction chamber when the adiabatic temperature in the reaction chamber is close to the stoppage temperature of the fuel. In certain embodiments, reducing the internal temperature includes removing heat from the reaction chamber. In certain embodiments, the method further includes increasing the stoppage temperature in the reaction chamber by reducing the oxygen content in the reaction chamber.

In certain embodiments, a method for oxidizing a fuel described herein includes determining with the processor an oxygen content level in a reaction chamber having an inlet and an outlet and configured to gradually oxidize the fuel in a gas mixture without a catalyst; And introducing a flue gas into the reaction chamber based on the determined oxygen content level, the flue gas received from the outlet of the reaction chamber and containing heated product gas from oxidation of fuel in the reaction chamber.

In certain embodiments, introducing the flue gas includes mixing the flue gas with a gas mixture. In certain embodiments, the flue gas is mixed with the gas mixture at or near the reaction chamber inlet. In certain embodiments, the method further includes determining whether the internal temperature in the reaction chamber is approaching or exceeds the stoppage temperature of the fuel. In certain embodiments, the method further includes reducing the internal temperature in the reaction chamber if the adiabatic temperature in the reaction chamber is near or exceeds the stoppage temperature of the fuel. In certain embodiments, reducing the internal temperature includes removing heat from the reaction chamber. In certain embodiments, the method further includes changing the stoppage temperature in the reaction chamber by reducing the oxygen content in the reaction chamber.

In certain embodiments, a method for oxidizing a fuel described herein includes an inlet temperature of a gas mixture comprising an oxidizable fuel in a first reaction chamber having an inlet and an outlet and configured to maintain a gradual oxidation process without a catalyst. Determining when the temperature approaches or falls below the autoignition temperature of the fuel at the reaction chamber inlet; And when the inlet temperature approaches or falls below the autoignition temperature of the fuel, introducing a flue gas comprising at least partially oxidized product gas from the reaction chamber into the gas mixture at or near the inlet, thereby producing a gas mixture. Increasing the inlet temperature of the.

In certain embodiments, a method for oxidizing a fuel described herein includes a first fuel in a first gas mixture in a first reaction chamber configured to maintain gradual oxidation of the first fuel in the first reaction chamber without a catalyst. Gradually oxidizing; Introducing a flue gas comprising a heated product gas into the second reaction chamber from oxidation of the first fuel in the first reaction chamber; Introducing a second fuel into the second reaction chamber; And oxidizing the second fuel in the second reaction chamber in a gradual oxidation process without catalyst, wherein the first internal temperature in the first reaction chamber is maintained below the burnout temperature of the first fuel.

In certain embodiments, the method further includes maintaining a second internal temperature within the second reaction chamber below the stoppage temperature of the second fuel. In certain embodiments, the method reduces the second internal temperature in the second reaction chamber when the adiabatic temperature in the second reaction chamber is at or near the burnout temperature of the second fuel in the second reaction chamber. It further comprises a step. In certain embodiments, reducing the second internal temperature includes removing heat from the second reaction chamber. In certain embodiments, the burnout temperature of the second fuel is higher than the burnout temperature of the first fuel. In certain embodiments, the method reduces the first internal temperature in the first reaction chamber when the adiabatic temperature in the first reaction chamber approaches or exceeds the burnout temperature of the first fuel in the first reaction chamber. It further comprises a step. In certain embodiments, reducing the first internal temperature includes removing heat from the first reaction chamber. In certain embodiments, the method further comprises determining a first inlet temperature of the gas mixture at the first reaction chamber inlet. In certain embodiments, the method further provides that when the first inlet temperature approaches or drops below the autoignition temperature of the first fuel in the first reaction chamber such that the first inlet temperature is maintained above the autoignition temperature, Increasing the first inlet temperature. In certain embodiments, the method further comprises determining a second inlet temperature at the second reaction chamber inlet. In certain embodiments, the method further provides that if the second inlet temperature approaches or drops below the autoignition temperature of the second fuel in the second reaction chamber such that the second inlet temperature is maintained above the autoignition temperature, Increasing the second inlet temperature. In certain embodiments, the method includes increasing the second inlet temperature, which further includes introducing flue gas to mix with the second fuel at or near the second reaction chamber inlet.

In certain embodiments, a method for oxidizing a fuel described herein includes a first fuel in a first gas mixture in a first reaction chamber configured to maintain gradual oxidation of the first fuel in the first reaction chamber without a catalyst. Gradually oxidizing; Introducing a flue gas comprising a heated product gas into a second reaction chamber structured to maintain gradual oxidation without catalyst from oxidation of the first fuel in the first reaction chamber; Determining with the processor the oxygen content level in the second reaction chamber; Introducing a second fuel into the second reaction chamber; And oxidizing the second fuel in the second reaction chamber in a gradual oxidation process without catalyst.

In certain embodiments, the amount and distribution in the second chamber of introduction of the flue gas into the second reaction chamber is based on the determined oxygen content level. In certain embodiments, the first internal temperature in the first reaction chamber is maintained below the burnout temperature of the first fuel. In certain embodiments, the method further includes maintaining a second internal temperature within the second reaction chamber below the stoppage temperature of the second fuel. In certain embodiments, the method reduces the second internal temperature in the second reaction chamber when the adiabatic temperature in the second reaction chamber is at or near the burnout temperature of the second fuel in the second reaction chamber. It further comprises a step. In certain embodiments, reducing the second internal temperature includes removing heat from the second reaction chamber. In certain embodiments, the method reduces the first internal temperature in the first reaction chamber when the adiabatic temperature in the first reaction chamber approaches or exceeds the burnout temperature of the first fuel in the first reaction chamber. It further comprises a step. In certain embodiments, reducing the first internal temperature includes removing heat from the first reaction chamber. In certain embodiments, the method further comprises determining a first inlet temperature of the gas mixture at the first reaction chamber inlet. In certain embodiments, the method further provides that when the first inlet temperature approaches or drops below the autoignition temperature of the first fuel in the first reaction chamber such that the first inlet temperature is maintained above the autoignition temperature, Increasing the first inlet temperature. In certain embodiments, the method further comprises determining a second inlet temperature at the second reaction chamber inlet. In certain embodiments, the method further provides that if the second inlet temperature approaches or drops below the autoignition temperature of the second fuel in the second reaction chamber such that the second inlet temperature is maintained above the autoignition temperature, Increasing the second inlet temperature. In certain embodiments, increasing the second inlet temperature further includes introducing flue gas to mix with the second fuel at or near the second reaction chamber inlet.

In certain embodiments, a system for oxidizing a fuel, as described herein, has a first inlet and a first outlet, and is structured to receive a first gas comprising a first oxidizable fuel, and progressively of the first fuel. A first reaction chamber configured to maintain an oxidation process; And a second reaction chamber having a second inlet and a second outlet, and configured to receive a second gas comprising a second oxidizable fuel, and configured to maintain a gradual oxidation process of the second fuel; And the second reaction chamber is configured to maintain an internal temperature in each reaction chamber below the combustion stop temperature of each fuel, and the second reaction chamber includes a flue gas comprising heated product gas in the first reaction chamber. And configured to receive in the second reaction chamber through the second inlet from oxidation of the fuel.

In certain embodiments, the system further includes a heat exchange medium disposed in at least one of the reaction chambers and configured to maintain the internal temperature of the reaction chamber below the adiabatic shutdown temperature. In certain embodiments, the system is structured such that at least one of the first or second reaction chambers reduces each internal temperature when the adiabatic temperature in each reaction chamber is near or exceeds the burnout temperature of each fuel. It is. In certain embodiments, at least one of the first and second reaction chambers is configured to reduce each internal temperature by removing heat from each reaction chamber by a heat exchanger. In certain embodiments, the heat exchanger includes a fluid introduced into each reaction chamber. In certain embodiments, the heat exchanger is structured to drain the fluid from each reaction chamber. In certain embodiments, the heat exchanger includes means for generating steam.

In certain embodiments, the heat exchanger is configured to attract heat from each reaction chamber when the temperature in each reaction chamber exceeds 2300 ° F. In certain embodiments, when the first inlet temperature approaches or drops below the autoignition temperature of the first fuel at the first inlet, the first reaction chamber increases the temperature of the first gas at the first inlet. It is structured to be. In certain embodiments, when the second inlet temperature approaches or drops below the autoignition temperature of the second fuel at the second inlet, the second reaction chamber increases the temperature of the second gas at the second inlet. It is structured to be.

In certain embodiments, when the second inlet temperature of the second gas at the second inlet approaches or drops below the autoignition temperature of the second fuel, the second reaction chamber mixes the flue gas with the second gas. It is structured to be. In certain embodiments, the distribution of flue gas in the second reaction chamber is based on at least one of a second inlet temperature of the second gas at the second inlet and an internal temperature of the second reaction chamber. In certain embodiments, the system further includes a turbine or piston engine that receives gas from at least one of the reaction chambers. In certain embodiments, the turbine receives gas from the second reaction chamber. In certain embodiments, before introducing the fuel mixture into at least one of the reaction chambers, the compressor receives the gas comprising the fuel mixture. In certain embodiments, the compressor is configured to compress the second gas prior to introducing the second gas into the second reaction chamber.

In certain embodiments, a system for oxidizing fuel described herein includes an oxidizer having a reaction chamber configured to receive and oxidize a gas mixture comprising an oxidizable fuel in a gradual oxidation process within the reaction chamber; An inlet configured to introduce a fluid into the reaction chamber during the oxidation process that is at an inlet temperature lower than the internal temperature of the reaction chamber such that the fluid is heated as the fluid is introduced into the reaction chamber; And an outlet configured to extract the heated fluid from the reaction chamber, wherein the reaction chamber is configured to maintain the internal temperature above the self ignition temperature of the fuel and below the fuel stop temperature of the fuel.

In certain embodiments, the inlet is structured to introduce liquid into the reaction chamber. In certain embodiments, liquid is introduced into the reaction chamber by passing one or more coils in the reaction chamber. In certain embodiments, the coils are not in fluid communication with the reaction chamber. In certain embodiments, liquid is introduced into the reaction chamber by injecting the liquid into the reaction chamber such that the liquid is mixed with the gas mixture in the reaction chamber. In certain embodiments, the inlet is structured to introduce the fluid as a gas into the reaction chamber. In certain embodiments, gas is introduced into the reaction chamber by passing one or more coils in the reaction chamber. In certain embodiments, the coils do not allow mixing of the gas and gas mixture in the reaction chamber. In certain embodiments, gas is introduced into the reaction chamber by injecting the gas into the reaction chamber such that the gas is mixed with the gas mixture in the reaction chamber. In certain embodiments, the outlet is configured to extract the heated fluid as a gas from the reaction chamber. In certain embodiments, the outlet is configured to add the gas back into the reaction chamber such that the gas is mixed with the gas mixture in the reaction chamber. In certain embodiments, fluid is introduced into the reaction chamber when the adiabatic reaction temperature in the reaction chamber is close to the burnout temperature. In certain embodiments, the inlet temperature is below the autoignition temperature of the fuel. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, is structured to receive and oxidize fuel in a gradual oxidation process in a reaction chamber, and wherein the internal temperature is above the autoignition temperature of the fuel and below the burnout temperature of the fuel. Adding a gas mixture comprising an oxidizable fuel to an oxidizer having a reaction chamber structured to maintain the fuel cell; Introducing a fluid into the reaction chamber during the oxidation process that is at an inlet temperature lower than the internal temperature of the reaction chamber at the inlet temperature such that the fluid is heated as the fluid is introduced into the reaction chamber; And extracting the heated fluid from the reaction chamber.

In certain embodiments, the fluid is introduced into the reaction chamber as a liquid. In certain embodiments, liquid is introduced into the reaction chamber by passing one or more coils in the reaction chamber. In certain embodiments, liquid is injected into the reaction chamber such that the liquid is mixed with the gas mixture in the reaction chamber. In certain embodiments, the fluid is introduced into the reaction chamber as a gas. In certain embodiments, gas is introduced into the reaction chamber by passing the gas through one or more coils in the reaction chamber. In certain embodiments, gas is injected into the reaction chamber such that the gas is mixed with the gas mixture in the reaction chamber. In certain embodiments, the heated fluid is extracted from the reaction chamber as a heated gas. In certain embodiments, the method further includes adding the heated gas back into the reaction chamber such that the heated gas is mixed with the gas mixture in the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, an oxidizer for oxidizing a fuel described herein includes one or more inlets configured to apply at least one gas of fuel, oxidant or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having one or more outlets configured to be; And at or before the one or more inlets, configured to maintain one or more temperatures of the at least one gas above the autoignition temperature of the resulting mixture in the reaction chamber comprising at least one gas of fuel, oxidant or diluent. And a heater, the reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature and the maximum reaction temperature in the reaction chamber below the mixture's stoppage temperature.

In certain embodiments, the reaction chamber comprises a single inlet. In certain embodiments, the oxidizer is structured to change the flow rate at which the mixture is introduced into the reaction chamber through the inlet. In certain embodiments, the heater comprises a heat exchanger that transfers heat from the reaction products to the mixture at or in front of one or more inlets. In certain embodiments, the heater is configured to mix at least one oxidant or diluent with fuel at or in front of one or more inlets. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive a generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through one or more inlets. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel, as described herein, is configured to add an inlet structured to apply at least one gas of fuel, oxidant, or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having an outlet; And means for maintaining the temperature of the inlet gas at or before the inlet above the autoignition temperature of the resulting mixture in the reaction chamber comprising at least one gas of fuel, oxidant or diluent in the reaction chamber, The reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature.

In certain embodiments, the reaction chamber includes a plurality of inlets. In certain embodiments, the reaction chamber comprises a plurality of outlets. In certain embodiments, the means for raising the temperature includes a heat exchanger that transfers heat from the reaction products to the mixture at or before the inlet. In certain embodiments, the means for raising the temperature is configured to mix the diluent with the fuel at or before the inlet. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which the mixture is introduced into the reaction chamber through the inlet. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through one or more inlets.

In certain embodiments, an oxidizer for oxidizing a fuel described herein includes one or more inlets configured to apply at least one gas of fuel, oxidant or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having one or more outlets configured to be; And structured to maintain the temperature of one or more of the at least one gas at or before the one or more inlets to be above the autoignition temperature of the resulting mixture comprising at least one gas of fuel, oxidant or diluent in the reaction chamber. The reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber above the mixture's burnout temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature. .

In certain embodiments, the oxidizer further includes a heat extractor structured to remove heat from the reaction chamber. In certain embodiments, the heat extractor is configured to remove heat from the reaction chamber by generating steam. In certain embodiments, the oxidizer has a reaction chamber in which the reaction chamber comprises a single inlet. In certain embodiments, the oxidizer is structured to vary the flow rate at which the mixture is introduced into the reaction chamber through a single inlet. In certain embodiments, the heater comprises a heat exchanger that transfers heat from the reaction products to the mixture at or in front of one or more inlets. In certain embodiments, the heater is configured to mix the diluent with fuel at or before one or more inlets. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through one or more inlets. In certain embodiments, the apparatus further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel, as described herein, is configured to add an inlet structured to apply at least one gas of fuel, oxidant, or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having an outlet; And means for maintaining the temperature of the inlet gas above the autoignition temperature of the resulting mixture comprising at least one gas of fuel, oxidant or diluent in the reaction chamber, at or before the inlet, wherein the reaction chamber comprises It is structured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber above the mixture's burnout temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature.

In certain embodiments, the reaction chamber comprises a plurality of inlets. In certain embodiments, the reaction chamber comprises a plurality of outlets. In certain embodiments, the means for raising the temperature includes a heat exchanger that transfers heat from the reaction products to the mixture at or before the inlet. In certain embodiments, the means for raising the temperature is configured to mix the diluent with the fuel at or before the inlet. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which the mixture is introduced into the reaction chamber through the inlet. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel described herein includes one or more inlets configured to apply at least one gas of fuel, oxidant or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having one or more outlets configured to be; And at or before the one or more inlets, structure the temperature of one or more of the at least one gas to be below the autoignition temperature of the resulting mixture comprising at least one gas of fuel, oxidant or diluent in the reaction chamber. The reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber below the mixture's burnout temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature. .

In certain embodiments, the reaction chamber comprises a single inlet. In certain embodiments, the oxidizer is configured to vary the flow rate at which the mixture is introduced into the reaction chamber through one or more inlets. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through one or more inlets. In certain embodiments, the oxidizer further includes a heat exchanger that transfers heat from the reaction products to the mixture at or in front of one or more inlets. In certain embodiments, the heater is configured to mix the diluent with fuel at or before one or more inlets. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel, as described herein, is configured to add an inlet structured to apply at least one gas of fuel, oxidant, or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having an outlet; And means for maintaining the temperature of the inlet gas at or before the inlet below the autoignition temperature of the resulting mixture in the reaction chamber comprising at least one gas of fuel, oxidant or diluent in the reaction chamber, The reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber below the mixture's stop flame temperature and the maximum reaction temperature in the reaction chamber below the mixture's flame stop temperature.

In certain embodiments, the reaction chamber includes a plurality of inlets. In certain embodiments, the reaction chamber comprises a plurality of outlets. In certain embodiments, the means for maintaining the temperature comprises a heat exchanger that transfers heat from the reaction products to the mixture at or before the inlet. In certain embodiments, the means for maintaining the temperature is configured to mix the diluent with the fuel at or before the inlet. In certain embodiments, the oxidizer is structured to generate steam using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which the mixture is introduced into the reaction chamber through the inlet. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel described herein includes one or more inlets configured to apply at least one gas of fuel, oxidant or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having one or more outlets configured to be; And at or before the one or more inlets, structure the temperature of one or more of the at least one gas to be below the autoignition temperature of the resulting mixture comprising at least one gas of fuel, oxidant or diluent in the reaction chamber. The reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber above the mixture's burnout temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature. .

In certain embodiments, the heat extractor is configured to remove heat from the reaction chamber. In certain embodiments, the heat extractor is configured to remove heat from the reaction chamber by generating steam. In certain embodiments, the oxidizer further includes a heat conveyor in the reaction chamber structured to distribute heat in the reaction chamber. In certain embodiments, the heat conveyor comprises a porous medium in the reaction chamber. In certain embodiments, the heat conveyor includes a flow medium in the reaction chamber. In certain embodiments, the heat conveyor includes a medium that is circulated through the reaction chamber. In certain embodiments, the reaction chamber comprises a single inlet. In certain embodiments, the oxidizer further includes a heat exchanger that transfers heat from the reaction products to the mixture at or in front of one or more inlets. In certain embodiments, the heater is configured to mix the diluent with fuel at or before one or more inlets. In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through one or more inlets. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the apparatus further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, an oxidizer for oxidizing a fuel, as described herein, is configured to add an inlet structured to apply at least one gas of fuel, oxidant, or diluent into the reaction chamber, and reaction products from the reaction chamber. A reaction chamber having an outlet; And a heater structured to maintain the temperature of the inlet gas at or before the inlet to be below the autoignition temperature of the resulting mixture in the reaction chamber comprising at least one gas of fuel, oxidant or diluent in the reaction chamber. And the reaction chamber is configured to oxidize the mixture and to maintain the adiabatic temperature in the reaction chamber above the mixture's burnout temperature and the maximum reaction temperature in the reaction chamber below the mixture's burnout temperature.

In certain embodiments, the oxidizer comprises means for removing heat from the reaction chamber. In certain embodiments, the means for removing heat is configured to remove heat from the reaction chamber by generating steam. In certain embodiments, the oxidizer comprises means for distributing heat in the reaction chamber. In certain embodiments, the means for distributing heat comprises a porous medium in the reaction chamber. In certain embodiments, the means for distributing heat comprises a flow medium in the reaction chamber. In certain embodiments, the means for distributing heat comprises a medium circulated through the reaction chamber. In certain embodiments, the reaction chamber includes a plurality of inlets. In certain embodiments, the reaction chamber comprises a plurality of outlets. In certain embodiments, the heater comprises a heat exchanger that transfers heat from the reaction products to the mixture at or in front of one or more inlets. In certain embodiments, the heater is configured to mix the diluent with the fuel at or before the inlet.

In certain embodiments, the oxidizer is structured to drive the generator for power generation using heat from the reaction products. In certain embodiments, the oxidizer is structured to drive the generator by a turbine or piston engine that is structured to expand reaction products from the reaction chamber. In certain embodiments, the oxidizer is structured to heat material that has not passed through the oxidizer using heat from the reaction products. In certain embodiments, the oxidizer is configured to vary the flow rate at which one or more of the at least one gas of fuel, oxidant or diluent is introduced into the reaction chamber through the inlet. In certain embodiments, the oxidizer is structured to change the flow rate at which reaction products are applied from the reaction chamber through the outlet. In certain embodiments, the oxidizer further includes a regulator structured to change at least one of the flow of the mixture or the pressure of the mixture at or near the inlet.

In certain embodiments, a system for oxidizing fuel described herein has a first inlet and a first outlet, and is structured to receive a first gas through the first inlet, the first gas comprising an oxidizable fuel, A first reaction chamber configured to maintain gradual oxidation of the gas and communicate flue gas through the first inlet; And a second reaction chamber separate from the first reaction chamber, the second reaction chamber having a second inlet and a second outlet and configured to receive through the inlet a second gas and a flue gas comprising an oxidizable fuel, A second reaction chamber configured to maintain gradual oxidation, the flue gas being communicated from the first inlet to the second inlet until the internal temperature in the second reaction chamber is above the self-ignition temperature of the second gas.

In certain embodiments, after the internal temperature is above the autoignition temperature, the flue gas is not communicated from the first outlet to the second inlet. In certain embodiments, at least one of the first or second reaction chamber is configured to reduce the respective internal temperature when the internal temperature in each reaction chamber is near or exceeds the burnout temperature of each fuel. In certain embodiments, at least one of the first or second reaction chambers is configured to reduce each internal temperature by removing heat from each reaction chamber. In certain embodiments, at least one of the first and second reaction chambers is configured to remove heat by a heat exchanger. In certain embodiments, the heat exchanger includes a fluid introduced into each reaction chamber. In certain embodiments, the heat exchanger is structured to drain the fluid from each reaction chamber. In certain embodiments, the heat exchanger includes means for generating steam. In certain embodiments, the heat exchanger is configured to attract heat from each reaction chamber when the temperature in each reaction chamber exceeds 2300 ° F. In certain embodiments, the second reaction chamber is structured to mix flue gas with the second gas when the temperature of the second gas at or near the second inlet approaches or falls below the autoignition temperature of the second fuel. It is. In certain embodiments, the system further includes a turbine or piston engine that receives gas from at least one of the reaction chambers. In certain embodiments, the turbine receives and expands gas from the second reaction chamber. In certain embodiments, the system further includes a compressor that receives and compresses the gas prior to introducing the gas into at least one of the reaction chambers. In certain embodiments, the compressor is configured to compress the second gas prior to introducing the second gas into the second reaction chamber.

In certain embodiments, a system for oxidizing a fuel described herein includes an agent having an outlet and configured to maintain gradual oxidation of the first gas comprising the oxidizable fuel and communicate the reaction product through the first outlet. 1 reaction chamber; And a second reaction chamber separate from the first reaction chamber, the second reaction chamber having an inlet and configured to receive a second gas and a reaction product comprising an oxidizable fuel, the internal temperature of the second reaction chamber being self-contained. And a second reaction chamber configured to maintain gradual oxidation of the second gas while below the ignition temperature, and to receive the reaction product from the first reaction chamber through the inlet.

In certain embodiments, after the internal temperature is above the autoignition temperature, the reaction products are not communicated from the first reaction chamber to the second reaction chamber. In certain embodiments, at least one of the first or second reaction chamber is configured to reduce the respective internal temperature when the internal temperature in each reaction chamber is near or exceeds the burnout temperature of each fuel. In certain embodiments, at least one of the first or second reaction chambers is configured to reduce each internal temperature by removing heat from each reaction chamber. In certain embodiments, when the temperature of the second gas at the inlet approaches or drops below the autoignition temperature of the second fuel, the second reaction chamber is configured to mix the reaction product with the second gas. . In certain embodiments, the system further includes a turbine or piston engine that receives gas from at least one of the reaction chambers. In certain embodiments, the turbine receives and expands gas from the second reaction chamber. In certain embodiments, further comprising a compressor to receive and compress the gas prior to introducing the gas into at least one of the reaction chambers. In certain embodiments, the compressor is configured to compress the second gas prior to introducing the second gas into the second reaction chamber.

In certain embodiments, a system for oxidizing fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, which receives a gas comprising an oxidizable fuel through the inlet and maintains the oxidation process without a catalyst. An oxidizer having a reaction chamber that is structured to be; A detection module that detects when the reaction chamber temperature of the gas approaches or falls below the autoignition threshold of the gas in the reaction chamber so that the reaction chamber does not oxidize the fuel; And based on the detection module, a calibration to output at least one of a residence time of the gas in the reaction chamber and an autoignition delay time in the reaction chamber sufficient to self-ignite and oxidize with respect to the gas simultaneously with the reaction chamber. Contains modules

In certain embodiments, the calibration module is configured to change the residence time of the gas in the reaction chamber by varying the flow of gas through the reaction chamber. In certain embodiments, the calibration module is configured to increase the residence time of the gas in the reaction chamber by reducing the flow of gas through the reaction chamber. In certain embodiments, the calibration module is configured to increase the residence time of the gas in the reaction chamber by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the calibration module is structured to change the autoignition delay time in the reaction chamber by changing the gas temperature in the reaction chamber. In certain embodiments, the calibration module is configured to reduce the autoignition delay time in the reaction chamber by increasing the gas temperature in the reaction chamber to the heater. In certain embodiments, the calibration module is structured to reduce the autoignition delay time in the reaction chamber by circulating the product gas from the outlet to the inlet. In certain embodiments, the reaction chamber is structured to maintain oxidation of the oxidizable fuel below the freeze temperature without catalyst. In certain embodiments, the system further includes a turbine or piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the system further includes a compressor that receives and compresses the gas comprising the fuel mixture prior to introducing the fuel mixture into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a system for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the structure being configured to receive a gas comprising an oxidizable fuel through the inlet and maintain an oxidation process An oxidizer having an advanced reaction chamber; A detection module that detects when the reaction chamber temperature of the gas approaches or falls below the autoignition threshold of the gas in the reaction chamber so that the reaction chamber does not oxidize the fuel; And based on the detection module, the processor is configured to determine at least one change in the residence time of the gas in the reaction chamber and the autoignition delay time in the reaction chamber sufficient to self-ignite and oxidize with respect to the gas simultaneously with the reaction chamber. And a calibration module, wherein the oxidizer is configured to oxidize the gas while the gas is present in the reaction chamber based on a change to at least one of the residence time and the autoignition delay time.

In certain embodiments, the calibration module is configured to change the residence time of the gas in the reaction chamber by varying the flow of gas through the reaction chamber. In certain embodiments, the calibration module is configured to increase the residence time of the gas in the reaction chamber by reducing the flow of gas through the reaction chamber. In certain embodiments, the calibration module is configured to increase the residence time of the gas in the reaction chamber by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the calibration module is structured to change the autoignition delay time in the reaction chamber by changing the gas temperature in the reaction chamber. In certain embodiments, the calibration module is configured to reduce the autoignition delay time in the reaction chamber by increasing the gas temperature in the reaction chamber to the heater. In certain embodiments, the calibration module is structured to reduce the autoignition delay time in the reaction chamber by circulating the product gas from the outlet to the inlet. In certain embodiments, the reaction chamber is structured to maintain oxidation of the oxidizable fuel below the freeze temperature without catalyst.

In certain embodiments, a system for oxidizing a fuel, as described herein, is an oxidizer having a reaction chamber having an inlet and an outlet, the structure being configured to receive a gas comprising an oxidizable fuel through the inlet and maintain an oxidation process An oxidizer having an advanced reaction chamber; And a module for outputting instructions to increase at least one of a residence time of a gas in the reaction chamber and a reaction temperature in the reaction chamber to oxidize fuel simultaneously with the reaction chamber based on the detection of the reaction chamber temperature. .

In certain embodiments, the module is structured to change the residence time of the gas in the reaction chamber by varying the flow of gas through the reaction chamber. In certain embodiments, the module is structured to increase the residence time of the gas in the reaction chamber by reducing the flow of gas through the reaction chamber. In certain embodiments, the module is configured to increase the residence time of the gas in the reaction chamber by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the module is structured to reduce the autoignition delay time in the reaction chamber by increasing the gas temperature in the reaction chamber to a heater. In certain embodiments, the calibration module is structured to reduce the autoignition delay time in the reaction chamber by circulating the product gas from the outlet to the inlet.

In certain embodiments, a method for oxidizing a fuel, as described herein, in an oxidation system containing a gas comprising an oxidizable fuel in a reaction chamber having an inlet and an outlet and configured to maintain an oxidation process, Detecting when the reaction chamber temperature approaches or falls below a level such that the reaction chamber alone does not support oxidation of the fuel; And based on the detection module, varying at least one of a residence time of the gas in the reaction chamber and a self-ignition delay time in the reaction chamber sufficient to self-ignite and oxidize to the gas simultaneously with the reaction chamber.

In certain embodiments, the residence time of the gas in the reaction chamber is changed by varying the flow of gas through the reaction chamber. In certain embodiments, the residence time of the gas in the reaction chamber is changed by reducing the flow of gas through the reaction chamber. In certain embodiments, the residence time of the gas in the reaction chamber is changed by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the autoignition delay time in the reaction chamber is changed by changing the gas temperature in the reaction chamber. In certain embodiments, the autoignition delay time in the reaction chamber is reduced by increasing the gas temperature in the reaction chamber with a heater. In certain embodiments, the self-ignition delay time is reduced by circulating the product gas from the outlet to the inlet. In certain embodiments, the reaction chamber maintains oxidation of the oxidizable fuel below the stoppage temperature without catalyst. In certain embodiments, the method further comprises expanding the product gas from the reaction chamber in a turbine or piston engine. In certain embodiments, the method further comprises compressing the gas prior to introducing the gas into the reaction chamber. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, in an oxidation system containing a gas comprising an oxidizable fuel in a reaction chamber having an inlet and an outlet and configured to maintain an oxidation process, Detecting when the reaction chamber temperature approaches or falls below a level such that the reaction chamber alone does not support oxidation of the fuel; And based on the detection module, varying the self-ignition delay time in the reaction chamber sufficient to self-ignite and oxidize with respect to the gas simultaneously with the reaction chamber.

In certain embodiments, varying the autoignition delay time includes introducing additional heat into the reaction chamber, thereby increasing the internal chamber temperature to a level at which oxidation of the fuel is maintained. In certain embodiments, the method further comprises changing the residence time of the gas in the reaction chamber by varying the flow of gas through the reaction chamber. In certain embodiments, the method further comprises changing the residence time of the gas in the reaction chamber by reducing the flow of gas through the reaction chamber. In certain embodiments, the method further comprises changing the residence time of the gas in the reaction chamber by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the reaction chamber maintains oxidation of the oxidizable fuel below the stoppage temperature without catalyst. In certain embodiments, the method further comprises expanding the product gas from the reaction chamber in the turbine or piston engine. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, when the reaction chamber temperature of the gas approaches or falls below a temperature level such that the reaction chamber alone does not support oxidation of the fuel alone, Introducing a heat source into the reaction chamber thereby increasing the internal reaction chamber temperature to a level at which oxidation of the fuel is maintained.

In certain embodiments, increasing the internal temperature reduces the autoignition delay time. In certain embodiments, the method further comprises changing the residence time of the gas in the reaction chamber by varying the flow of gas through the reaction chamber. In certain embodiments, the method further comprises changing the residence time of the gas in the reaction chamber by reducing the flow of gas through the reaction chamber. In certain embodiments, the method further includes changing the residence time of the gas in the reaction chamber by recycling the flow of gas from the outlet to the inlet of the reaction chamber. In certain embodiments, the reaction chamber maintains oxidation of the oxidizable fuel below the stoppage temperature without catalyst. In certain embodiments, the method further comprises expanding the product gas from the reaction chamber in the turbine or piston engine. In certain embodiments, the oxidizable fuel is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso -At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, a method for oxidizing a fuel, as described herein, may be used to mix a gas having a low-energy-content (LEC) fuel to produce a high-energy-content. (HEC) forming a gas mixture having at least one of a group comprising a gas comprising fuel, a gas comprising an oxidant and a gas comprising a diluent, all of which are below the autoignition temperature of any of the gases being mixed. Present at a temperature of; Increasing the temperature of the gas mixture to at least the autoignition temperature of the gas mixture and self-igniting the gas mixture; And maintaining the temperature of the gas mixture below the burnout temperature while oxidizing the self-ignited gas mixture.

In certain embodiments, the gas mixture is raised to at least the autoignition temperature by a heat exchanger. In certain embodiments, a heat exchanger is placed in a reaction chamber that maintains oxidation of the gas mixture without catalyst. In certain embodiments, the gas mixture is raised to at least the autoignition temperature in the reaction chamber that maintains oxidation of the gas mixture without catalyst. In certain embodiments, the reaction chamber maintains oxidation of the mixture below the stoppage temperature of the gas mixture. In certain embodiments, the method further includes expanding the gas with a turbine or piston engine that receives the gas from the reaction chamber. In certain embodiments, the gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso- At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, the oxidation method described herein comprises at least self-ignition of a first gas mixture comprising a gas with an oxidant mixed with a determined range of low energy-content (LEC) fuel and high energy-content (HEC) fuel. Heating the first gas mixture to a temperature; After heating, injecting a second gas mixture of LEC fuel gas and HEC fuel, wherein the ratio and injection rate of the LEC and HEC gas are substantially the same as when injected into a heated gas comprising an oxidant Selected to generate; At the rate of producing a substantially homogeneous first gas mixture at a time less than the ignition delay time for the second gas mixture while self-igniting the first gas mixture, the injected second gas mixture is heated first with oxidant. Mixing with a gas mixture; And oxidizing the self-ignited first gas mixture while maintaining the temperature of the first gas mixture below the burnout temperature.

In certain embodiments, the first gas mixture is raised to at least the autoignition temperature by a heat exchanger. In certain embodiments, a heat exchanger is placed in the reaction chamber that maintains oxidation of the first gas mixture without a catalyst. In certain embodiments, the first gas mixture is raised to at least the autoignition temperature in the reaction chamber that maintains oxidation of the gas mixture without catalyst. In certain embodiments, the reaction chamber maintains oxidation of the second gas mixture below the stoppage temperature of the gas mixture. In certain embodiments, the method further includes expanding the gas with a turbine or piston engine that receives the gas from the reaction chamber. In certain embodiments, the first gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, At least one of iso-pentane, n-pentane, acetylene, hexane and carbon monoxide. In certain embodiments,

In certain embodiments, the oxidation method described herein includes a low energy-content (LEC) fuel, a high energy-content (HEC) fuel gas, an oxidant-comprising (OC) gas and a diluent-containing ( receiving a gas mixture comprising at least one of a group of diluent-containing) (DC) gases into the reaction chamber inlet, the gas mixture having an initial temperature below the self-ignition temperature of the mixture before being received into the inlet; Maintaining the internal temperature of the reaction chamber below the combustion stop temperature by a heat exchange medium disposed within the reaction chamber; Maintaining the reaction chamber inlet temperature above the mixture's autoignition temperature by transferring heat through a heat exchange medium; Subjecting the mixture to the inlet through the first passage through a medium hotter than the mixture's autoignition temperature until the mixture reaches a temperature above the autoignition temperature of the mixture; And applying the mixture to the reaction chamber outlet via a second passage that generally opposes the first passage.

In certain embodiments, the reaction chamber maintains oxidation of the gas mixture without catalyst. In certain embodiments, the reaction chamber maintains oxidation of the mixture below the stoppage temperature of the gas mixture by circulating a heat exchange medium from the reaction chamber. In certain embodiments, the method further includes expanding the gas with a turbine or piston engine that receives the gas from the reaction chamber outlet. In certain embodiments, the gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso- At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, the oxidizer described herein is a reaction chamber having an inlet and an outlet, the inlet having a low energy-content (LEC) fuel, a high energy-content (HEC) fuel gas, an oxidant-containing (OC) gas, and A reaction chamber configured to receive a gas having a mixture of at least one of the group of diluent-containing (DC) gases, the gas mixture being below the autoignition temperature of the gas mixture; A heat exchange medium disposed within the reaction chamber, the heat exchange medium configured to maintain the internal temperature of the reaction chamber below the burnout temperature, and to maintain the reaction chamber inlet temperature of the fuel above the autoignition temperature of the fuel; And at least one flow passage through the chamber from the inlet to the outlet, until the gas mixture reaches a temperature above the autoignition temperature of the gas mixture, the first passageway passes the gas through a medium hotter than the autoignition temperature of the gas mixture. And configured to enter the inlet, and the flow passage is structured to pass the second passage through the medium to apply the oxidizing gas mixture, so that the second passage defines at least one flow passage generally opposed to the first flow passage. Include.

In certain embodiments, the reaction chamber is structured to maintain oxidation of the gas mixture along at least one of the first and second flow passages without a catalyst. In certain embodiments, the reaction chamber is configured to maintain oxidation of the mixture below the stoppage temperature of the gas mixture by circulating a heat exchange medium from the reaction chamber. In certain embodiments, the system further includes at least one of a turbine or a piston engine configured to receive gas from the reaction chamber outlet and expand the gas. In certain embodiments, the gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso- At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, the oxidizer described herein is a reaction chamber having an inlet and an outlet, the inlet having a low energy-content (LEC) fuel, a high energy-content (HEC) fuel gas, an oxidant-containing (OC) gas, and A reaction chamber configured to receive a gas having a mixture of at least one of the group of diluent-containing (DC) gases, the gas mixture being below the autoignition temperature of the gas mixture; And a thermal controller structured to increase the temperature of the gas mixture to at least the self-ignition temperature of the mixture, thereby self-igniting the gas mixture, and maintaining the temperature of the gas mixture below the burnout temperature while oxidizing the self-ignitioned gas mixture. It includes (controller).

In certain embodiments, the heat controller includes a heat exchanger structured to raise the temperature of the mixture to at least the autoignition temperature. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, after the mixture is in the reaction chamber, the heat exchanger is structured to heat above the autoignition temperature. In certain embodiments, the reaction chamber is structured to maintain oxidation of the mixture below the stoppage temperature of the gas mixture without catalyst. In certain embodiments, the gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso- At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, the oxidizer described herein is a reaction chamber having an inlet and an outlet, the inlet having a low energy-content (LEC) fuel, a high energy-content (HEC) fuel gas, an oxidant-containing (OC) gas, and A reaction chamber configured to receive a gas having a mixture of at least one of the group of diluent-containing (DC) gases, the gas mixture being below the autoignition temperature of the gas mixture; A thermal controller structured to heat the first gas mixture to at least the autoignition temperature of the first gas mixture comprising a gas with an oxidant mixed with a determined range of low energy-content (LEC) fuel and high energy-content (HEC) fuel. ; An injector structured to inject a second gaseous mixture of LEC fuel gas and HEC fuel after the first gas is heated to at least the autoignition temperature of the first gaseous mixture, wherein the injector is formed when the gas is injected into the reaction chamber; Inject at a rate of injection and a ratio of LEC and HEC gas selected to produce a ratio of LEC and HEC gas substantially the same as the first gas mixture, the reaction chamber self-igniting the first gas mixture and for the second gas mixture To mix with a heated gas containing an oxidant to produce a substantially uniform first gas mixture at a time less than the ignition delay time, and to oxidize the self-ignited first gas mixture with the temperature of the first gas mixture. It is structured to maintain below the burnout temperature.

In certain embodiments, the heat controller includes a heat exchanger structured to raise the temperature of the mixture to at least the autoignition temperature. In certain embodiments, the heat exchanger is disposed in the reaction chamber. In certain embodiments, the reaction chamber is structured to maintain oxidation of the first gas mixture in the reaction chamber without catalyst. In certain embodiments, the reaction chamber is configured to maintain oxidation of the second gas mixture in the reaction chamber below the stoppage temperature of the gas mixture without catalyst. In certain embodiments, the system further comprises at least one of a turbine or a piston engine that receives gas from the reaction chamber and expands the gas. In certain embodiments, the first gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, At least one of iso-pentane, n-pentane, acetylene, hexane and carbon monoxide.

Description of one or more embodiments of these concepts is set forth in the accompanying drawings and the description below. Other features, objects, and advantages of these concepts will be apparent from the description and drawings, and from the claims. As described herein, the various embodiments described above or described below may be used in conjunction with and in conjunction with other embodiments described or implied herein. A separate discussion of the various embodiments, unless otherwise expressly stated, provides that the embodiments described in one part, feature, section, or paragraph may be combined with other embodiments described in other parts. It should not be considered to mean distinct or disjoint from one another.

BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings, which are incorporated in and further understood and incorporated into part of this specification, illustrate the disclosed embodiments and the description provided to explain the principles of the disclosed embodiments.
FIG. 1A-1 is a schematic diagram of a conventional fired or supplemental fired oxidizer system for the disposal of a waste stream containing VOCs.
1ab is a schematic diagram of a conventional catalytic oxidizer system.
1ac is a schematic diagram of a conventional oxidizer system including a recuperator.
1ad is a schematic diagram of a conventional regenerative oxidizer system.
1ba is a diagram of the ignition energy of an air-methane mixture.
1bb is a diagram of reaction temperatures of various combustion and oxidation processes.
1C is a diagram of gradual oxidation of a pre-mixed air-fuel mixture in accordance with certain aspects of the present disclosure.
1D is a diagram of gradual oxidation of a fuel mixture when injected into pre-heated air, in accordance with certain aspects of the present disclosure.
1db is a diagram of a gradual oxidation process used to heat an external fluid, in accordance with certain aspects of the present disclosure.
1dc is a diagram of a multistage gradual oxidation process in accordance with certain aspects of the present disclosure.
1E is a flowchart of an exemplary gradual oxidation process of a pre-mixed air-fuel mixture in accordance with certain aspects of the present disclosure.
1F is a flowchart of an exemplary gradual oxidation process of a fuel mixture injected into pre-heated air, in accordance with certain aspects of the present disclosure.
1G is a schematic diagram of an example pre-mixed oxidation system in accordance with certain aspects of the present disclosure.
1H is a schematic diagram of an example implantation gradual oxidation system in accordance with certain aspects of the present disclosure.
1I is a schematic diagram of an example turbine-driven power-generating system, in accordance with certain aspects of the present disclosure.
1J is a schematic diagram of an example turbine-driven power-generating system, in accordance with certain aspects of the present disclosure.
1K is a cutaway view of an exemplary GO reaction chamber with a direct fuel or air-fuel mixture, in accordance with certain aspects of the present disclosure.
1L schematically illustrates a flow through a gradual oxidation system having a sparger, in accordance with certain aspects of the present disclosure.
1M is a schematic diagram of a multistage GO reaction chamber in accordance with certain aspects of the present disclosure.
1N is a schematic representation of a fluidized bed GO reaction chamber in accordance with certain aspects of the present disclosure.
1oa is a schematic representation of a recirculating bed GO reaction chamber in accordance with certain aspects of the present disclosure.
1ob is a schematic representation of another recycle bed GO reaction chamber in accordance with certain aspects of the present disclosure.
1P is a schematic diagram of a GO reaction chamber with flue gas recycle, in accordance with certain aspects of the present disclosure.
1qa and 1qb present a GO reaction chamber with structured reaction elements, in accordance with certain aspects of the present disclosure.
2A is a schematic diagram of an oxidizer coupled to a heat exchanger to provide process heating to an industrial process, in accordance with certain aspects of the present disclosure.
2B is a schematic diagram of an oxidizer coupled to a heating chamber to heat a process material, in accordance with certain aspects of the present disclosure.
2C is a schematic diagram of an oxidizer including an internal heat exchanger through which a process gas passes, in accordance with certain aspects of the present disclosure.
FIG. 2D is a schematic diagram of another embodiment of an oxidizer including a plurality of internal heat exchangers through which a process gas passes, in accordance with certain aspects of the present disclosure. FIG.
FIG. 2E is a schematic diagram of an oxidizer including multiple progressive oxidation zones with adjacent reaction zones in which batches of process material are heated, in accordance with certain aspects of the present disclosure.
FIG. 2F is a schematic diagram of an oxidizer including multiple progressive zones of oxidation with adjacent reaction zones in which continuous flows of process material are heated, in accordance with certain aspects of the present disclosure.
2G and 2GB are perspective and cross-sectional views of exemplary design details of an oxidizer element, in accordance with certain aspects of the present disclosure.
FIG. 2H is a plot of temperatures using the oxidizers of FIGS. 2GA and 2GB, in accordance with certain aspects of the present disclosure.
FIG. 2I is a perspective view of an oxidizer assembly using the oxidizer element of FIGS. 2GA and 2GB, in accordance with certain aspects of the present disclosure. FIG.
3A is a schematic diagram of an example Schnepel cycle power generation system in accordance with certain aspects of the present disclosure.
3B is a conceptual diagram of a power generation system, in accordance with certain aspects of the present disclosure.
3C-3J are schematic diagrams of an exemplary Schnefel cycle power generation system, in accordance with certain aspects of the present disclosure.
4A is a three-step gradual oxidizer fluid heater system in accordance with certain aspects of the present disclosure.
4B is another embodiment of a three-step gradual oxidizer fluid heater system in accordance with certain aspects of the present disclosure.
4C is another embodiment of a single-stage recuperative fluid heating system in accordance with certain aspects of the present disclosure.
4D is another embodiment of a two-stage water-tube type steam generation system in accordance with certain aspects of the present disclosure.
4E is another embodiment of a two-stage fire-tube type fluid heating system in accordance with certain aspects of the present disclosure.
4F schematically illustrates a flow through a gradual oxidation system that generates steam, with a sparger, in accordance with certain aspects of the present disclosure.
5A is a schematic diagram of an example gradual oxidation system that combines steam generation and additional fuel injection, in accordance with certain aspects of the present disclosure.
5B is a schematic diagram of an example gradual oxidation system that combines steam generation and cogeneration, in accordance with certain aspects of the present disclosure.
5C is a schematic diagram of an exemplary gradual oxidation system that incorporates a dual compressor using intercooling, in accordance with certain aspects of the present disclosure.
5D is a schematic diagram of an example gradual oxidation system that incorporates a starter gradual oxidizer, in accordance with certain aspects of the present disclosure.
5E is a schematic diagram of an example gradual oxidation system that mixes multiple points of water injection, in accordance with certain aspects of the present disclosure.
5F is a diagram of typical gas content of the exhaust of various systems.

The following description discloses embodiments of a system for the oxidation of a gas comprising an oxidizable fuel. In certain embodiments, the system gradually oxidizes the fuel while maintaining the temperature in the oxidizer below the burnout temperature so that the formation of unwanted contaminants such as nitrogen oxides (NOx) and carbon monoxide (CO) is significantly limited. And an oxidizer that can be operated to cause. The fuel is preferably introduced into the oxidizer at or near the autoignition temperature of the fuel. The system is specially adapted for the use of fuel having a low energy content, such as a methane content of less than 5%, in a sustainable gradual oxidation process for driving a turbine that not only drives a compressor in the system but also drives a power generator. .

In the following detailed description, numerous specific details are set forth in order to provide an understanding of the present disclosure. However, it will be apparent to one skilled in the art that embodiments of the present disclosure may be practiced without some of the specific details. In other instances, well known structures and techniques have not been shown in detail in order not to obscure the disclosure.

Certain embodiments of the methods and systems disclosed herein are powered using low energy-containing fluids such as methane-containing gas as main fuel and high energy-containing fluids such as natural gas or industrial propane as auxiliary fuels. It is presented against a turbine system that drives a generator. For example, and unless specifically indicated, the application of any of the methods or systems disclosed herein should not be construed as limited to any particular primary or auxiliary fuel or turbine system of this particular arrangement. Other arrangements of turbine-compressor systems known to those skilled in the art can be used, and the components and principles disclosed herein can be applied to these other systems.

Certain embodiments of the methods and systems disclosed herein are presented relative to an oxidizer coupled to a reciprocating-piston system driving a power generator. For example, unless specifically noted, in this disclosure, either in this disclosure, from application to a reciprocating-piston system, or a combination of reciprocating-piston and turbine systems, in connection with a turbine system, such as the use of auxiliary fuel during some of its operation, The application of any method or system disclosed in the description should not be construed as limiting.

The methods and systems disclosed herein are presented in contrast to integrated process equipment that utilizes a GO process separately from or in combination with material processing functions. For example, unless otherwise indicated, the use of auxiliary fuel during some of the operation, either from this disclosure, from application to integrated process equipment, or combinations of one or more of reciprocating-piston systems, turbine systems, and integrated process equipment. As such, the application of any method or system disclosed herein in connection with a turbine system or a reciprocating-piston system should not be construed as limiting.

In this document, the term "NOx" refers to a group of oxides of nitrogen, including nitric oxide and nitrogen dioxide (NO and NO2). There are at least three conventional identified processes for forming NOx. “Thermal NOx” is formed when oxygen and nitrogen present in the combustion air dissociate in the hot zone of the combustion zone and subsequently react to form oxides of nitrogen. "Prompt NOx" is that fuel fragments attack molecular nitrogen to form products such as HCN and N, which are then formed in close proximity to the combustion front as NOx is formed. "Fuel NOx" is formed by nitrogen containing fuel compounds, such as amines and cyano species, when the fuel containing nitrogen is combusted. Diatomic nitrogen (N2) is not considered to be fuel-bound nitrogen that generates fuel NOx.

In this document, the term “flammable” refers to the properties of a substance that causes the substance to burn with oxygen in an exothermic self-sustainable or self-proliferation reaction when the substance and oxygen are present within a defined range of relative amounts. do. This may require an initiation situation, such as sparks or flames, to initiate the exothermic reaction.

In this document, the terms "lower flammability limit" (LFL), often referred to as "lower explosive limit", and the term "upper flammability, often referred to as" upper explosive limit ". limit) "(HFL) refers to the fuel volume concentration at which a flame may be present. Concentrations below LFL or above UFL will not sustain or propagate the flame reaction.

In this document, the term "low-energy-content fuel" (LEC fuel) refers to a gas comprising a combustible gas as the second component and an inert gas as the main component. Non-limiting examples of LEC fuels are methane-containing gases released from landfills or other disposal sites. For example, LEC methane gas typically contains less than about 30% methane, but may contain as low as 1-5% methane.

In this document, the term "high-energy-content fuel" (HEC fuel) refers to a gas comprising combustible gas as its main component. The HEC fuel may contain a second component which is inert, which cannot be naturally mixed with the main component or economically removed. Non-limiting examples of HEC fuels include "commercial propane", whose composition varies locally but typically contains> 85% propane (C3H8), up to 10% propylene, 10% Less than ethane (C2H8), up to 2.5% butane (C4H10), and heavier hydrocarbons, and may contain about 0.01% odorant, typically ethyl mercaptan. A second non-limiting example of HEC fuel is "natural gas," where a typical unrefined composition is as little as 70% methane and a combination of at least 20% ethane, propane and butane, It may also contain smaller amounts of carbon dioxide (CO 2), oxygen (O 2), nitrogen (N 2) and hydrogen sulfide (H 2 S). A third non-limiting example is a landfill gas comprising more than about 50% methane and the remaining CO 2, N 2 and low O 2.

In this document, the term "oxidant" refers to a gas containing enough oxygen to support combustion or oxidation of combustible fuels. Non-limiting examples of oxidants include ambient air.

In this document, the term "diluent" generally refers to an inert gas. Non-limiting examples of diluents are commercial CO 2, N 2 and H 2 O. Diluents may be present in the oxidation product or fuel reactants.

In this document, the term “generally inert” refers to a combustible or oxygen free material or mixture that is sufficient to support combustion or oxidation when mixed with oxygen or fuel when the ignition source is supplied. Used to.

In this document, the term “combustible concentration” refers to the amount of combustible material present in the mixture, where the concentration is typically indicated in terms of the ratio of the combustible material to the total gas in the mixture.

In this document, the term "gradual oxidation" refers to a process in which a material is burned with oxygen in an exothermic reaction while the material remains below a temperature determined during the entire process. A non-limiting example of this determined temperature is 2300 ° F., where oxidation processes staying below this temperature will generally not form significant amounts of NO _X in relation to air pollution control and standards.

In this document, the term "air-fuel mixture" refers to a gaseous mixture comprising a mixture of combustible fuels and oxidants, preferably air. Air-fuel mixtures are generally considered to be homogeneous unless otherwise indicated. In certain atmospheres, LEC or HEC fuel is mixed with ambient air to form an air-fuel mixture. In certain atmospheres, the LEC fuel may contain enough oxygen and fuel to be considered to be an air-fuel mixture without further addition of air or fuel.

In this document, the term “autoignition” refers to the spontaneous ignition of an oxidation or combustion process in a mixture comprising combustible materials and oxidants. The autoignition temperature is the minimum temperature at which an oxidation or combustion process occurs in the absence of an ignition source and may depend on the pressure and / or oxygen and fuel concentration of the mixture.

In this document, the term “autoignition delay time” refers to the amount of time for a mixture at a temperature above the autoignition temperature to oxidize and to release most of its exothermic energy. By way of illustration, methane has an autoignition temperature of about 1000 ° F. As the mixture of methane and air rises to 1000 ° F, they eventually react to produce H2O and CO2. However, if this same mixture reaches a higher temperature, such as 1200 ° F., the ignition delay time will be 2 seconds. When the mixture reaches 1400 ° F., the delay time will be 100 milliseconds. The self-ignition delay time is generally exponentially faster with increasing temperature and is a function of fuel and oxygen concentrations. Self-ignition delay time can be calculated with chemical kinetic software programs that use complex kinetic mechanisms that can include hundreds of reactions and dozens of molecular and radical types.

In this document, the term “premixed” refers to air and combustible materials, such as LEC or, for forming a generally uniform air-fuel mixture before introducing the mixture into the chamber where oxidation or combustion takes place. Refers to the mixing of HEC fuel.

In this document, the term "short residence time" is relatively defined for combustion devices such as conventional combustion engines, gas turbine combustors, reciprocating engines, burners for boilers and the like. In these conventional combustors, the combustion process is typically completed within a time period of less than 1 second, typically less than 100 milliseconds, and may be less than 10 milliseconds. Processes with residence times closer to or greater than 1 second are referred to as having a "long residence time".

In this document, the term “volatile organic compound” (VOC) refers to an organic compound that enters the gas phase when at a temperature in the range of 40 to 120 ° F. and combines with oxygen in an exothermic reaction. Can be. Examples of VOCs include acetone, acrolein, acrylonitrile, allyl alcohol, allyl chloride, benzene, butene-1, chlorobenzene, 1-2 dichloroethane, ethane, ethanol, ethyl acrylate, ethylene, ethyl formate, ethyl Mercaptans, methane, methyl chloride, methyl ethyl ketone, propane, propylene, toluene, triethylamine, vinyl acetate and vinyl chloride.

In this document, the term "maximum reaction temperature" refers to the maximum temperature of the chemical oxidation reaction, which includes heat transfer or loss of work or addition. For example, if heat is removed while the reaction occurs, the maximum reaction temperature will be less than the adiabatic reaction temperature. Similarly, the maximum reaction temperature may be higher than the adiabatic reaction temperature if heat is added.

In this document, the terms "flame strain rate" or "flame stretch" refer to flame front by stretching or curvature that removes heat from the flame front. Refers to coupling of turbulent straining. The high rate of flame stretch can be produced with strong shear layers, and a sufficiently high strain rate can extinguish the flame.

In this document, the term “adiabatic reaction temperature” refers to the temperature resulting from a complete chemical oxidation reaction that occurs without any action, heat transfer or change in kinetic or potential energy. This is often referred to as constant-volume adiabatic reaction temperature.

In this document, the term "flameout temperature" refers to the temperature of a substantially uniformly mixed air-fuel mixture in which no flame propagates through the mixture. In some cases, as illustratively and as presented herein, the burnout temperature may be comparable to the LFL at any particular temperature of the air-fuel mixture.

Gradual oxidation

1ba is a diagram of the ignition energy of an air-methane mixture. The mixture of methane and air is combustible in the range of approximately 5-15 vol% methane. A stoichiometric mixture of methane and air, ie a mixture with exactly enough oxygen to combine with methane, is approximately 9.5% by volume. 1B suggests that the stoichiometric air-fuel mixture 55 requires the least ignition energy and that increased energy is needed at lower and higher methane concentrations to ignite the mixture.

1bb is a diagram of reaction temperatures of various combustion and oxidation processes, as pointed out by system 60. In zone 1, combustion must be propagated by the energy source. As is typical for combustion devices, in the flow source of the mixture, the energy source for stabilizing combustion must be relatively constant over time. This energy source is typically produced by creating hot local pockets of hot combustion products in the recycle zone. These bands are created behind bluff bodies or other geometric features (V-gutter, corner recycling bands). The second method is to swirl a portion of the mixture sufficiently to cause a "vortex breakdown", and a recycle zone is formed inside or after the swirling mixture. These types of flame stabilization techniques are well known in the combustion art. The hot recycle zone serves as a continuous ignition source to keep the pre-mixed fuel and air mixture in zone 1 constant burning.

In zone 2 of FIG. 1bb, even if initiated by a spark or other ignition source, the flame will not propagate through the air-fuel mixture. The uniform air-fuel mixture is so lean that it does not burn. One of the methods of reacting the pre-mixed air-fuel mixture in this zone is to lower the activation energy of the reaction to the catalyst. Another method is to provide a locally richer mixture in the combustion chamber. This locality has a combustible concentration and therefore a reaction temperature consistent with zone 1. This more abundant mixture burns in the combustion chamber to maintain flame, but this does not result in propagation of the reaction into depletion zones in the combustion chamber by flame propagation, and would have to be done using gas mixing techniques.

Zone 1 and Zone 2 are distinguished by lines representing the burnout temperature over the temperature range. One cannot maintain flame at pre-mixed fuel concentrations resulting in adiabatic reaction temperatures below this line. To expand on this, if one starts with a pre-mixed flame in zone 1 and gradually reduces the fuel concentration, the flame temperature-in this case the maximum reaction temperature presented in the Y axis of FIGS. 1 and 2-will decrease. If the temperature approaches the burnout temperature line, the flames will be extinguished.

The uniform air-fuel mixture in zone 3 of FIG. 1bb will self-ignite and react relatively quickly. The challenge of this "flameless combustion" quadrant is to uniformly mix fuel and air and to reach the desired temperature before the air-fuel mixture self-ignites. For example, as indicated by point 62 in zone 1, mixing fuel and air at a temperature below the autoignition limit line, in zone 1 sparks will ignite the mixture still present in any unplanned zone 1 will be. In addition, once the air-fuel mixture is completely mixed at point 62, the air-fuel mixture is heated to point 64, for example by a heat exchanger or other heating method.

The salt free combustion practitioner avoids the challenge of mixing at low temperatures without combustion by mixing hot air and fuel in zone 3. To prevent ignition from occurring before reaching a uniform mixture, self-ignition is delayed by using one of two techniques. One technique is to inject fuel into a mixture of air and recycled flue gas. The flue gas has excess CO 2 and H 2 O, and a reduced amount of O 2, relative to air. The reduced O 2 concentration will retard autoignition, thereby allowing the mixture of fuel and air-combust gas mixtures to reach a generally uniform composition.

The second technique is to attract "flame strain rate" or "flame stretch" to retard autoignition. Strained flames are flames that occur at higher turbulent flows with strong shear layers. They delay the reaction and, in extreme cases, create turbulent-chemical interactions that can extinguish the flame. To operate the flame stretch, fuel is injected into the turbulent air flow. For example, air is released from the nozzle at high speed and fuel is injected into the stream of released air. The air-fuel mixture generally reaches a uniform composition before the flow of the air-fuel mixture becomes non-turbulent, and the flame stretch causes a delay in self-ignition during this mixing period. It is possible to combine the two techniques and inject fuel into a jet of oxidant comprising a mixture of air and recycled flue gas, which delays autoignition of the oxidant-fuel mixture by both a reduction in O2 concentration and flame stretch. This achieves a distributed reaction throughout the chamber.

One aspect of the flame structure in zone 1 is that the oxidation reaction occurs in a relatively narrow reaction zone, referred to as the flame front. In this locality, chemical radicals from heat and flames from the post-combustion zone diffuse molecularly and volatilely in unreacted gases. In zone 2, the reaction occurs locally near the catalyst and is referred to as heterogeneous combustion. Only in zones 3 and 4 can run volume-distributed reactions due to self-ignition initiating the reaction, as opposed to thermal feedback from existing flames.

Zone 4 is a hot zone where the fuel concentration is too low to maintain flame, i.e., below the burnout temperature line, and is high enough to self-ignite. Progressive oxidation is suitable for oxidation of fuels in this zone. Unlike zones 1-2, the reactions in zone 4 can occur relatively uniformly within the total reactor / combustion volume without the “reaction flame forward” being well defined.

1C is a schematic diagram of an example gradual oxidation process in accordance with certain aspects of the present disclosure. 1C shows various zones 72, 74, 75, 76a, 76b and 78 of flame reaction behavior for a uniform air-fuel mixture at a constant pressure. The ordinate is the temperature of the air-fuel mixture and the abscissa is the concentration of the fuel in the air-fuel mixture. As the temperature of the air-fuel mixture increases, the LFL becomes even lower, i.e., there is a further lack of combustible concentrations. As the temperature increases, the UFL becomes higher, ie, the enrichable concentration becomes more abundant. A wider range of combustible concentrations can be seen to be more flammable.

Zone 72 is a zone where the flame does not autoignite, but after the introduction of sufficient energy source the flame propagates through the air-fuel mixture. Although other devices such as glow plugs or ionized plazma may be used, a common form of energy introduction is sparks from spark plugs or igniters.

Zone 74 is below LFL and below autoignition temperature. In this zone, the flame will not propagate through the mixture, even if initiated by sparks.

Band 76 is divided into two bands 76a and 76b to account for the time to complete the reaction. If sparks occur within zone 76a or 76b, the flame will commence and propagate through the air-fuel mixture. Air-fuel mixtures in zones 76a or 76b may also self-ignite, where the energy contained by the air-fuel mixture at these temperatures does not affect the activation energy of the air-fuel mixture as discussed above with respect to FIG. Because it exceeds. The minimum temperature at which the mixture self-ignites, given sufficient time, is known as autoignition temperature (AIT). Zone 76 is bounded by AIT and UFL and LFL, and any mixture having a concentration and temperature combustible within zone 76b or 76a will self-ignite. Combustion of the air-fuel mixture in zone 76a will self-ignite and will react in a shorter timeframe than a short residence time. Air-fuel mixtures at combustible concentrations and temperatures in zone 76b will self-ignite and react, but will react in long residence times and in a consistent timeframe.

In zone 78, sparks or other energy sources will not initiate the flame or propagate the flame through the air-fuel mixture. Allowing enough time to complete the oxidation reaction allows the fuel to oxidize through autoignition. The time for these reactions in zone 78 is consistent with the long residence time.

Band 75 is independent of most combustion devices. Since the combustible composition is so rich, the flame cannot propagate through the air-fuel in zone 75. If the oxidation process is initiated in the portion of zone 75 above the autoignition temperature, there is not enough air present to complete the oxidation of the fuel, and the oxidation process will self-extinguish, so that unburned fuel is exhausted from the combustion device. do.

In certain aspects, the process starting at point 80 heats the air-fuel mixture to a temperature above the autoignition temperature of the air-fuel mixture indicated by point 82. The reaction chamber, such as the reaction chamber 500 of FIG. 1K, oxidizes the air-fuel mixture and indicates maximum reaction with the adiabatic temperature in the reaction chamber, as indicated by the dotted connection points 82 and 84 remaining below the LFL. It is structured to maintain the temperature below the burnout temperature of the air-fuel mixture.

1D is a diagram of the gradual oxidation of a fuel mixture when injected into pre-heated air, in accordance with certain aspects of the present disclosure. In this process, ambient air at point 92 in zone 74 is heated to point 94 in zone 78 by various means (heat exchange, compression). The fuel, which can then be LEC fuel, diluted HEC fuel, or a mixture of HEC and LEC fuels, is added to the hot air, whereby the air-fuel mixture can be moved from point 94 to point 96. This occurs within zone 76a of FIG. 1c where the air-fuel mixture self-ignites, and point 96 is within zone 76a of FIG. As the combustion process proceeds, the temperature of the air-fuel will rise as the concentration of combustible gas drops, and the process will follow the arrow from point 96 to point 98. As point 98 is above the thermal NOx formation temperature, this process will produce a greater amount of NOx than the process that survives below the thermal NOx formation temperature.

However, when a diluent, such as recycled flue gas, is added to the air, the oxygen content of the resulting air-diluent mixture is reduced. In addition, the use of hot recycled flue gas may help to heat the air from point 92 to point 94. The addition of diluents to air, as well as the use of flame stretch mixing techniques, to fuel fuel into the air-diluent mixture, has shown that flammable upper and lower limits are set to UFL (air + diluent + stretch) and LFL (air + Diluent + stretch) to move the tin to the new lines.

In the addition of diluents and the use of flame stretch mixing techniques, point 96 no longer exists in zone 76a, but exists in zone 76b, where the reaction process is delayed longer than in zone 76a. The diluent in the mixture reduces the temperature rise so that the process follows the arrow from point 96 to point 99 and remains below the thermal NOx forming temperature. Thus, the use of diluents can reduce the amount of NOx produced by the combustion / oxidation process.

In certain aspects, the process starting at point 92 heats the air to the temperature indicated by point 97, which is above the autoignition temperature of the target air-fuel mixture. The fuel is then injected into hot air, which causes the air-fuel mixture to move to point 97. The reaction chamber, such as the reaction chamber 500 of FIG. 1K, oxidizes the air-fuel mixture and points the adiabatic temperature in the reaction chamber, as indicated by the dotted connection points 97 and 98 that rapidly transition below LFL. It is structured to maintain above the burnout temperature of and to keep the maximum reaction temperature in the reaction chamber below the burnout temperature of the mixture.

1 db is a diagram 120 of a gradual oxidation process used to heat an external fluid, in accordance with certain aspects of the present disclosure. The ambient air at point 92 is heated to point 94 where fuel is injected into the preheated air, which causes the air-fuel mixture to move to point 96. As the air-fuel mixture is above the autoignition temperature, gradual oxidation begins, and at the same time the air-fuel mixture causes the temperature of the air-fuel mixture to drop as fuel concentration is further reduced to point 122, For example, heat is transferred to an external fluid through the steam coil 5220 of FIG. 5C. Then, the air-fuel mixture is moved away from the external fluid so that the temperature of the air-fuel mixture rises as the fuel concentration continues to decrease, while the fuel concentration continuously oxidizes gradually without losing heat to the external fluid. This moves to the point 124 where the fuel is completely consumed.

1dc is a diagram 130 of a multi-step gradual oxidation process in accordance with certain aspects of the present disclosure. As the fuel is consumed completely, the ambient temperature air-fuel mixture at point 132 is heated to a point 134 above the autoignition temperature so that gradual oxidation begins and the air-fuel mixture proceeds to point 136 as the fuel is consumed completely. . The hot air-diluent mixture passes through a heat exchanger and heat is removed, thereby moving the air-diluent mixture to point 138. Additional fuel is incorporated into the air-diluent mixture, which causes the mixture to move to point 140. A gradual oxidation process is initiated as the mixture is still above the autoignition temperature, which moves along the line to point 142 as the fuel is consumed again completely. It can be seen that the hot air-diluent mixture can be circulated again through the heat exchanger before the point 142-138-140 and as the loop of the point is repeated several times until all the oxygen in the mixture is consumed. In all cases, the peak reaction temperatures are kept below the thermal NOx formation temperature.

1E and 1F are flowcharts of an exemplary gradual oxidation process in accordance with certain aspects of the present disclosure. FIG. 1E discloses a pre-mix process 100 in which the oxidant, diluent and LEC and HEC fuel are mixed and then heated to the autoignition temperature, whereby gradual oxidation of the fuel is initiated. Certain embodiments of the process of FIG. 1E may include only some of the disclosed steps, or may have these steps in a different order than that indicated in FIG. 1E. As one example, most of the complete process begins at step 102 where LEC fuel, such as landfill gas, is provided at step 102.

An oxidant such as air is added to the LEC fuel in step 104. In some aspects, the amount of oxidant added depends on the concentration of combustible gas in the LEC fuel to reach a target concentration of combustible gas in the resulting oxidant-LEC fuel mixture. In some embodiments, the amount of oxidant added depends on the concentration of oxygen in the LEC fuel to reach the minimum concentration of oxygen in the resulting oxidant-LEC fuel mixture. In some aspects, the concentration of combustible gas and / or oxygen in the LEC fuel is measured at least periodically, and the amount of oxidant added in step 104 is adjusted in response to this measurement.

HEC fuel is optionally added in step 106. In some aspects, the amount of HEC fuel added depends on the concentration of combustible gas in the oxidant-LEC fuel mixture to reach a target concentration of combustible gas in the resulting oxidant-LEC-HEC fuel mixture. In some aspects, the concentration of combustible gas in the oxidant-LEC fuel mixture is measured at least periodically, and the amount of HEC fuel added in step 106 is adjusted in response to this measurement.

Step 108 adds a diluent, such as recycled flue gas, to the oxidant-fuel mixture. In certain embodiments, the amount of diluent is adjusted to reach a target concentration of combustible gas in the resulting oxidant-fuel-diluent mixture. In certain embodiments, the recycled flue gas also heats the oxidant-fuel mixture, thereby reducing the amount of heat subsequently added in step 112. In some embodiments, the concentration of combustible gas in the oxidant-fuel mixture is measured at least periodically, and the amount of diluent added in step 108 is adjusted in response to this measurement. Oxidizers, LEC and HEC fuels, and diluents are mixed in a uniform mixture generally in step 110. In certain aspects, incremental mixing occurs after one or more steps 104, 106, and 108. The uniform oxidant-fuel-diluent mixture is heated in step 112 until the temperature of the mixture reaches at least the autoignition temperature of the mixture. The oxidant-fuel-diluent mixture self-ignites in step 114 and is progressively oxidized in step 116 until fuel and oxygen no longer react in the mixture and process 100 is complete.

FIG. 1F discloses a fuel-injection process 150 in which the oxidant and diluent are mixed and then heated to the autoignition temperature whereby a mixture of LEC and HEC fuel is injected and mixed into the oxidant-diluent mixture. Certain embodiments of the process of FIG. 1F may include only some of the disclosed steps, or may have these steps in a different order than that indicated in FIG. 1F. As one example, most complete processes begin at step 104a, where an oxidant is provided. The diluent is added to the oxidant in step 108, mixed in step 110a, and heated in step 112 to at least the autoignition temperature of the target oxidant-diluent-fuel mixture. In some embodiments, the amount of diluent added depends on the concentration of oxygen in the oxidant to reach the target concentration of oxygen in the resulting oxidant-diluent mixture. In certain embodiments, where the diluent is recycled flue gas, the recycled flue gas also heats the oxidant, thereby reducing the amount of heat subsequently added in step 112.

In a parallel process, LEC fuel is provided in step 102, HEC fuel is added in step 106, and mixed in step 110b. In some aspects, the amount of HEC fuel added depends on the concentration of combustible gas in the LEC fuel to reach a target concentration of combustible gas in the resulting LEC-HEC fuel mixture. In some aspects, the concentration of combustible gas in the LEC fuel is measured at least periodically, and the amount of HEC fuel added in step 106 is adjusted in response to this measurement.

The LEC-HEC fuel mixture is injected into the hot oxidant-diluent mixture in step 152 and mixed in step 110c. In certain aspects, the mixing of step 110c comprises providing the oxidant-diluent mixture into the oxidation chamber via a turbulent-induced jet and the fuel mixture is injected into the turbulent oxidant-diluent mixture flow. The oxidant-diluent mixture and the fuel mixture rapidly mix in a turbulent flow in step 110C, then self-ignite in step 114, and gradually in step 116 until the fuel and oxygen in the mixture no longer react. Oxidation, thereby completing the process (150).

1G is a schematic diagram of an example pre-mixed oxidation system 200 in accordance with certain aspects of the present disclosure. LEC fuel is obtained in this embodiment from gas fill 2020 through gas-collection piping system 204 and provided as LEC fuel flow 206a. In certain embodiments, for example, if the methane content of the LEC fuel flow 206a is less than the determined percentage, HEC fuel 210 is added into the mixer 208a and a LEC-HEC fuel mixture 206b is produced. In certain embodiments, for example, if the oxygen content of the LEC-HEC fuel mixture 206b is less than the determined percentage, an oxidant 212, such as air, is added into the mixer 208b and an oxidant-fuel mixture 206c is produced. . In certain embodiments, for example, if the oxygen content of the oxidant-fuel mixture 206c is less than the determined percentage, a diluent 214, such as recycled flue gas, is added into the mixer 208c and the oxidant-diluent-fuel mixture 206d ) Is generated. In certain embodiments, mixer 220 is provided to further mix oxidant-diluent-fuel mixture 206d, resulting in a homogenized oxidant-diluent-fuel mixture 206e. In certain aspects, a compressor or blower 222 is provided to pressurize and heat the homogenized oxidant-diluent-fuel mixture 206e and to be introduced into the oxidizer 224. Diluent-fuel mixture 206f is produced. After the gradual oxidation process is complete, exhaust 226 is discharged from oxidizer 224. In certain aspects, a portion of the exhaust 226 taps off to provide the diluent 214. The remaining exhaust 226 is provided to other systems or vented to the atmosphere.

1H is a schematic diagram of an example implantation gradual oxidation system 300 in accordance with certain aspects of the present disclosure. Many of the elements of system 300 are common to system 200 discussed above, and their description is not repeated with respect to FIG. 1H. In system 300, oxidant 212 is separately compressed and heated with compressor or blower 222a, and the resulting pressurized oxidant 304 is provided to oxidizer 224. In certain embodiments, diluent (not shown in FIG. 1H) is added to oxidant 212 before compressor 222a. Separately, the LEC-HEC fuel mixture 206b is a separate compressor or blower 222b to produce a pressurized fuel mixture 302 that is injected into the pressurized oxidant-diluent mixture 304 within the oxidizer 224. Is compressed and heated. Methods of injecting the fuel mixture 302 into the oxidant-diluent mixture 304 in the oxidizer are discussed in the context of the following figures.

1I is a schematic diagram of an example turbine-driven power-generating system, in accordance with certain aspects of the present disclosure. Many of the elements of system 400 are common to the systems discussed above, and their description is not repeated with respect to FIG. 1I. In system 400, oxidant-diluent-fuel mixture 206d is provided at the inlet of compressor 410 coupled to shaft 412 which is also coupled to turbine 414 and power generator 416. . The oxidant-diluent-fuel mixture 206f pressurized from the compressor 410 passes through a heat exchanger 418, where the mixer 206f absorbs heat from the exhaust 420. The heated mixture 206g is provided to the oxidizer 224. Exhaust 226 is provided to turbine 414 which extracts some of the energy from hot compressed exhaust 226, thereby driving compressor 410 and generator 416 through shaft 412. In certain aspects, a portion of the exhaust from the turbine is taken out to provide the diluent 214, and the remaining exhaust 420 passes through the heat exchanger 418 mentioned above and then passes the second heat exchanger 422. Passes, where the exhaust gas is further cooled by the flow of water 430 before being exhausted to the branch. The heated water 430 may be used for advantageous use such as hot water supply, building, heating or other applications after passing through the heat exchanger 422.

1J is a schematic diagram of an example turbine-driven power-generating system, in accordance with certain aspects of the present disclosure. Many of the elements of system 450 are common to the systems discussed above, and their description is not repeated with respect to FIG. 1J. System 450 includes a warmer combustor 454 and a turbine combustor 456, respectively, before and after oxidizer 224. HEC fuel 452 is optionally provided at each of the heater combustor 454 and turbine combustor 456. A method of initiating the operation of an oxidizer-driven turbine using these combustors 454, 456 is described in the above-referenced US patent application 13 / 289,996.

1K is an interior view of an exemplary GO reaction chamber 500 in accordance with certain aspects of the present disclosure. GO reaction chamber 500 has, in certain embodiments, a vessel 510 that is structured to withstand pressurized internal gas. Tower 514, in this embodiment, is disposed along the central axis of vessel 510 and is configured to receive at the outer end a flow of oxidant-diluent-fuel mixture 530 through inlet 515. Multiple distribution pipes 516 are coupled to tower 514 such that oxidant-diluent-fuel mixture 530 passes from tower to distribution pipe 516. Each distribution pipe 516 includes a number of injection holes (not shown in FIG. 1K) that allow the mixture 530 to pass from the interior of the distribution pipe 516 into the interior of the vessel 510. The interior of the container is at least partially filled with porous medium 512. The medium 512 absorbs heat from the GO process and then releases this heat into the unreacted mixture 530, thereby raising the temperature of the unreacted mixture 530 above the autoignition temperature. Porous medium 512 also functions to mix the products of oxidation from previous steps with an unreacted oxidant-diluent-fuel mixture injected through pipe 516.

In certain aspects, GO reaction chamber 500 includes a sensor 524 that includes a temperature sensing element and outputs a signal representing a temperature within reaction chamber 500. In certain aspects, GO reaction chamber 500 includes a sensor 525 that includes a temperature sensing element and outputs a signal representing the temperature of oxidant-diluent-fuel mixture 530. In certain aspects, the temperature signals from the sensors 524 and 525 are configured to adjust the temperature in the reaction chamber 500 when the temperature in the reaction chamber 500 approaches the burnout temperature so that the temperature remains below the burnout temperature. Is received by a controller 529 that outputs a reducing signal 532. In certain aspects, the adjustment of the temperature in the reaction chamber 500 may include the flow of the oxidant-diluent-fuel mixture 530, the temperature of the oxidant-diluent-fuel mixture 530, the flow of the auxiliary air-fuel mixture 540. , The temperature of the auxiliary air-fuel mixture 540, the flow of exhaust gas through the outlet 520, the flow of coolant through the internal heat exchanger, such as that shown in FIG. 2C (not shown in FIG. 1K), or injection This is accomplished by adjusting one or more of the flow of non-combustible fluid introduced into the reaction chamber 500 through a subsystem (not shown in FIG. 1K). In certain aspects, the signal 532 is provided to a control module 531 structured to control at least one of the flow rate, composition, and temperature of the oxidant-diluent-fuel mixture 530.

In certain aspects, the detection module 527 is such that the reaction temperature in the reaction chamber 500, such as the temperature in the sensor 524, approaches the stoppage temperature of the oxidant-diluent-fuel mixture in the reaction chamber 500 or To detect at least one of above and when the reaction chamber inlet temperature, ie, the temperature of the oxidant-diluent-fuel mixture 530 at the sensor 525 approaches or falls below the autoignition threshold. It is structured.

In certain aspects, the controller 529 is configured to detect at least one of the removal of heat from the reaction chamber or the temperature of the oxidant-diluent-fuel mixture 530 at the inlet of the tower 514 in the reaction chamber. And a calibration module 528 that outputs instructions based on. In certain aspects, the calibration module 528 is structured, for example, in the sensor 524 to maintain the actual temperature in the reaction chamber below the burnout temperature and / or to maintain the inlet temperature above the fuel's self-ignition threshold. have. In certain aspects, the calibration module 529 exceeds the burnout temperature of the oxidant-diluent-fuel mixture 530 at the inlet of the tower 514 for the gas in the reaction chamber 500 to oxidize without catalyst. Structured to maintain. In certain aspects, the controller 529 is configured to reduce the temperature in the reaction chamber remaining below the burnout temperature, and to maintain the temperature of the oxidant-diluent-fuel mixture 530 above the autoignition threshold. And is configured to determine at least one of the increase in temperature of the oxidant-diluent-fuel mixture 530 at the inlet of.

In certain aspects, the controller 529 is configured such that the temperature of the oxidant-diluent-fuel mixture 530 at the inlet of the tower 514 approaches or approaches the autoignition threshold of the oxidant-diluent-fuel mixture 530. When falling below, the temperature of the oxidant-diluent-fuel mixture 530 at the inlet of the tower 514 is maintained above the autoignition threshold and the reaction chamber 500 oxidizes the fuel in the reaction chamber 500 without catalyst. In order to maintain the < Desc / Clms Page number 5 > In certain embodiments, the calibration module 528, based on the detection module 527, is present in the reaction chamber 500 while in the reaction chamber sufficient to self-ignite and oxidize the oxidant-diluent-fuel mixture 530. Change the residence time of the gas in the reaction chamber, for example by reducing the flow of the oxidant-diluent-fuel mixture 530, and / or adjust the autoignition delay time, for example by adjusting the composition of the oxidant-diluent-fuel mixture 530; The heater 522 outputs instructions for changing by increasing the temperature in the reaction chamber 500.

In certain aspects, the detection module 527 is configured to detect when the reaction chamber inlet temperature of the gas approaches or falls below the level so that the reaction chamber alone does not support oxidation of the fuel, The calibration module 528 changes the residence time of the gas in the reaction chamber and / or the self-ignition delay time in the reaction chamber based on the detection module 527 to be sufficient to self-ignite and oxidize while present in the reaction chamber 500. It is structured to be.

In some embodiments, the temperature of the fuel or gas mixture in the reaction chamber may be above the flammable lower limit or the burnout temperature. In these cases, for example when mixing HEC fuel gas into the reaction chamber, there may be a time for the mixture to pass through the flammable region, which is below the flammable upper limit and above the flammable lower limit. The residence time in this zone may in some cases be undesirable to reduce the residence time of the mixture in the zone by changing the temperature of the mixture or by changing the flow of the mixture. In some cases, heat may be drawn from the reaction chamber to reduce the temperature of the mixture below the flammable lower limit or the burnout temperature such that the residence time of the mixture in the combustible region is less than the autoignition delay time. In some cases, the flow rate of the mixture from the reaction chamber can be increased to reduce the residence time of the mixture in the reaction chamber; This reduced residence time of the mixture in the reaction chamber may be equal to the reduced residence time of the mixture exposed to the temperature in the reaction chamber present in the flammable region, and accommodates cases where the residence time is less than the autoignition delay time. . In some cases, heat may be added to the mixture such that the reaction is temporarily shifted into the combustible region for a summarized period of time compared to the autoignition delay time.

In some cases, at least one of the flow or temperature of the mixture through the reaction chamber may be controlled such that the residence time of the fuel in the combustible region is less than about 5% of the autoignition delay time. In some cases, the residence time of the fuel in the combustible region can be from about 5% to about 10% of the autoignition delay time. In some cases, the residence time of the fuel in the combustible region can be from about 10% to about 20% of the autoignition delay time. In some cases, the residence time of the fuel in the combustible region can be from about 15% to about 25% of the autoignition delay time. In some cases, the residence time of the fuel in the combustible region can be from about 25% to about 50% of the autoignition delay time. In some cases, the residence time of the fuel in the combustible region can be from about 30% to about 75% of the autoignition delay time.

In certain aspects, the control module 531 controls the temperature of the oxidant-diluent-fuel mixture 530 to or above the autoignition temperature of the oxidant-diluent-fuel mixture 530 at or before the inlet 515. It is structured to raise as. In certain embodiments, the reaction chamber 500 oxidizes the oxidant-diluent-fuel mixture 530 and maintains the adiabatic temperature above the autoignition temperature of the oxidant-diluent-fuel mixture 530 and the reaction chamber 500. It is configured to maintain the maximum actual temperature below the burnout temperature of the oxidant-diluent-fuel mixture 530.

In certain aspects, the oxidizer 500 may, in a system not shown in FIG. 1K, use a gas with LEC fuel, with all gas present at a temperature below the autoignition temperature of any of the gases being mixed. It is structured to produce an oxidant-diluent-fuel mixture 530 by mixing with one or more of the group consisting of a gas comprising an HEC fuel, a gas comprising an oxidant, and a gas comprising a diluent. The oxidizer 500 is also structured to increase the temperature of the oxidant-diluent-fuel mixture 530 to at least the autoignition temperature of the oxidant-diluent-fuel mixture 530. ) Is allowed to autoignite, the temperature of the oxidant-diluent-fuel mixture 530 is maintained below the burnout temperature as the self-ignited oxidant-diluent-fuel mixture 530 is oxidized.

In certain aspects, the porous medium 512 in the oxidizer 500 is structured to maintain the internal temperature of the reaction chamber below the burnout temperature and the reaction chamber inlet temperature of the fuel above the autoignition temperature of the fuel. . In certain embodiments, at least one of the flow passages from the inlet to the outlet of the oxidizer 500 is at a temperature at which the oxidant-diluent-fuel mixture 530 is above the autoignition temperature of the oxidant-diluent-fuel mixture 530. And is configured to apply to the oxidant-diluent-fuel mixture 530 through a portion of the porous medium 512 that is above the autoignition temperature of the oxidant-diluent-fuel mixture 530 until it is reached. Is added to apply an oxidant-diluent-fuel mixture 530 that oxidizes to the outlet along a passage generally opposite to the first flow passage using, for example, an internal baffle such as the tube 1055/1060 shown in FIG. 2gb. It is structured as

In some embodiments, controller 529 may be applied to other parts of the oxidation system. For example, other controls that may be applied by the controller 529 are described in co-pending US patent application Ser. No. 13 / 289,989, filed Nov. 4, 2011, and in 13 / 289,996, filed Nov. 4, 2011. Both of which are incorporated herein by reference in their entirety to the extent that the teachings in the applications are inconsistent with the teachings of this description.

1L schematically illustrates a flow through a gradual oxidation system 4500 having a sparger, in accordance with certain aspects of the present disclosure. The process and elements of FIG. 1L are described in connection with oxidizer 500 of FIG. 1K. The following processes occur as air 4502 and fuel 4220 flow through the oxidizer.

1. Fuel / air mixer 4510 produces an initial lean air-fuel mixture from one or both of air 4502 and fuel 4220.

2. Heater 4512 heats the air-fuel mixture to a temperature close to the autoignition temperature. In addition, heat may be added through compression of the mixture as well as heat exchange. In some embodiments, heat may be added by introducing a heated gas (eg, flue gas).

3. A first stage gradual oxidizer which may include a heater 522 (FIG. 1K) or a heater 4516 (FIG. 1L), such as a pilot burner, to initiate gradual oxidation 4518. In certain embodiments, the heater is various types of electric heaters known to those skilled in the art. Its output is a hot gas comprising micronized O ₂ and oxidation products CO ₂ and H ₂ O. Since a portion of the fuel and air flowing into this first oxidizer 4518 is small, little heat is required to heat the mixture above the autoignition temperature to initiate the oxidation reaction. In certain embodiments, heat is added to the first stage by preheating the porous medium to the starter-combustor upstream. The preheated medium then heats the fuel / air mixture at 4516 to begin oxidation. Since only a small portion of the flow passes through the medium heated in the heater 4516, the thermal state and energy of the energy opposite to the direction of flow can maintain the medium at a temperature high enough to continuously heat the flow. .

4. As shown by processes 4514, 4520 and 4518, a portion of the air-fuel mixture is split, mixed with hot gas from the previous process, and gradually oxidized, for example sparger 514 of FIG. 1K. Separation-mixing-oxidation step 4530 as occurring in arm 516 of the control. Since the previous oxidized gases from oxidizer 4518 are high temperatures, typically greater than 1400 ° F. and less than 2300 ° F., they heat the unreacted fuel and air from separator 4414 in mixer 4520 and in the next stage of oxidation. Function to initiate oxidation.

5. Repetition of step 4530 oxidizes all fuel from the LEC source 4220 such that no fuel remains after the final oxidizer 4518. Anchoring Initiating the oxidation process in the first step and then a staged-approach to the oxidized portion of the gas is a gradual oxidation process.

1M is a schematic diagram of a multistage GO reaction chamber in accordance with certain aspects of the present disclosure. In this embodiment, the chamber 600 includes four reaction chambers 602a, 602b, 602c and 602d that are coupled together in series. In this embodiment, a flow of air-fuel mixture 604, such as LEC fuel, is provided in each of the four reaction chambers 602a, 602b, 602c and 602d. In certain aspects, the amount of air-fuel mixture 604 provided in the reaction chambers 602a, 602b, 602c and 602d is different. In certain embodiments, one or more different air-fuel mixtures (not shown in FIG. 1L) are provided in downstream reaction chambers 602b, 602c and 602d. In certain embodiments, one or more different air-fuel mixtures (not shown in FIG. 1M) are provided separately in downstream reaction chambers 602b, 602c and 602d. In certain embodiments, HEC fuel (not shown in FIG. 1M) is provided separately in one or more reaction chambers 602a, 602b, 602c and 602d.

FIG. 1N is a schematic diagram of a fluidized bed GO reaction chamber 700 in accordance with certain aspects of the present disclosure. In this embodiment, the reaction chamber 700 includes a vessel 710 at least partially filled with a medium 720, wherein gas is introduced at the bottom of the medium 720 and gradually fluidized. As the mixture 604 passes through the fluidized medium 720, the air-fuel-diluent mixture 604 gradually oxidizes and is removed at the top as the exhaust 226. The fluidized medium circulates in vessel 710 and heat is transferred from the exhaust products of oxidation to the inlet reactant. Fluidized particles 720 near the exhaust end of vessel 710 (close to exhaust 226) are heated by the hot products of oxidation. The fluidized medium is then intentionally or incidentally transferred to the inlet end of the oxidation vessel 710. The heated fluidized medium is then imparted to the cooler unreacted air-fuel-diluent mixture 604 that introduces their heat, thereby heating the flow, as taught for the GO process. Thus, fluidized medium 720 functions to transfer heat from the products of oxidation to air-fuel-diluent reactants. There are several ways to implement a fluidized bed, especially when combined with the staged injection of a GO process to transfer heat to a closed chemical reaction system, and implementing a fluidized bed is one example of how heating is achieved.

1OA is a schematic diagram of a recirculating bed GO reaction chamber 800 in accordance with certain aspects of the present disclosure. In this embodiment, reaction chamber 800 includes a container 810 at least partially filled with medium 820. The portion 810a of the medium 820 is at least periodically removed from the bottom of the vessel 810 and transferred through the delivery system 820 to the top of the vessel 810, whereby the portion 810a is the vessel 810. ) Is recovered inside. At the same time, the flow of the air-fuel mixture 604 is introduced at the bottom of the vessel 810 and passes upward through the medium 820. The mixture 604 gradually oxidizes as it passes through the medium 820 and is removed at the top as the exhaust 226. As the portion 810a is removed at the bottom and the media 820 present in the vessel 810 moves downstream, the hottest medium 820, i.e., the top of the medium 820 within the vessel 810, is removed. Medium 820 moves toward the inlet, thereby counteracting the tendency of the incoming air-fuel mixture 604 to cool the medium 820 locally. The cold medium portion 810a removed from the bottom is delivered to the top where the portion 810a is heated by hot oxidized gas.

FIG. 1ob is a schematic diagram of another recycle bed GO reaction chamber 801 in accordance with certain aspects of the present disclosure. In this embodiment, recycle portion 810b is drawn from the hot portion of layer 820, such as the midpoint at the depth of layer 820, and circulated through pipe 822, from recycle portion 810b. Column 824 is extracted. The cold portion 810b is provided back to the chamber 801, for example at the top, to fall over the top of the layer 820. This extraction of heat from recycle portion 810b draws heat from reaction chamber 801. In certain aspects, the flow rate of portion 810b is controlled to maintain the internal temperature of reaction chamber 801 below the burnout temperature.

1P is a schematic diagram of a GO reaction chamber 850 with flue gas recirculation, in accordance with certain aspects of the present disclosure. Vessel 810 and medium 820 are similar to those of GO oxidizer 800 of FIG. 1O. However, in the embodiment of FIG. 1P, the portion 852 of the exhaust gas 226, also referred to herein as the flue gas, is used to heat and secure the incoming air-fuel mixture 604 in the vessel 810. , As well as to provide additional diluent to the incoming air-fuel mixture 604, is provided at the bottom of the vessel 810.

In certain aspects, GO reaction chamber 850 includes an oxygen sensor, such as sensor 524 of FIG. 1K, which determines a oxygen content level within reaction chamber 850 and provides a signal representative of the oxygen content level. It is structured to provide. In certain embodiments, the controller (not shown in FIG. 1P) accepts an oxygen content level and contains a flue gas 852 that is received from an outlet of the reaction chamber and contains product gases from oxidation of fuel in the reaction chamber. The instructions for introducing into the reaction chamber 850 are output based on the level.

In certain embodiments, the oxidizer has a mixture of at least one of a group of low energy-content (LEC) fuels and high energy-content (HEC) fuels, oxidant-containing (OC) gases and diluent-containing (DC) gases. The reaction chamber inlet may be configured to receive a gas. The gas mixture may be adjusted to be present at a temperature below the autoignition temperature of the gas mixture. The oxidizer may also include a heat exchange medium disposed in the reaction chamber. The medium may be structured to maintain the internal temperature of the reaction chamber below the burnout temperature and the reaction chamber inlet temperature of the fuel above the self-ignition temperature of the fuel. The reaction chamber may provide at least one flow passage from the inlet to the outlet through the chamber. The flow passage may be structured to introduce gas into the inlet through the first passage through the medium that is above the autoignition temperature of the gas mixture until the gas mixture reaches a temperature above the autoignition temperature of the gas mixture, The flow passage is thus further structured to apply a gas mixture to the outlet which oxidizes through the second passage through the medium, the second passage being generally opposed to the first flow passage. Embodiments thereof are illustrated in FIGS. 2ga-2i.

In certain embodiments, the oxidation method disclosed herein is one of a group of low energy-content (LEC) fuels, high energy-content (HEC) fuels, oxidant-containing (OC) gases and diluent-containing (DC) gases. Receiving in the reaction chamber through a chamber inlet structured to receive a gas having a mixture of any of the above, wherein the gas mixture is at a temperature below the autoignition temperature of the gas mixture; A heat exchange medium disposed within the reaction chamber maintains the internal temperature of the reaction chamber below the combustion stop temperature, transfers heat through the heat exchange medium to maintain the reaction chamber inlet temperature of the fuel above the self-ignition temperature of the fuel, Introducing gas into the inlet through the first passage through the medium at a temperature above the autoignition temperature of the gas mixture until the gas mixture reaches a temperature above the autoignition temperature of the gas mixture; And applying gas to the chamber outlet through a second passage through the medium, the second passage generally comprising a step opposite to the first flow passage.

In certain embodiments, the reaction chamber is configured to maintain oxidation of the gas mixture along at least one of the first and second flow passages without a catalyst. In certain embodiments, the reaction chamber is configured to maintain oxidation of the mixture below the stoppage temperature of the gas mixture by circulating a heat exchange medium from the reaction chamber. In certain embodiments, the system further includes at least one of a turbine or a piston engine configured to receive gas from the reaction chamber outlet and expand the gas. In certain embodiments, the gas mixture is hydrogen, methane, ethane, ethylene, natural gas, propane, propylene, propadiene, n-butane, iso-butane, butylene-1, butadiene, iso- At least one of pentane, n-pentane, acetylene, hexane and carbon monoxide.

In certain embodiments, the oxidizers described herein include at least one of a group of low energy-content (LEC) fuels, high energy-content (HEC) fuel gases, oxidant-containing (OC) gases, and diluent-containing (DC) gases. It is structured to receive a gas having one mixture. The gas mixture may be adjusted to be present at a temperature below the autoignition temperature of the gas mixture. The oxidizer is structured to increase the temperature of the gas mixture to at least the autoignition temperature of the gas mixture, thereby self-igniting the gas mixture, and to maintain the temperature of the gas mixture below the burnout temperature while oxidizing the self-ignitioned gas mixture. It may also have a thermal controller.

In some embodiments, a method for oxidizing a fuel described herein includes a gas having a low energy-content (LEC) fuel, a gas comprising a high energy-content (HEC) fuel, a gas comprising an oxidant and a diluent Mixing with one or more of the group of gases, wherein all of the gases are present at a temperature below the autoignition temperature of any of the gases being mixed; Increasing the temperature of the gas mixture to at least the autoignition temperature of the gas mixture and self-igniting the gas mixture; And maintaining the temperature of the gas mixture below the burnout temperature while oxidizing the self-ignited gas mixture.

In certain embodiments, the oxidizer comprises a mixture of at least one of a low energy-content (LEC) fuel and a high energy-content (HEC) fuel, an oxidant-containing (OC) gas and a diluent-containing (DC) gas. It may include an inlet structured to receive the gas having. The gas mixture may be adjusted to be present at a temperature below the autoignition temperature of the gas mixture. The controller (eg, the thermal controller) heats the gas to at least the autoignition temperature of the first gas mixture comprising the gas with an oxidant mixed with the determined range of low energy-content (LEC) fuel and high energy-content (HEC) fuel. Can be structured to The inlet (eg, injector) is also configured to inject a second gas mixture of LEC fuel gas and HEC fuel after the first gas is heated to at least the autoignition temperature of the first gas mixture. The inlet or injector may inject a ratio of LEC and HEC gas at a rate of injection selected to produce a substantially equal proportion of LEC and HEC gas as the first gas mixture when gas is injected into the reaction chamber. The reaction chamber is adapted to mix with the heated gas containing the oxidant to produce a substantially uniform first gas mixture for the second gas mixture and less than the ignition delay time to self-ignite the first gas mixture. And may be configured to maintain the temperature of the first gas mixture below the burnout temperature while oxidizing the self-ignited first gas mixture.

In certain embodiments, the oxidation method described herein comprises at least self-ignition of a first gas mixture comprising a gas with an oxidant mixed with a determined range of low energy-content (LEC) fuel and high energy-content (HEC) fuel. Heating the first gas mixture to a temperature; After heating, injecting a second gas mixture of LEC fuel gas and HEC fuel, wherein the ratio and injection rate of the LEC and HEC gas are substantially the same as when injected into a heated gas comprising an oxidant Selected to generate; At the rate of producing a substantially homogeneous first gas mixture at a time less than the ignition delay time for the second gas mixture while self-igniting the first gas mixture, the injected second gas mixture is heated first with oxidant. Mixing with a gas mixture; And oxidizing the self-ignited first gas mixture while maintaining the temperature of the first gas mixture below the burnout temperature.

1QA and 1QB show a GO reaction chamber 860 with structured reaction elements 864, in accordance with certain aspects of the present disclosure. 1qa is a schematic representation of a vessel 862 containing a stack of structured reaction elements 864 in this embodiment.

1QB shows an example structured reaction element 864 formed as the disk 866 with a number of holes 868 through the thickness of the disk 866. In certain embodiments, the edges of the disk 866 are raised to provide a gap between the stacked elements 864, whereby the air-fuel mixture causes a stack of reaction elements 864. As it passes, lateral flow of the air-fuel mixture is allowed. When stacked in the container 862, the elements 864 are not lined up with the holes 868 of adjacent elements 864, which results in more winding passages through the stack of elements 864. It can be rotated randomly about the center point to provide a serpentine path.

As another example of a structured medium in vessel 862, an extruded metal or ceramic, such as cordierite, functions to conduct heat from the downstream of the flow upstream of the flow in proximity to the exit 226. something to do. This will function to heat the inlet air-fuel mixture 604 above the autoignition temperature and initiate the oxidation reactions.

Gradual oxidizer as heat source

2A is a schematic diagram of an oxidizer 224 coupled to a heat exchanger 1010 to provide process heating to an industrial process, in accordance with certain aspects of the present disclosure. In FIG. 2A, gradual oxidation reactant gases 604 enter the oxidizer 224 and exit as product gas 1015 passing through a heat exchanger 1010 that undergoes gradual oxidation and heat is rejected, and the product gases are At reduced temperature it is exhausted into the atmosphere as exhaust 1030. Entering the other path of the heat exchanger 1010 is a low temperature fluid 1020, such as air, water or industrial fluid, which is advantageously heated and exhausted as a high temperature fluid 1025 flowing to its point of use (in FIG. 2A). Not shown). Heat exchanger 1010 may be co-flow, counterflow, cross-flow, or any of the other heat exchanger specifications described and illustrated herein, or in the art. It may be structured as another that may be known to. The gradual oxidation reaction products 1015 consisting of contaminant-free hot gases are a stream of air to warm a residential space for individual comfort, or a volume of water in a home, or any industrial material that requires heating. Is applied to a heat exchanger which advantageously heats.

2B is a schematic diagram of an oxidizer 224 coupled to a heating chamber 1050 to heat process material 1055, in accordance with certain aspects of the present disclosure. Air-fuel mixture 604 is introduced into oxidizer 224 where it undergoes gradual oxidation and exits as product gas 1015, which is then heated in a heating chamber where material 1055 is advantageously heated by a hot gas ( 1050, the gases are then discharged from the heating chamber as exhaust 1030 and evacuated to the atmosphere. The material 1055 may be processed by one or more of thawing, melting, evaporating, subliming, drying, baking, curing, sintering or calcining using advantageous heat. In a similar embodiment (not shown in FIG. 2B), when sufficient ventilation prevents harmful levels of coral deficiency, hot gradual oxidation reaction products are applied within the occupied space for comfortable heating. In another similar embodiment (not shown in FIG. 2B), hot products are added to an absorption chiller to provide motive energy for the absorption-refrigeration cycle.

FIG. 2C is a schematic diagram of an oxidizer 224 including an internal heat exchanger 1060 through which fluid passes, in accordance with certain aspects of the present disclosure. The heat exchanger 1060 is disposed inside the oxidizer 224 reaction chamber. Air-fuel mixture 604 enters oxidizer 224 and undergoes gradual oxidation. The cold fluid 1020 is introduced into the heat exchanger 1060 and a portion of the thermal energy generated by the gradual oxidation process is transferred to the fluid through the heat exchanger 1060. The cooled product gases exit the exhaust 1030. Hot fluid 1025 flows out of heat exchanger 1060 and is applied at its point of use (not shown in FIG. 2C). An exemplary embodiment of the oxidizer 224 includes a vessel lined with tubes, where air is conveyed through the tubes.

In certain embodiments, heat is drawn from the reaction chamber of the oxidizer 224 using one of the low temperature fluid 1020, which is at least one partially evaporating fluid in the heat exchanger 1060, and the low temperature fluid 1020. Is a gas, or the low temperature fluid 1020 is a fluid whose temperature is increased without evaporation. In certain embodiments, the amount of heat drawn from the reaction chamber of the oxidizer 224 may include controlling the flow rate of the low temperature fluid 1020, controlling the flow rate of the high temperature fluid 1025, or the low temperature fluid 1020. And controlling the temperature of at least one of the hot fluids 1025. In certain aspects, the low temperature fluid 1020 is at a temperature less than the internal temperature in the oxidizer 224, where the reaction chamber has an internal temperature above the autoignition temperature of the fuel in the air-fuel mixture 604 and the air- The fuel mixture 604 is structured to maintain below the combustion stop temperature of the fuel.

2D is a schematic diagram of another embodiment of an oxidizer 224 that includes a number of internal heat exchangers 1060, in accordance with certain aspects of the present disclosure. Similar to FIG. 2C, the air-fuel mixture 604 enters the oxidizer 224, where gradual oxidation occurs, and a portion of the thermal energy is transferred to the low temperature fluid 1020 through the heat exchanger 1070. , Which is disposed inside the gradual oxidizer 224. In certain embodiments, heat exchangers 1060 are heat removal surfaces located proximate to the interior of the outer periphery of the oxidizer vessel to absorb most of the beneficial heat otherwise dissipated into the atmosphere through incomplete wall insulation (FIG. 2D). Not shown).

2E includes a plurality of progressive oxidation zones 1075A-1075C with adjacent reaction zones 1080A-1080C where batches of process material are heated, in accordance with certain aspects of the present disclosure. A schematic diagram of the oxidizer 224. The air-fuel mixture 604 enters the oxidizer 224 in three separate reactant streams 1090A, 1090B and 1090C applied to the gradual oxidation zones 1075A-1075C, where gradual oxidation and gas The release of exothermic energy from is generated. Industrial granular material (not shown in FIG. 2E) is disposed in the reaction zones 1075A-1075C, where they are fluidized by the reaction gases and advantageously heated in a batch manner. The fraction of the heat removal surface is arranged in such a way that it sufficiently absorbs the beneficial heat from the gradual oxidation process to reduce local temperatures below the point where damage to internal components can occur. The product gases from the gradual oxidation process are recombined into a single exhaust stream 1030 which exits to the atmosphere or other end use. In a similar embodiment (not shown in FIG. 2E), to allow the gradual oxidation process to operate at greater energy-release-density without overheating and damaging internal components, thereby allowing a smaller overall reactor volume. ), Additional heat removal surfaces are provided.

FIG. 2F illustrates multiple progressive oxidation zones 1075A − together with adjacent reaction zones 1120A-1120C where continuous flows of process material 1105 are heated, in accordance with certain aspects of the present disclosure. Schematic diagram of oxidizer 224 including 1075C). As in FIG. 2E, the air-fuel mixture 604 is introduced into the oxidizer 224 in three separate reactant streams 1090A, 1090B and 1090C applied to the gradual oxidation zones 1075A-1075C, respectively. Where, after gradual oxidation and release of exothermic energy from the gas occurs, the product gas streams are recombined into a single exhaust 1030 which is discharged to the atmosphere. Low temperature unreacted and granular industrial materials 1105A-1105C are introduced into reaction zones 1120A-1120C, where the materials are fluidized by gradual oxidation reactant gases and in a continuous manner, oxidizer 224 Heated to advantageously modified conditions 1110A-1110C.

On the downstream side of the reaction zones 1120A-1120C, it retains some of the advantageously heated granular materials and allows a balance 1110A-1110C so that the modified materials are collected for later use (Fig. Not shown in 2f) weirs (1085A-1085C) exist. Each of the multiple stages of the gradual oxidation process is independently carried out in the presence of a circulating fluidized bed of granular process material, which causes the material 1105A-1105C itself to dry, cure, sinter, calcination or other thermal due to heat from the progressive oxidizing gases. Simultaneously exchange heat with the gradual oxidizing gases that react while undergoing the induced modification. A circulating fluidized bed process that advantageously alters the granular material can be carried out in a batch or continuous manner in each gradual oxidation step. In a continuous manner, the rate of addition of the low temperature unreacted granule material 1105A-1105C should be small enough so that the gradual oxidation process is not quenched reliably and not digested. In certain embodiments, the mass rate of the low temperature unreacted granule material 1105A-1105C added continuously to the reaction zones 1120A-1120C is gradually introduced into the reaction zones 1120A-1120C. 1-20% of the mass flow rate of oxidizing gases.

2G-2GB are perspective and cross-sectional views of exemplary design details of oxidizer element 1150, in accordance with certain aspects of the present disclosure. After continuous gradual oxidation, at point A, the incoming air-fuel mixture 604 flows through the smaller pipe 1060, flowing out of the oxidizer element 1150 as fully oxidized product gas at point C. Two concentric pipes after entering the inner pipe 1060 and exiting from the inner pipe 1060 at point B and forming a process to back-flow between the inner pipe 1060 and the outer pipe 1055. 1055 and 1060 are used. The air-fuel mixture 604 is heated through the inner pipe 1060 by hot product gas that flows back-out of the pipe 1060.

FIG. 2H is a plot of temperatures using the oxidizers of FIGS. 2GA and 2GB, in accordance with certain aspects of the present disclosure. The mixture begins the flow through the inner pipe 1060 by heat transfer from the hot gas back-flowing between the inner pipe 1060 and the outer pipe 1055 to the temperature T ₂ when the gradual oxidation reaction begins. Is heated during the part. The exothermic release of chemical energy in the gradual oxidation process raises the temperature to T ₃ where most of the reaction has already occurred. The gas then flows into the middle section between the two concentric pipes 1055 and 1060 and flows back counter to the starting flow. The gas temperature may increase slightly due to continuous gradual oxidation, or may decrease as heat is lost to the outer pipe 1055. The gas then maintains movement and exchanges thermal energy with the (cooler) air-fuel mixture 604 entering through the walls of the inner pipe 1060, which cools the product gas to T ₄ .

FIG. 2I is a perspective view of an oxidizer assembly using the oxidizer element of FIGS. 2GA and 2GB, in accordance with certain aspects of the present disclosure. FIG. Assembly 1200 includes a number of elements 1150 disposed in housing 1205, which in this embodiment is a cylindrical container. In certain embodiments, the container 1205 is shaped other than circular. In certain embodiments, the vessel 1205 is pressurized. Two tight cross-sectional plates 1210 and 1220 are disposed across the interior of the vessel 1205. Inner pipes 1160 pass through plate 1210 and outer pipes 1055 are attached to plate 1220. Separate paths 1225 are provided through the plate 1220. The air-fuel mixture 604 flowing through the vessels 1205 passes through the pipes 1060 and 1055 into the inner pipes 1060, respectively, as discussed above with respect to FIGS. 2ga and 2gb, and then through the path. Passes through 1225 to the outside of the outer pipe 1055. As air-fuel mixture 604 is converted to product gas, the mixture runs three times through vessel 1205 of the same length: (1) through inner pipe 1060, (2) inner and outer pipe ( Between 1060 and 1055, and (3) through the volume between the exterior of the outer pipe 1055 and the vessel 1205. This provides additional heat exchange and promotes higher efficiency and smaller volume of oxidizer assembly 1200.

Schnepel Cycles for Reciprocating Engines

FIG. 3A is a schematic diagram of an example Schnefel cycle power generation system 3000, in accordance with certain aspects of the present disclosure. An air-fuel mixture 3005 comprising a mixture of LEC fuel, HEC fuel, oxidant and diluent, as described with reference to air-fuel mixture 206e of FIG. 1G, is found in conventional internal combustion engines with reciprocating cylinders. A compressor cylinder 3010 having a piston 3030a coupled via a connecting rod 3032 to a crankshaft 3034 that is generally similar to a crankshaft. In certain aspects, the compressor cylinder 3010 is part of the drive assembly 3036 as pointed out by the dashed box 3036 as an assembly, generally similar to some of conventional internal combustion engines having reciprocating cylinders. As the piston 3030a descends in the compressor cylinder 3010, the air-fuel mixture 3005 is drawn into the interior space 3015 via a controllable intake valve (not shown in FIG. 3A). When the piston 3030a is close to the bottom of its stroke, the intake valve closes. As the piston 3030a rises, the internal volume 3015 decreases, thereby compressing the air-fuel mixture 3005. When the piston 3030a reaches the designated point, the outlet valve (not shown in FIG. 3A) opens and connects the interior space 3015 to the line 3040, which results in a compressed air-fuel mixture 3005. Is allowed to flow in line 3040. In this embodiment, the compressed air-fuel mixture 3005 passes through the recuperator 3045 and then through line 3050 in heat exchanger 3055, then in line 3060 and oxidizer 224. To pass).

As described above, air-fuel mixture 3005 is gradually oxidized in oxidizer 224 and exits as hot combustion product gas in line 3065. This hot gas is passed to the second side of the heat exchanger 3055, where the hot gas delivers some of its thermal energy to the incoming air-fuel mixture 3050. The product gas then flows through line 3070 into the interior space 3025 of the inflator cylinder 3020.

In operation, the inlet valve (not shown in FIG. 3A) allows the piston 3030a to be top-dead-center so that hot pressurized product gas can flow in the interior space 3025. Open if present at or immediately after it. As the crankshaft 3034 rotates and the piston 3030b descends in the inflator cylinder 3020, the hot pressurized new gas continues to flow into the interior space 3025, thereby internally for the entire stroke. Constant pressure in the space 3025 is maintained.

In certain aspects of operation, the inlet valve closes before the piston 3030b reaches the bottom of its run. As the piston runs from its midpoint to the bottom-dead-center, the gas pressure decreases and cools due to the expanding volumetric cavity.

Compressor cylinder 3010 and inflator cylinder 3020 are coupled to a common crankshaft 3034 and are about 180 ° of rotation of the crankshaft 3034, ie the piston 3030a at the bottom of its stroke. When present, the pistons 3030b are at the top of their stroke, thereby offsetting each other. The air-fuel mixture in the interior space 3025 of the compressor cylinder 3010 while the pressure in the interior space 3025 is at or near the maximum pressure reached at the end of the compression stroke in the compressor cylinder 3010. As 3005 is at atmospheric pressure in this embodiment, there is an unbalanced force for most of the 180 ° of rotation as the piston 3030b descends and the piston 3030a rises. This is an unbalanced force that drives the rotation of the crankshaft 3034. This force also drives the rotation of the generator 416, thereby generating power. In certain aspects, generator 416 generates electricity. In certain aspects, generator 416 generates pressurized fluid or generates mechanical work. As the piston 3030b of the compressor cylinder 3010 reaches the top of its stroke, there is a short period of time where the pressure in the interior space 3015 is approximately equal to the pressure in the interior space 3025. There is no pure driving force during this period, but the inertia of the rotating crankshaft, which may include a flywheel (not shown in FIG. 3A) to provide increased rotational inertia, causes the compressor cylinder 3010 to After the retractor 3045 is attracted in the fresh air-fuel mixture 3005 and the expander cylinder evacuates gas from the interior space 3025 via line 3080, and after the gas is evacuated as exhaust 3085. Will allow the crankshaft to pass through the top-dead-center.

In certain aspects, the drive assembly 3036 is referred to as a split cycle reciprocating engine with an intake to receive the air-fuel mixture 3005, and the compressor cylinder 3010 is a compression chamber coupled to the reciprocating engine. And the interior space 3015 is referred to as a reciprocating piston chamber. In certain aspects, the oxidizer 224 is structured to receive the mixture from the compression chamber through the first inlet and maintain oxidation of the mixture at an internal temperature below the stoppage temperature of the mixture and sufficient to oxidize the mixture without catalyst. It is referred to as an oxidation chamber. In certain aspects, the inflator cylinder 3020 is referred to as an expansion chamber that receives the heated oxidation product gas from the oxidation chamber and expands the product gas within the expansion chamber, thereby driving the reciprocating engine.

3B is a conceptual diagram of a power generation system 3000 in accordance with certain aspects of the present disclosure. Engine assembly 3036 is centrally mounted and oxidizer 224 is attached at one end via recuperator 3045 and heat exchanger 3055. In this embodiment, LEC fuel, such as from remote landfill 202 (not shown in FIG. 3B), is provided via line 3007 and air-fuel mixture 3005 is indicated. Generated from the box.

FIG. 3C is a schematic diagram of an exemplary Schnefel cycle power generation system 3000, in accordance with certain aspects of the present disclosure. Many elements of system 3100 are common to system 3000 and their description is not repeated with respect to FIG. 3C. System 3100 includes a turbine 3110 coupled to a compressor 3105. The compressor 3105 is such that the compression ratio of the piston compressor 3010 is reduced compared to the system 3000 having a compressor 3105 that provides sufficient compression to convert the output from the piston compressor 3010 to the system pressure. It functions in series with the reciprocating piston compressor 3010. In certain aspects, the system pressure of the system 3100 is higher than the system pressure of the system 3000, thereby improving efficiency. The output of the compressor 3105 passes through the heat exchanger 3055 into the oxidizer 224. The output of the oxidizer 224 passes through the turbine 3110 before passing through the heat exchanger 3055 into the piston expander 3020 and then the pressurized gas is exhausted into the atmosphere. The absolute pressure and temperature of the fluid at the various numbered points shown in FIG. 3C in the system 3100 are provided by illustrating in the table below the figure of FIG. 3C.

FIG. 3D is a schematic diagram of an exemplary Schnefel cycle power generation system 3150 in accordance with certain aspects of the present disclosure. Many elements of system 3150 are common to system 3100, and their description is not repeated with respect to FIG. 3D. In this embodiment, the air-fuel mixture 3005 is pressurized by the compressor 3105 and then provided to the piston compressor 3010, which is the reverse of the structure of the system 3100. The absolute pressure and temperature of the fluid at the various numbered points shown in FIG. 3D in the system 3500 are provided in the table below the figure of FIG. 3D.

FIG. 3E is a schematic diagram of an exemplary Schnefel cycle power generation system 3200 in accordance with certain aspects of the present disclosure. Many of the elements of system 3200 are common to the systems provided above, and their description is not repeated with respect to FIG. 3E. In this embodiment, the output from the oxidizer 224 is passed to the piston compressor 3010 and then to the turbine 3110 via the heat exchanger 3055, after which the gas is exhausted.

FIG. 3F is a schematic diagram of an exemplary Schnefel cycle power generation system 3250 in accordance with certain aspects of the present disclosure. Many of the elements of system 3250 are common to the systems provided above, and their description is not repeated with respect to FIG. 3F. In this embodiment, the air-fuel mixture 3005 is compressed in a turbine-driven compressor 3105. Exhaust from oxidizer 224 passes through heat exchanger 3055 followed by piston expander 3020 before passing through turbine 3110 and exhausting.

FIG. 3G is a schematic diagram of an exemplary Schnefel cycle power generation system 3300 in accordance with certain aspects of the present disclosure. Many of the elements of system 3300 are common to the systems provided above, and their description is not repeated with respect to FIG. 3G. This embodiment is similar to the system 3250 except that the output from the oxidizer 224 is provided to the piston expander 3020 and then passes to the heat exchanger 3055.

FIG. 3H is a schematic diagram of an exemplary Schnefel cycle power generation system 3350 in accordance with certain aspects of the present disclosure. Many of the elements of system 3350 are common to the systems provided above, and their description is not repeated with respect to FIG. 3H. This embodiment, except that the output from the oxidizer 224 is provided to the heat exchanger 3055 before reaching the piston expander 3020, and then after passing through the turbine 3110, the gas is evacuated. Is similar to the system 3250.

FIG. 3I is a schematic diagram of an exemplary Schnefel cycle power generation system 3400 in accordance with certain aspects of the present disclosure. Many of the elements of system 3400 are common to the systems provided above, and their description is not repeated with respect to FIG. 3I. This embodiment, except that the output from the oxidizer 224 is provided to the heat exchanger 3055 before reaching the piston expander 3020, and then after passing through the turbine 3110, the gas is evacuated. Is similar to the system 3200.

FIG. 3J is a schematic diagram of an exemplary Schnefel cycle power generation system 3450 in accordance with certain aspects of the present disclosure. Many of the elements of system 3450 are common to the systems provided above, and their description is not repeated with respect to FIG. 3J. This embodiment, except that the output from the oxidizer 224 is provided to the heat exchanger 3055 before reaching the turbine 3110, and then after passing through the piston expander 3020, the gas is evacuated. Is similar to the system 3200.

Process Equipment Using Progressive Oxidation

4A is a schematic diagram of a three-step gradual oxidizer fluid heater system 4000 in accordance with certain aspects of the present disclosure. The pre-mixed air-fuel mixture 4005 is provided to a series of three oxidizers 4010a, 4010b and 4010c. In certain aspects, the three oxidizers 4010a, 4010b and 4010c are substantially the same. Air-fuel mixture 4005 is introduced into first oxidizer 4010a where fuel is consumed by a portion of oxygen in the air and hot combustion products 4035a are produced. Product 4035a lacks a fuel to oxidizer ratio, i.e., depending on the excess air, contains oxygen. Hot combustion product 4035a is applied through a first fluid heat exchanger 4020a where heat is transferred from the hot combustion product 4035a to the heat transfer fluid, in this embodiment water 430, which is more hot. As a fluid, it flows out as steam 4040 in this embodiment. In certain aspects, a heat transfer fluid, such as oil or gas, is provided in place of water 430 and the output is a hot heat transfer fluid.

In certain aspects, the first oxidizer 4010a is configured to maintain the first internal temperature within the first reaction chamber below the stoppage temperature of the first fuel, while the first fuel, i.e., air, in the first reaction chamber without catalyst is present. It is referred to as a first reaction chamber that is structured to maintain gradual oxidation of the fuel component of the fuel mixture 4005.

The product gas 4035a then passes into the second oxidizer 4010b and mixes with the LEC fuel 4007. In certain aspects, LEC fuel 4007 is mixed with one of an oxidant, diluent or flue gas, and HEC fuel (not shown in FIG. 4A) before being provided to oxidizer 4010b. The fuel of the resulting mixture is consumed by the portion of oxygen in the mixture and hot combustion products 4035b are produced. Hot combustion product 4035b is applied in a second fluid heater 4020b where heat is transferred from the hot combustion product 4035b to a separate flow of water 430 that exits as steam 4040, which is the first Mixed with steam 4040 from heat exchanger 4020a.

In certain aspects, the second oxidizer 4010b is configured to maintain gradual oxidation of the second fuel, ie, the remaining fuel in the hot combustion product 4035a and the newly introduced LEC fuel 4007 in a gradual oxidation process without catalyst. It is referred to as a structured second reaction chamber. In certain aspects, the second oxidizer 4010b includes an oxygen sensor (not shown in FIG. 4A) coupled to the processor that is part of the controller (not shown in FIG. 4A), where the processor is It is structured to determine the oxygen content level.

Product gas 4035b or flue gas is then passed into third oxidizer 4010c and mixed with additional LEC fuel 4007. In certain aspects, LEC fuel 4007 provided to oxidizer 4010c is one of an oxidant, diluent or flue gas, and HEC fuel (not shown in FIG. 4A) prior to being provided to oxidizer 4010c. Mixed with In certain aspects, the air-fuel mixture provided to oxidizer 4010c is different from the air-fuel mixture provided to oxidizer 4010b. The fuel of the mixture produced in the oxidizer 4010c is consumed by the portion of oxygen in the mixture, producing a hot combustion product 4035c. These hot combustion products 4035c are applied in a third fluid heat exchanger 4020c where heat is transferred from the hot combustion products 4035c to a separate flow of water 430 that exits as steam 4040, which is Mixed with steam 4040 from first and second heat exchangers 4020a and 4020b.

Multiple steps of gradual oxidation, heat transfer to a fluid that reduces gas temperature, and introduction of new fuel (FIG. 4A) thermally modulate the gas temperature while reducing the amount of oxygen exhausting from the hot combustion product 4035c. It can be used to limit below the NOx temperature threshold. The high efficiency, measured by the amount of energy transferred from the fuels 4005 and 4007 to the steam 4040, is such that the oxygen content exiting the system 4000 through the hot combustion product 4035c is as low as possible, typically from 3 to 5 Provided by volume%. This also provides for the outgoing hot combustion product 4035c to be as cold as possible. If we want to oxidize the fuel in one step, the fuel to air ratio will approach the stoichiometric value, which yields a high temperature. For example, the adiabatic reaction temperature of methane in stoichiometric distribution is 3484 ° F., which is significantly higher than the threshold of 2300 ° F. for the formation of thermal NOx. The staged process of FIG. 4A allows three oxidizers so that more fuel can be introduced and oxidized and most of the oxygen can be removed from the system in the formation of H ₂ O and CO ₂ without producing high temperature and thermal NOx. Various gas flows 4035a, 4035b, 4035c from 4010a, 4010b, and 4010c are cooled.

Other structuring of the fluid flow from the input source, output from water 430 in this embodiment, and steam 4040 in this embodiment will be apparent to those skilled in the art. System 4000 may have fewer or more oxidizers and heat exchangers. One or more heat exchangers 4020a, 4020b, etc. may be connected in series to increase the temperature of the output fluid. The air-fuel mixture provided in each of the oxidizers 4010a, 4010b, etc. may be different and adjustable in response to the measurement of oxygen in the combustion product flows 4035a, 4035b, and the like.

The gradual oxidizer fluid heater arrangement 4000 promotes efficient oxidation of fuel and air and capture of thermal energy by the fluid in three steps. The first step includes a first gradual oxidizer that enables gradual oxidation of the fuel and produces a high temperature low emission product gas stream applied within the first fluid heater, wherein the first fluid stream is advantageously heated. In order to reduce or eliminate the flashback and explosion propensity of the fuel 4005 entering the first stage oxidizer 4010a, the concentration of fuel in the air-fuel mixture 4005 limits the lower flammability of the fuel. Limited to about 20-90% of the concentration. In certain embodiments, it is desirable to limit the fuel content to 25-50%. In certain aspects, there may be applicable fire safety standards that limit the acceptable fuel concentration of the air-fuel mixture 4005.

After oxidation of the fuel in the first oxidizer 4010a, the product gas 4035a contains about 11-19% oxygen, as well as carbon dioxide and water vapor, at a temperature of approximately 1500-2300 ° F. In certain aspects, the oxidation process is controlled such that the temperature of the product gas 4035a is between 1600 and 2000 ° F. After transferring a portion of its heat to the heat transfer fluid, product gas 4035a is present at a temperature between 700 and 1300 ° F, more preferably between 900 and 1200 ° F. At this reduced temperature, the fuel stream 4007 can be blended into the product gas 4035a without undergoing an incremental reaction, which can occur at or above 1400 ° F. Nevertheless, the temperature of the mixed product gas 4035a and fuel 4007 is high enough to initiate oxidation reactions after an ignition delay of 0.01 to 5 seconds. In certain aspects, the ignition delay is 0.1 to 0.5 seconds.

After the ignition delay occurs, the mixture will enter the second oxidizer 4010b, which is the preferred location for efficient oxidation of the fuel that occurs. The second oxidizer 4010b produces a hot product gas stream 4035b having 2-16% oxygen at a temperature applied within the second fluid heater 4020b, preferably at a temperature of 1600-2000 ° F., and thermal Part of the energy is transferred to the heat transfer fluid. The temperature of product gas 4035b is then reduced to 900-1200 ° F., and a second stream of LEC fuel 4007 is blended in product gas 4035b without premature reaction. The mixture of fuel 4007 and product gas 4035b flows into third oxidizer 4010c, where the oxidation process is repeated, producing exhaust gas 4035c with 1.5-14% oxygen. In certain aspects, it may be combined between two and six stages of gradual oxidation followed by fluid heating, with the ultimate goal of producing a final product gas stream having a temperature of 1.5-5% oxygen and a temperature of approximately 150-700 ° F. Let's do it. In certain embodiments, the temperature of the final product gas stream is approximately 250 to 400 ° F. The heated fluid streams may be combined together as shown in FIG. 4A, or may remain remote.

4B is another embodiment of a three-step gradual oxidizer fluid heater system 4100 in accordance with certain aspects of the present disclosure. Air-fuel mixture 4005 is introduced into first oxidizer 4110a, where fuel is consumed by the portion of oxygen in air-fuel mixture 4005, passes through first steam coil 4120a and Boil stream 4130 to produce heat that produces saturated steam 4105. Cooled product gases 4035a flow out of the first oxidizer 4110a and are mixed with additional LEC or HEC fuel and diluent 4007, so that the mixture enters the second gradual oxidizer 4110b. . Similar to the reaction in the first oxidizer 4110a, the fuel in the fuel-generating gas mixture is consumed by the portion of heat in the mixture, passes through the first steam coil 4120b and boils the stream 4130 of liquid water. To generate heat to produce saturated steam 4105. Cooled gases 4035b flow out of the second oxidizer 4110b and are mixed with additional fuel 4007, whereby the mixture enters the third oxidizer 4110c, where the process repeats, Liquid water 4130 is heated in third steam coil 4120c to produce saturated steam 4105.

It will be apparent to those skilled in the art that the fluid heating system 4100 can be used with various heat transfer fluids. For example, the oil may be used to absorb heat therefrom within one or more oxidizers 4110A, 4110b, and the like. Separate flows of various types of heat exchange fluids may be provided separately to one or more oxidizers 4110a, 4110b, etc., and may be provided for separate use by external systems (not shown in FIG. 4b). have. In certain aspects, one or more oxidizers 4120A, 4120B, and the like may be connected in series.

Partially-cooled product gases 4035c are applied in an economizer 4140, where allowable heat in product gases 4035c is applied to the subcooled liquid water stream 4150. The temperature is raised to a temperature slightly below the saturation temperature of the water. The cooled product gases 4035d are exhausted into the atmosphere.

Although similar to the more general fluid heater of FIG. 4A, one of the distinguishing features of system 4100 is the installation of a fluid heating element, ie a steam coil, into the same unit as a gradual oxidizer. Preferred temperatures have the same range as in the previous embodiment, and the oxygen level at the outlet of each step is the same as in the previous embodiment. The final heat recovery unit, or economizer 4140, is added to the tail end of the product gas stream to extract as much heat as possible from the gases before venting to the atmosphere. Steam coils 4120a, 4120b, 4120c may be implemented in the porous ceramic layer of oxidizers 4110a, 4110b, 4110c, or may be suspended below the top of the layer. In certain embodiments, an additional layer height or porous partial radioactive shield is used to help ensure that gases are not quenched by the relatively cold surfaces of the steam coils 4120a, 4120b, 4120c before the gradual oxidation reactions are completed. It can be added between the gradual oxidation zone and the steam generation zone.

4C is another embodiment of a single-stage recuperative fluid heating system 4200 in accordance with certain aspects of the present disclosure. Air 4210 is applied within the cold side of recuperator 3045, where it receives heat and is preliminary in combination with reduced-oxygen recycled product gases 4225 that are added to LEC fuel 4220. It exits as a heated air stream. In certain aspects, LEC fuel 4220 comprises HEC fuel. In certain aspects, the LEC or HEC fuel may be mixed with air 4210 before entering the recuperator 3045.

The air-fuel diluent mixture enters the oxidizer 224 where fuel is consumed by the portion of oxygen and the heat generated.

Liquid water stream 4230 is heated in economizer 3055 to produce a hot water stream that is applied to steam coil 4240. A portion of the heat from the oxidation process is transferred into the hot water through the steam coil 4240, which results in steam 4242 for advantageous use. The partially-cooled product gases exit the oxidizer 224 and are separated into two steams. A portion of the product gases is applied through recycle blower 4245, where the product gases exit at slightly higher pressures and are combined with the air-fuel stream as previously described. The remaining portion of the product gases passes through the economizer 3055 where more heat is removed, thereby cooling the product gases after the inlet water 4230 is heated to the hot side of the recuperator 3045. And additional heat is removed, whereby the incoming air 4210 is heated before the fully-cooled product gases are discharged into the atmosphere.

The system maintains the oxygen concentration of the mixture entering the oxidizer 224 through recycle of the product gases 4225 to less than 12%, preferably less than 9% by flashback of the pre-mixed air-fuel mixture. Suppress the explosion. Recirculation is provided in the range of 700 to 1300 ° F, preferably 900 to 1200 ° F, relative to the oxidizer inlet temperature. Through recycling, this embodiment also generates a total hot gas flow rate through the oxidizer at 1.5 to 4.0 times, preferably 2.0 to 3.0 times the exhaust flow. Higher air temperature gas flow rates allow for the installation of more heat transfer surface area in the oxidizer 224 and the generation of higher amounts of steam. The specific heat (c _p ) of the gas stream carrying out the heat transfer to the steam coil is also higher than the specific heat of the oxidation products with less CO ₂ , less H ₂ O and more O ₂ . Higher specific heat leads to higher potential for heat transfer with a fixed temperature difference between the cold and hot streams.

System 4200 employs an economizer 3055 that recovers heat from the product gas stream by raising water 4230 to just below its boiling point. The system 4200 also incorporates a recuperator 3045 that recovers additional heat by preheating combustion air before it enters the oxidizer 224. This recuperator 3045 reduces or eliminates the amount of auxiliary heat added to initiate a gradual oxidation process in oxidizer 224 and also reduces the loss of heat in the exhaust.

4D is another embodiment of a two-stage water-tube type steam generation system 4300 in accordance with certain aspects of the present disclosure. Air-fuel mixture 4005 is provided at the bottom inlet of oxidizer 4321. The air-fuel mixture 4005 flows through a sparger tree 4322 and enters the porous medium 512 where gradual oxidation occurs and all fuel is consumed by the portion of oxygen. A portion 4315 of the hot product flue gas exits the layer 512 and passes through the steam coil 4325, where heat is removed from the gas, and a smaller portion 4314 of the hot gas passes through the core zone, No steam coils are placed here and no heat is removed. The first steam coil 4325 is arranged around the outer periphery of the enclosure such that the product gases 4314 flowing upward relative to the central axis of the enclosure remain at a high temperature and occur only in the upper section. It will function as an ignition source for the step gradual oxidation.

Additional LEC fuel or HEC fuel is injected into the middle zone of the oxidizer 4321 and mixed with the product gases 4315, through a number of horizontal spokes that penetrate the walls of the cone 4324. An oxidant-diluent-fuel mixture 4316 is introduced into the inverted sparger cone 4324. These spokes have multiple injection holes to distribute the mixture 4316 in an almost uniform manner. The hot gas portion 4314 flows into the sparger cone 4324 inverted through the opening at the bottom and functions to initiate gradual oxidation of the mixture stream 4316, thereby consuming additional fuel and reducing-oxygen high temperature. Product stream 4317 is generated.

Product stream 4317 is applied through steam coil 4326, where heat is removed from product stream 4317 and then exits from oxidizer 4321 as cooled product gases 4318. Water 4335 is contained in each steam coil 4325 and 4326 in a nearly saturated state and flows out as a saturated steam stream 4354. The two stage water tube gradual oxidizer steam generator 4300 is arranged in a single enclosure and is equipped with means for reducing the gas pressure drop in the second stage. The vertical enclosure is mixed with a first gradual oxidizer for oxidizing fuel and producing a hot product gas stream, followed by a first set of steam coils (water tube) to remove heat from the product stream. .

The amount of water or steam applied to the final coil 4326 may be higher than the previous steps to remove as much heat as possible from the gas flow 4317 before exiting to the atmosphere as exhaust 4318. While it is desirable to maintain the product gas temperature above 900 ° F as it exits from the main or intermediate steps 4316, dropping below 900 ° F is a multistage since there is no subsequent gradual oxidizer requiring a temperature above 900 ° F. This is not a consideration at the end of the system. The steam generating surface area and / or any economizer surface area may be as large as required to achieve the purpose of heat removal in the final step.

4E is another embodiment of a two-stage fire-tube type fluid heating system 4400 in accordance with certain aspects of the present disclosure. The air-fuel mixture 4005 enters the bottom zone of the sparger tree 4422. Air-fuel mixture 4005 flows through sparger tree 4422 and enters a layer of porous ceramic 512 in which gradual oxidation occurs and all fuel is consumed by portions of oxygen. The hot product gas 4319 exits the porous medium 512 and flows into the plumbing 4425 where heat is removed from the gas by the surrounding water 4451.

Additional LEC or HEC fuel 4220 and optionally diluent (not shown) are mixed with the cooled product stream 4319 to form an oxidant-diluent-fuel mixture, which is a second sparger 4462 and Contained within a second layer of porous medium 512, where additional fuel is consumed, reduced-oxygen hot product stream 4415 is generated, and heat is removed by ambient water 4451. Is applied through. Cooled product gases 4415 are collected at plenum 4430 and exit from the oxidizer as cooled exhaust stream 4417. The two gradual oxidation zones have insulated walls 4424 and 4428 to prevent excessive cooling of the reactant gases leading to unwanted quenching of the gradual oxidation reactions. Water 4451 is contained within the gradual oxidizer enclosure 4401 in the subcooled or near-saturated states and exits as saturated steam 4452. In certain aspects, additional heating surfaces are added to superheat steam 4452 to a temperature substantially above its boiling point. In certain aspects, water 4451 is pressurized, leading to a higher saturated steam temperature.

By reducing the oxygen in the final exhaust gas stream by 1.5-5.0% while reducing the effluent gas temperature to 250-400 ° F., all cycle efficiencies are estimated to be 85-90%, which is typically operated at 80-86% cycle efficiency. Improved over the steam generator. Increased cycle efficacy corresponds to reduced fuel use for the same useful heat output.

By maintaining gradual oxidation temperatures below about 2300 ° F., preferably below 2000 ° F., the formation of thermal NOx is reduced. Conventional burners have a flame with a maximum reaction temperature in excess of 2300 ° F. and generate substantially more NOx than a gradual oxidation process.

In certain embodiments, the electrical heating elements (not shown in FIG. 4E) may be used to initiate oxidation of the air-fuel mixture 4005 or the oxidant-diluent-fuel mixture at that location. Disposed at one or both inlets.

In certain embodiments, the porous ceramic medium 512 is reduced or absent in an amount and the reaction temperature is allowed higher in the open volume. Moreover, once the polymorphic medium is removed, a larger fraction of the total flow can be distributed to the final sparger 4462.

In certain aspects, the internal pressure is kept low enough that fuel can be added at each stage using only line pressure, ie without a gas pressure booster.

In certain embodiments, an economizer or recuperator (not shown in FIG. 4D or 4E) is added to condense the humidity of the combustion from the product gases or alternatively to leave water in the vapor phase.

In certain aspects, a fluidized bed (not shown in FIG. 4D or 4E) similar to the system shown in FIG. 1M may be used to promote thermal feedback and ignition in the oxidizers 4321 and 4401 as well as for the steam coil. Replace porous medium 512 to improve heat transfer. Other options include flue gas recirculation and structured medium similar to the system shown in FIGS. 1O and 1 Pa / 1Pb.

4F schematically illustrates a flow through a gradual oxidation system 4600 with a sparger, in accordance with certain aspects of the present disclosure. The processes and elements of FIG. 4F are described with respect to system 4500 of FIG. 1L where steps 1-6 are achieved, which is shown to accept the output from point A of system 4500. In certain aspects, air 4602 and fuel 4220 are mixed for example with a mixer similar to mixer 4510 of system 4500 and provided in place of point A in FIG. 4F. The gas mixture entering from point A undergoes the following process steps.

7. The hot gas leaving from the lower section is divided into portions 4315 and 4314, where portion 4315 passes through a heat exchanger, such as coil 4325 of FIG. 4D, and a portion of heat extracted from the hot gas, This cools the gas to a temperature close to the autoignition temperature. This step uses the extracted heat to generate steam or to vaporize other liquids.

8. In this embodiment, fuel 422 is injected into both streams 4314 and 4315. Portion 4314 is hot enough to initiate gradual oxidation in the portions that are mixed at each step 4630.

Hybrid cycle and gradual oxidation

5A is a schematic diagram of an example gradual oxidation system 5100 that mixes steam generation and additional fuel injection, in accordance with certain aspects of the present disclosure. Compressor 410 is coupled to a shaft further coupled to turbine 414 and power generator 416, as shown above in FIG. 1I. The air-fuel mixture 5102 is provided to a compressor 410 that provides a pressurized air-fuel mixture 206f to a heat exchanger 418 that heats the mixture 206f with heat from the turbine exhaust 420. Hot pressurized mixture 206g is conveyed in oxidizer 224. In certain aspects, additional air-fuel mixture 5104 is injected into the oxidizer. In certain aspects, the air-fuel mixture 5104 includes only LEC or HEC fuel. Air-fuel mixtures 206g and 5104 are gradually oxidized in oxidizer 224 and hot flue gas 226 is exhausted to turbine 414. As it passes through the turbine, energy is extracted from the hot flue gas 226 and the cooled and expanded turbine exhaust 420 passes back to the heat exchanger 418. After passing through the heat exchanger 418, the flue gas 420 may still contain free oxygen. Additional air-fuel mixture 5112 is injected into flue gas 420 in duct burner 5110 to reheat the flue gas to produce hot flue gas 5111, which then passes through heat exchanger 422, Here heat is transferred from hot flue gas 5111 to water 430, which results in steam 5108 being provided for end use (not shown in FIG. 5A). The cooled flue gas is then exhausted as an exhaust stream 5106 to the atmosphere. In certain aspects, the air-fuel mixture 5102 only includes air and fuel is provided from the air-fuel mixture 5104.

5B is a schematic diagram of an example gradual oxidation system 5200 that mixes steam generation and cogeneration in accordance with certain aspects of the present disclosure. Many elements of system 5200 are common to system 5100 discussed above, and their description is not repeated with respect to FIG. 5B. In system 5200, steam-generating coil 5220 is embedded in oxidizer 224. Extraction of heat from the oxidation process in oxidizer 224 reduces the maximum reaction temperature, thereby reducing NOx formation while generating steam 5204. Air-fuel mixture 5104 is then injected into the cooled gas in oxidizer 224, which is "downstream" of coil 5220, so that additional combustion is carried out in exhaust 226 into turbine 414. Is allowed to reduce the oxygen level. This injection of additional fuel and additional combustion that reduces oxygen in the exhaust 226 increases the mass flow through the turbine 414, increases the specific heat of the exhaust gas 226, reduces the proportion of specific heat, and thus This increases the power output of the turbine 414. System 5200 removes duct burner 5110 and still generates steam from coil 5220. As coils 5220 operate at the peak temperature of system 5200, steam 5204 will be at a higher temperature or pressure than steam 5108 generated in system 5100.

In certain aspects, steam 5230 is injected into a working fluid in oxidizer 224. Injection of steam in the gradual oxidation process in oxidizer 224 helps to reduce emissions while burning at stoichiometric-near air-fuel ratios. In certain embodiments, the injection of steam 5230 is closer to the stoichiometric ratio without the pre-mixed air-fuel mixture 206a exceeding the flammability range of the air-fuel mixture 206a due to the inert water vapor present. Allow. In certain aspects, steam is injected in a manner that creates a vortex flow pattern in the oxidizer 224 that further assists in a gradual oxidation process. In certain aspects, steam 5230 is introduced through an axial pipe (not shown in FIG. 5B) with radioactive holes and disposed around the periphery of oxidizer 224. In certain aspects, steam 5204 from coil 5220 is recovered as steam 5230, and if steam 5204 is equal to or higher than the pressure in oxidizer 224, steam 5230 is There is less parasitic energy loss because it is already pressurized.

FIG. 5C is a schematic diagram of an exemplary gradual oxidation system 5300 that utilizes dual compressors 410, 5308 using intercooling, in accordance with certain aspects of the present disclosure. Many elements of system 5300 are common to the systems 5100 and 5200 discussed above, and their description is not repeated with respect to FIG. 5C. The use of an intercooler 5304 allows for higher total compression across the compressors 410 and 5308, thereby improving the efficiency of the system 5300. The intercooler 5304 cools the steam 5302 that is further extruded by 5308. Lower temperatures into the compressor 5308 reduce the amount of thermodynamic work, ie the power used to compress the gas. The intercooler allows the flow at 5310 to be present at a lower temperature than is present without the intercooler 5304. This allows more thermal energy to be recovered at the recuperator 418. The amount of energy recovered from the recuperator 418 is proportional to the temperature difference between the turbine exhaust 420 and the recuperator inlet temperature 5210.

5D is a schematic diagram of an exemplary gradual oxidation system that incorporates a starter gradual oxidizer, in accordance with certain aspects of the present disclosure. Many elements of system 5400 are common to systems 5100, 5200, and 5300 discussed above, and their description is not repeated with respect to FIG. 5D. Air-fuel mixture 5102 is provided at the inlet of oxidizer 224 as a flow of warmed and compressed air-fuel mixture 5408. The use of starter oxidizer 5520 allows the main oxidizer 224 to be warmed up to the working temperature, i.e., with reduced amount of NOx formation compared to using a conventional combustor that burns HEC fuel in an open flame. Allowed above the autoignition temperature of the compressed air-fuel mixture 5408 (eg, FIG. 1J). Starter oxidizer 5420 is provided with a supply of air-fuel mixture 5428, and in certain embodiments is pressurized with blower 5542. Hot combustion product gases, such as flue gas, are provided from the outlet of starter oxidizer 5520 to the inlet above oxidizer 224. In certain embodiments, flue gas from starter oxidizer 5520 is introduced into oxidizer 224 through the same inlet as warmed and compressed air-fuel mixture 5408. The valve 5526 is provided to shut off this starting subsystem when the main oxidizer 224 reaches operating temperature and the compressor / turbine 410/414 subsystem starts. In system 5400, filters 5402 and 5424 are provided to remove certain and other unwanted components from each air-fuel mixture 5102 and 5428.

Advantages of using the starter gradual oxidizer of FIG. 5D include a reduction in the release of reference contaminants such as NOx during the start of the system. It also allows the use of native LEC gas at sites other than maintaining a separate HEC supply of fuel for the starting combustion system.

5E is a schematic diagram of an example gradual oxidation system 5500 that mixes multiple points 5504, 5510, 5516, and 5522 of water 430 injection, in accordance with certain aspects of the present disclosure. Many elements of system 5500 are common to systems 5100-5300 discussed above, and their description is not repeated with respect to FIGS. 5A-5D. Subsequent processes 5504, 5510, 5516 and 5522 at each injection point will evaporate some amount of water into the gas at the process input while cooling the process output gas flow due to the potential heat of evaporation of the injected water. Water injection can be strategically performed only at individual locations or in combination with other injection locations.

Water injection at location 5504 can be used to cool the inlet flow stream temperature of compressor 410. Lower inlet temperatures increase the density of fluid entering the gas turbine cycle, which increases power output. Lower compressor inlet temperatures reduce the amount of work (power) used to compress gas 5558 and allow more shaft power 412 to drive the generator 416.

Water injection at locations 5510, 5516 and into heat exchanger 418 increases the power output of the turbine cycle. Compression of liquid water, as typically implemented by a pump, may be more efficient than compressing the gas mixture in the compressor 410. These cycles are often referred to in the art as "humid air cycles." Thus, the system 5500 can leverage the beneficial effects of water injection in the cycle without generating thermal NOx due to the gradual oxidation process.

The injection and evaporation of water in the recuperator 418 may be more than the thermodynamic cycle performance advantages listed in the previous paragraph. Recuperator 418 is naturally heated by exhaust flow 5526. Evaporation of water can increase the effective heat transfer coefficient of the flow between 5512 and 5514, which allows for smaller physical heat exchangers.

Other embodiments and methods of injecting water can also be used in accordance with the description provided herein. For example, other systems and methods of injecting water into an oxidation system are described in US patents filed March 15, 2011, the disclosure of which is incorporated herein by reference in its entirety to the extent that the teachings are not inconsistent with this description. Application 13 / 048,796.

5F is a diagram 5600 of a typical gas content of the exhaust of various systems. Conventional gas turbines can generally be observed to operate with approximately 9% by mass of free oxygen remaining in the exhaust stream. By using progressive oxidation techniques in the oxidizers of FIGS. 5B and 5C while generating steam at the same time, the oxygen content flowing out of the oxidizers and gas turbine cycles will be low, preferably in the range of 1.5 to 5%. 5F shows this as being below the range for conventional gas turbines. Therefore, the simultaneous generation of contaminant-free flue gas and steam in the gradual oxidizer / steam generator, system 5200 of FIG. 5B is new in the art. As discussed earlier in this document, lower oxygen and higher levels of CO ₂ and H ₂ O are advantageous for the Brayton gas turbine cycle.

Control of the gradual oxidation system can be implemented in a number of ways. In certain aspects, the method of ensuring complete oxidation changes the residence time of the fuel and air mixture in the oxidizer vessel. In certain aspects, the gas turbine supplies a gradual oxidizer, and the turbine is structured to change its rotational speed using, for example, various speed generators and power electronics or inverters. In, the fan supplies a fuel and air mixture to the oxidizer, for example as shown in FIG. 2A, the fan is operated by variable speed drive, and the fan speed is reduced to increase the residence time in the oxidizer.

In some embodiments, the oxidation systems described herein can be used to oxidize fuel in a flexible, efficient and clean manner. The oxidation reactions described herein provide methods for the oxidation of waste materials and thereby for preventing or minimizing air pollution. For example, methods and systems in which oxidation reactions are used are described in US patent application filed May 25, 2011, which is hereby incorporated by reference in its entirety to the extent that the teachings are not inconsistent with this description. / 115,910 and US Patent Application 13 / 115,902, filed May 25, 2011.

The previous description is provided to enable any person skilled in the art to practice the various aspects described herein. While the foregoing has been described as being the best mode and / or other embodiments, various modifications to these aspects will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other aspects. . In addition, although various embodiments may be depicted in various sections, paragraphs with reference to the various figures, various embodiments may be combined with other described embodiments unless otherwise indicated. Thus, the claims are not intended to be limited to the embodiments set forth herein, but the full scope is to be accorded the language of the claims, where the singular reference to the elements is other than "one or more". Unless specifically noted, it does not mean "one and only one." Unless specifically indicated otherwise, the terms "a set" and "some or some" refer to one or more. Headings and subheadings, if present, are used for convenience only and do not limit the disclosure.

It is understood that the specific order or hierarchy of steps in the processes disclosed is an illustration of exemplary approaches. Based upon design preferences, it is understood that the specific order or system of steps in the processes may be rearranged. Some steps may be performed simultaneously. The accompanying method claims present elements of the various steps in a sample order, and are not intended to limit the specific order or scheme provided.

The terms, such as "top", "bottom", "front", "rear", etc., as used in this disclosure, refer to the usual gravitational reference of reference. Rather than in a frame, it should be understood to refer to an arbitrary frame of reference. Thus, the top surface, the bottom surface, the front surface and the back surface may extend upwards, downwards, diagonally or horizontally in the gravitational frame of reference.

The phrase, such as “aspect,” does not mean that this aspect is essential to the present technology or that such aspect applies to all structures of the present technology. The disclosure relating to one aspect may apply to all structures or one or more structures. Phrases such as an aspect may refer to one or more aspects or vice versa. The phrase such as "embodiment" does not mean that this embodiment is essential to the present technology or that such embodiment applies to all structures of the present technology. A disclosure relating to one embodiment may apply to all embodiments or one or more embodiments. Phrases such as an embodiment may refer to one or more embodiments or vice versa.

The letter "exemplary" is used herein to mean "functioning as an example or illustration." Any aspect or design described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other aspects or designs.

As used herein, at least one of A, B and C, or at least one of A, B and C, or at least one A, B or C (at The enumeration citing "at least one of A, B or C)" means only A, only B, only C, or any combination of A, B and C, including all of A, B and C.

All structural and functional equivalents to the elements of the various aspects described throughout this disclosure, known to or after one of ordinary skill in the art, are intended to be incorporated herein by reference, and are incorporated by reference. Furthermore, nothing herein is disclosed as being dedicated to the public regardless of what is explicitly recited in the claims. If an element is not quoted using the phrase "means for," or in the case of a method claim, the element is not quoted using the phrase "step for", No claim element is found under 35 USC § 112, provisions of 35 U.S.C. § 112, sixth paragraph. Moreover, when the terms "include", "have" and the like are used in the description or the claims, such terms are used in the claims as "comprise". As used in the following description, it is intended to be included in a manner analogous to the term “comprise”.

Claims (1)

An oxidizer having a reaction chamber having an inlet and an outlet, comprising: an oxidizer structured to maintain an oxidation process without a catalyst, the reaction chamber being configured to receive a gas comprising an oxidizable fuel through the inlet;
detect at least one of (a) the reaction temperature in the reaction chamber is close to the flameout temperature of the fuel in the reaction chamber, or (b) the reaction chamber inlet temperature is close to the autoignition threshold. A detection module; And
Based on the detection module, a correction module that outputs instructions for changing at least one of (i) removal of heat from the reaction chamber or (ii) inlet temperature of the reaction chamber.
Including;
The calibration module is structured for at least one of (i) maintaining the actual temperature in the reaction chamber below the burnout temperature or (ii) maintaining the inlet temperature above the fuel's self-ignition threshold.
System for oxidizing fuel.

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