MXPA06006920A - Apparatus and method for the production of energy - Google Patents

Abstract

Apparatus and processes are provided for combusting hydrocarbon containing waste fuel with an oxidizer, preferably liquid oxygen, and producing a substantially clean exhaust gas and a separate high purity steam product (e.g., superheated steam) that can be used to generate electrical power. The apparatus includes a plurality of combustion chambers in series with means to control the combustion temperature while facilitating complete combustion. The apparatus and method are useful for transforming waste materials, particularly solid and liquid wastes, such as the rubber from scrap tires into non-hazardous materials and energy.

Description

APPARATUS AND METHOD FOR THE PRODUCTION OF ENERGY FIELD OF THE INVENTION - This invention is found in general terms in the field of combustion apparatuses for burning fuels, and more particularly to combustion systems for creating steam and / or electrical energy, and more particularly to a combustion system that uses products of waste as a source of fuel and means for waste disposal.

BACKGROUND OF THE INVENTION Production of electrical energy and pollution Conventionally, electricity is produced in thermoelectric plants by electric generators powered by gas turbines, steam turbines, hydroelectric dams, and large diesel engines. The steam used in these plants is conventionally created by burning coal, oil or natural gas, or by nuclear reactors. Today the world faces a complex and persistent crisis of energy and electrical energy. During the last ten years, the demand for electric power increased by approximately 30%, while the transmission capacity increased by only half. It is projected that the demand for electricity and the fuels used to produce electricity will increase. With the worldwide growth of energy demand, sensitive energy policies require careful balancing of three objectives: (a) low cost; (b) minimal environmental impact; and (c) security of supply. Energy security depends on the ability to adequately manage the economic, supply and environmental consequences of the energy sources used to produce electricity. The United States of America currently produces electricity using several different fuels, including coal, which represents approximately 57% of the electricity supply, and nuclear energy, which represents approximately 20% of the electricity supply. The rest is supplied by power plants that work with natural gas, hydroelectric dams, and small amounts of renewable energy. Solar cell and fuel cell technologies are currently underdeveloped and expensive. Hydroelectric and wind power are inconveniently limited in terms of use due to geographic location issues. For a long time, the energy industry has been looking for more efficient, safer, environmentally less aggressive and effective alternatives for energy costs from coal, natural gas and nuclear.

Thermoelectric plants that use coal Coal is a non-renewable resource, and only extractable coal remains for approximately 200 years. The combustion of coal generally has an efficiency of only 20% (only about 20% of the kcal / hour in coal is actually used to convert water into steam). Currently, about 40 million tons of coal are used annually to generate energy. Thermoelectric plants that use coal release millions of tons of toxic emissions into the atmosphere each year. The US public interest research group recently reported that air pollution from thermoelectric plants increases, and a significant amount of the increase comes from coal-fired plants. Although it is relatively cheap to burn coal, this is one of the most impure fuels. The charred coal produces millions of kilograms of "coal ash" and "volatile ash", solid waste combustion materials containing highly poisonous and / or radioactive chemical compounds, such as arsenic, uranium, mercury, lead and thorium. (The ash content varies from approximately 5% to 15% of the calcined coal). Other environmental contaminants that are produced by conventional combustion-based power generation plants include sulfur dioxide (S02); other sulfur oxides, such as SO, S02 and / or S0, collectively known as SOx; nitrogen dioxide (N02), the main component in smog; Nitric oxide (DO NOT); other nitrogen oxides, such as NO, N20 and / or N02, collectively known as N0X; carbon monoxide (CO); carbon dioxide (C02); methane (CH); hydrochloric acid (HCl); dioxin; volatile organic compounds (VOC), w cause smog and are dangerous for plants and animals; various metals, such as zinc, thallium, cadmium, nickel and chromium; radioactive materials in addition to the isotopes of uranium and thorium, such as radium, radon, polonium, bismuth and lead; other carcinogenic and / or mutagenic substances; and particulate matter, w is an air pollutant by assessment (criteria air pollutant). Plants that use conventional coal use air as the source of oxygen for combustion.

However, the air contains 76.9% by weight of nitrogen (N2) and 23.1% by weight of oxygen (02), as well as a certain amount of argon and C02. These non-oxygenated components make air a non-ideal source for oxygen, because they can contribute to environmental pollutants, such as NOx, SOx, and CO. The US regulatory requirements Current regulations prescribe the amounts of atmospheric emissions that are allowed in particular sites by specific power plants. The permissible emission threshold levels are continuously reduced, w puts an increasing pressure on the power generating plants to reduce emissions.

Thermoelectric plants that use natural gas Compared to nuclear and coal power plants, conventional natural gas-powered power plants can be built at a relatively low cost. However, the disadvantage is that these plants are extremely sensitive to increases in the price of fuel, w often occurs as a result of problems with the supply. Likewise, the combustion of natural gas by conventional methods usually has an efficiency of only about 30% (only about 30% of the energy value of natural gas is actually used to convert water into steam). In addition, high levels of the air pollutant are often emitted by N0X titration into the atmosphere from power plants powered by conventional natural gas.

Inefficiency of conventional power generation Conventional generation of electric power and heat separately (as opposed to co-generation, tri-generation, and the like) is usually inherently inefficient, converting only about one third of the Potential energy of a fuel into usable energy. For example, thermoelectric power plants that use traditional coal, oil or natural gas generally do not convert more than a third of the initial energy of the fuel into useful electricity; the remainder is discarded as residual heat. There is now a need for safe, rapid, low-cost, efficient and environmentally clean methods and appliances to produce electrical power, and to produce steam and flue gas exhaust products that can be used in the production of electrical energy. .

Disposal of waste materials and hazardous materials There is always an abundant supply of hydrocarbon waste materials on the planet. Each year, about 725.8 kg of garbage per person are discarded, of w approximately 80% is disposed of in landfills. The rates of decomposition in the landfill for many of these hydrocarbon materials are tens to hundreds of years. Old tires, plastic debris, and carpet and textile debris are three types of hydrocarbon-based waste materials that are often disposed of in landfills. Approximately 270 million tires (3.4 million tons) are discarded as old tires every year in the United States of America, and almost 800 million tires are still waiting to be disposed of in landfills. Many states have banned throwing old tires complete and / or partial in landfills. In order to avoid discharge payments or the effort required to legally remove old tires, many old tires are thrown away illegally. These illegally disposed tires present health and environmental problems, are unattractive, and create fire hazards. Currently there are no adequate methods to properly remove old tires.

Approximately 34.02 million tons (75 billion pounds) of plastic are produced each year in the United States of America. Examples of these plastics include containers and polyethylene products. Most plastic ends up in landfills, where decomposition takes many years. It would be desirable to provide more suitable means for removing the waste plastic. The amount of carpet that enters the waste stream increases continuously. Approximately 96% of this waste is disposed of in landfills. According to the United States Environmental Protection Agency (US EPA), approximately 6.35 million tons (14 billion pounds) of textile and carpet waste is disposed of in landfills each year in the United States of America. The carpet takes almost 50 years to begin to decompose, the landfill space decreases, and many landfills no longer accept carpets. It would be desirable to provide appropriate means for eliminating carpet waste. Currently there is a need for methods and apparatus to remove old tires and plastic, carpets, textiles and other hydrocarbon waste materials in a safe, fast, low cost, efficient and environmentally clean manner. There is also a growing need to eliminate hazardous materials in a safe, effective, efficient, and cost-effective manner. Examples of hazardous materials include infectious medical waste; biological and chemical weapons such as anthrax, agents that attack the nervous system, and rockets or containment devices for them; and hazardous air pollutants. The proper disposal of such materials is expensive and usually presents a serious risk to the health of humans and other animals. Existing means to safely dispose of hazardous materials are undesirable. In many cases, this has involved dumping hazardous materials into deep sanitary landfills or enclosing them in protective containers and then burning these containers in sanitary landfills or in the open sea. Other hazardous materials are eliminated by combustion in garbage dumps or commercial incinerators. However, depending on the incineration parameters, such destruction is often laborious, incomplete, and produces dangerous levels of harmful environmental contaminants. There is a need for safe, fast, inexpensive and efficient methods and equipment for the complete destruction of hazardous materials (making them non-hazardous) without producing unacceptable levels of environmental contaminants.

Description of the prior art The patent E.U.A. No. 3,779,212 discloses a system for generating steam that burns fuel in a pure oxygen atmosphere to heat water in a heat exchanger to convert water to steam. This uses a single processing chamber, individual combustion. The patent E.U.A. No. 4,915,038 discloses a method and a burner for sudden expansion to incinerate waste materials and hazardous fluids or gaseous entrained in air and combined with another fuel. The patent E.U.A. No. 5,709,077, patent E.U.A.

No. 5,970,702, and patent E.U.A. No. 5,680,764 discloses an apparatus for generating gas including water vapor and carbon dioxide from the combustion of a hydrocarbon gas with oxygen. The patent E.U.A. No. 6,206,684 discloses a system for injecting fuel mixtures into a combustion chamber, including a steam generator injector designed to inject fuel, oxidant and cooling water into a combustion chamber. The patent E.U.A. No. 5,715,673 and the patent E.U.A. No. 5,956,937 describe large-scale electric power generation systems that use thermal energy from the combustion of a liquid or gaseous hydrocarbon fuel (propane, methane, natural gas or light alcohols) using liquid oxygen, and they are said to be free of pollution, or have low pollution. The patent E.U.A. No. 6,247,316 and the patent E.U.A. No. 6,170,264 describe generators with low contamination. All of these patents describe mixing cooling water with hot combustion gases that are generated by a combustion reaction in a single reaction / chamber, whereby a gaseous mixture of steam and carbon dioxide is supplied to a turbine. However, it would be desirable if the cooling water does not come into contact with the combustion gas products, so that carbon dioxide does not have to be separated from the vapor. It would also be desirable to prevent the exhaust products of the flue gas from coming into contact with the turbines or with the electric power generating equipment, in order to minimize corrosion or other damage from the ash or other products of incomplete combustion. It would also be desirable to provide a useful combustion system with a variety of fuel types.

SUMMARY OF THE INVENTION Devices are provided for use as a hydrocarbon combustion gas generator. In a preferred embodiment, the apparatus comprises (a) a first combustion chamber in which a first combustion of fuel and oxidant can be effected to produce an incomplete combustion product, the first combustion chamber has an inlet end and an end of exit; (b) control and dosing means for dosing separately a fuel and an oxidant within the first combustion chamber to achieve incomplete combustion of the fuel in the first chamber; (c) a second combustion chamber in which a second combustion of fuel and additional oxidant can be effected to produce a second combustion product, the second combustion chamber has an inlet end and an exit end in which the end inlet of the second combustion chamber is in fluid communication with the outlet end of the first combustion chamber; (d) control and dosing means for dosing additional oxidant into the second combustion chamber for additionally burning fuel in the second chamber; (e) means for dosing the incomplete combustion product that occurs in the first combustion chamber into the second combustion chamber; and (f) heat exchanger means for cooling the first and second combustion chambers and optionally converting the cooling water to steam, in which the cooling water and steam are kept separate from the combustion gases produced for the first and second combustions. This preferably includes an electronic ignition system or other means for igniting the fuel in the first combustion chamber. In one embodiment, the second combustion is a complete combustion. In one embodiment, the means for dosing into the second combustion chamber the incomplete combustion product produced in the first combustion chamber comprises a plurality of tubular openings. In another embodiment, the apparatus also includes (g) a third chamber or combustion space in which a third combustion of the fuel and additional oxidant can be effected to produce a third combustion product; (h) control and dosing means for dosing additional oxidant into the third chamber or combustion area to burn additionally fuel in the third chamber or area; e (i) additional heat exchange means for cooling the third chamber or combustion area and for optionally converting the cooling water to steam, in which cooling water and steam are kept separate from the combustion gases produced by the third combustion. Optionally, this also includes means for metering the incomplete combustion product that occurs in the second combustion chamber into the third combustion chamber. Preferably, the air is not allowed to mix with the fuel or oxidant in the combustion chambers. In various embodiments, the control and dosing means for separately dosing a fuel and an oxidant into the first combustion chamber, the fuel and the oxidant comprise a plurality of orifices near the inlet end of the first combustion chamber. For example, the fuel, the oxidant, or both can be metered into each of the combustion chambers or areas in an inclined manner, which results in at least one point of collision between the fuel and the oxidant. The heat exchanger means may comprise a plurality of tubes forming one or more tube assemblies, having at least one cooling water inlet and at least one vapor outlet. In one embodiment, the tube assemblies form walls that define one or more of the combustion chambers or areas. In general terms, the apparatus includes a source of oxidant, such as LOX, 0, 03, H202 or HAN, and a source of one or more fuels. The control and dosing means for dosing a fuel separately can be adapted to separately dose two or more types of fuel within the first combustion chamber. In one embodiment, at least one fuel is in the form of solid particles, for example, constituted by plastic, rubber, or other waste materials, and has a particle size ranging from about 31 to about 2,300 microns. In one embodiment, at least one additional fuel is a liquid or gaseous fuel. Examples of suitable fuels include fuels EF-1, EF-2, EF-3, EF-4, EF-5, EF-6, EF-7, EF-8, EF-9, EF-10, EF- 11, EF-12, EF-13, EF-14, EF-15, EF-16, EF-17 or EF-18 described in the present invention. By using the apparatus, preferably from about 97% to about 100% of the fuel metered in the first combustion chamber is burned by the apparatus. In another aspect, a system is provided to generate electricity. This system comprises the combustion apparatus that generates steam, and a device generating electric power driven by said steam. For example, the electric power generator may comprise a steam driven turbine. In preferred embodiments, the system can produce from about 1 to about 600 megabytes of electric power per day. The system can be a co-generation system, a tri-generation system, or a quad-generation system. In another aspect, a combustion process is provided which comprises supplying at least one fuel to the apparatus; supplying at least one oxidant to said apparatus; and burning said fuel and said oxidant in said apparatus. In the process, the first combustion may occur at a temperature ranging from about 648.88 ° C to about 3204.44 ° C, at a pressure ranging from about 35.15 kg / cm2 to about 105.45 kg / cm2 and over a period of time It varies from about 0.025 to about 10 seconds. The second combustion may occur at a temperature ranging from about 1648.88 ° C to about 3204.4 ° C, at a pressure ranging from about 21.09 kg / cm2 to about 105.45 kg / cm2 and over a period ranging from about 0.025. up to 10 seconds approximately. Preferably, the combustion gas exhaust product does not contain, or contains insignificant amounts of, mercury, SO, S02, S03, NO, N02, N20, CO, CH4, HCl or dioxin. The oxidant preferably comprises LOX. The fuel may comprise a material that is not waste, such as wood, coal, hydrogen, methane, ethane, butane, propane, natural gas, gasoline, diesel fuel, kerosene, fuel oil, methanol, alcohol, a product containing plastic, mixed plastic or plastic resin, or a combination thereof. In another aspect, a method is provided to eliminate hazardous or waste materials. This comprises supplying a fuel to the apparatus, in which the fuel comprises at least one hazardous or waste material; supplying at least one oxidant to said apparatus; and burning said fuel and said oxidant in said apparatus. Examples of hazardous material include infectious medical waste, biological or chemical weapons, components thereof, or a container therefor. Examples of waste material include old tires, plastic-based packaging materials, or components thereof.

BRIEF DESCRIPTION OF THE FIGURES Figure 1 is a cross-sectional view of the of an embodiment of the hydrocarbon combustion gas generator described in the present invention. Line 5-5 represents the cross-sectional plane of the generator shown in Figure 5. Similarly, lines 6-6, 8-8, and 9-9 represent the cross-sectional planes of the generator shown in Figures 6 , 8, and 9, respectively. Figure 2 is an enlarged cross-sectional view of a portion of the hydrocarbon combustion gas generator shown in Figure 1, extending from the fuel inlet distributor 12 to the second transfer injector plate 84. The Figure 3 is an enlarged cross-sectional view of another portion of the hydrocarbon combustion gas generator shown in Figure 1, extending from the second water distributor 98 to the sixth super-heated steam outlet 148. Figure 4 is a cross-sectional view of the first oxidant distributor 41, the first oxidant distributor plate 40, the first oxidant injector ports 46, the first fuel openings 34, the first fuel opening tubes 36, the flame tubes 29, and the first transfer injector plate 44 of the hydrocarbon combustion gas generating apparatus shown in Figure 1.

Figure 5 is a cross-sectional view of the first oxidant distributor 41, the first oxidant distributor plate 40, the first oxidant injector ports 46, the first transfer injector plate 44, the first outer housing 50, the oxidant transfer tube 49, flame tubes 29, and individual water tubes of the first tube assembly 71 of the gas generator shown in Figure 1, seen from the first combustion chamber 70 towards the fuel inlet distributor 12 and taken along plane 5-5 of Figure 1. Figure 6 is a cross-sectional view of the first water inlet 62, the first water distributor plate 60, the first outer housing 50, the second fuel openings 65, the second fuel opening pipes 66, the fuel wear plate 63, the second superheated steam outlet 67 and the individual water pipes of the first pipe assembly or 71 of the gas generator shown in Figure 1, seen from the first combustion chamber 70 towards the second combustion chamber 100 and taken along the plane 6-6 of Figure 1. Figure 7 is a sectional view of the second superheated steam outlet 67, the second water inlet 62, the supply water distributor 64, the first water distributor plate 60, the fuel wear plate 63, the second fuel openings 65 , the second fuel opening tubes 66, the second oxidant inlet 81, the second oxidant distributor 82, the second oxidant distributor plate 80, the second oxidant injector ports 85, and the second transfer injector plate 84 of the gas generator shown in Figure 1. Figure 8 is a cross-sectional view of the second oxidant distributor 82, the second oxidant injector orifices 85, the second transducer injector plate. S 84, the second fuel openings 65, the second fuel opening tubes 66, the oxidant transfer tube 49, the second outer housing 90, and the individual water pipes of the second tube assembly 101 of the gas generator shown in figure 1, with the excess oxidant leading to the oxidant transfer tube 49, seen from the second combustion chamber 100 towards the first combustion chamber 70 and taken along the plane 8-8 of figure 1. Figure 9 is a cross-sectional view of the second oxidant distributor 82, the second oxidant distributor plate 80, the second oxidant inlet 81, the second oxidant injector orifices, the second fuel openings 65, the second tubes of fuel opening 66, and the oxidant transfer tube 49 of the gas generator shown in Figure 1, seen from the first combustion chamber 70 towards the second combustion chamber 100 and taken along the plane 9-9 of figure 1. Figure 10 is a detailed view of the second transfer injector plate 84, the second fuel openings 65, and the second oxidant injector ports 85 shown in Figure 8. Figure 11 is a cross-sectional view of the first transfer injector plate 44, the first oxidant injector ports 46 and the first fuel opening tubes 36 shown in Figure 4. Figure 12 is a detailed view of the second transfer injector plate 84, the second oxidant injector ports 85, the second fuel openings 65, and the second fuel opening tubes 66 shown in FIG. Figure 7. Figure 13 is a detailed view of the second oxidant injector orifices 85 shown in Figures 7 and 12. Figure 14 is a procedural flow chart showing a modal of a trigeneration steam energy generating plant including a hydrocarbon combustion gas generator described in the present invention.

DETAILED DESCRIPTION OF THE INVENTION Methods and apparatus have been developed to generate safe, rapid, cost-effective, and efficient high-energy, high-purity steam in an environmentally clean form from a variety of hydrocarbon fuel sources. Preferably, the fuel source is a waste material, such as rubber from old tires, discarded carpets, waste plastic, or hazardous waste material. Steam can be used to generate large amounts of electrical energy without corroding or otherwise damaging turbines, condensers or other equipment or devices for producing electrical energy. In another aspect, the methods herein provide for the removal of hydrocarbon waste materials in a safe, fast, cost-effective, efficient and environmentally clean manner, by diverting waste material from landfills. Conveniently, the methods can simultaneously or consecutively produce (a) a super-heated steam product or dry saturated steam product that can be used to produce electrical energy when it is introduced into a device or system generating electrical energy; and (b) transform hazardous materials into non-hazardous materials. To enable these procedures, a combustion generator that is operated using a non-air source of oxygen has been developed and includes a multi-chamber combustion system in which the cooling water does not mix directly with the combustion gases. The apparatus therefore provides complete combustion of the fuel while generating a highly pure vapor product that does not need to be subjected to a separation process to separate it from the combustion product carbon dioxide. The hydrocarbon combustion gas generator generally includes: (a) one or more means for receiving a liquid or gaseous oxidant, in which the oxidant is not air; (b) one or more means for receiving a hydrocarbon fuel; (c) means for dosing the oxidant and the fuel within a first combustion chamber in an oxidant / fuel mixture ratio, and under conditions, which may cause incomplete combustion of the fuel in the first combustion chamber after it is ignited, including inlet means and distribution means for the oxidant and for the fuel; (d) one or more means for igniting the fuel and the oxidant in the first combustion chamber; (e) means for dosing additional oxidant and the combustion gas product that is produced in the first combustion chamber into a second combustion chamber or area in an oxidant / fuel mixture ratio, and under conditions that cause complete combustion of the combustion chamber. fuel in the second chamber or combustion area, including inlet means and distribution means for the additional oxidant and for the combustion gas product that is produced in the first combustion chamber; (f) means for containing the combustion gas products that are produced in the first combustion chamber and in the second combustion chamber in a controlled flow; (g) means for a flue gas exhaust product to exit the hydrocarbon combustion gas generator; (h) means for introducing water into one or more areas or components of the hydrocarbon combustion gas generator that are positioned in contact with, or in a proximity sufficiently close to, one or more exterior surfaces of one or more walls of a or more chambers or combustion areas, in which the water cools said walls and in this way preserves the structural integrity of the chambers or combustion areas, and in which at least a certain amount of the water becomes a vapor product which does not come into contact with and remains separate from the flue gas exhaust product, including water inlet means and water distribution means; e (i) means for the vapor product to exit the hydrocarbon combustion gas generator separately from the flue gas exhaust product. The hydrocarbon combustion gas generator may optionally include a third (and more) combustion chambers. In such embodiments, the generator may include means for dosing additional oxidant and the product of combustion gas that is produced (which in this case may have been incompletely burned) in the second chamber or combustion area to a third area (or chamber) of combustion in an oxidant / fuel mixture ratio, and under conditions, which may cause complete combustion of the fuel in the third chamber or combustion area (or incomplete combustion of the fuel in the third chamber or combustion area if one or more additional combustion chambers or areas are present in the hydrocarbon combustion gas generator), including inlet means and distribution means for the additional oxidant and for the combustion gas product that is produced in the second chamber or combustion area. If the gas generator has more than three chambers or combustion areas, the hydrogen combustion gas generator usually also has additional components and conditions corresponding to those described above. In general terms, a flue gas exhaust product that results from complete combustion of a fuel (or some other material, such as waste material or a hazardous material) leaves the last chamber or combustion area (the one that is more downstream) that is present in a hydrocarbon combustion gas generator of the invention. A variety of blends can be used as fuels in the methods and apparatus described in the present invention. The mixtures have one percent by weight (% by weight) of 100, contain the hydrogen element, the carbon element, or the hydrogen and carbon elements, and contain two or more of the following components: from about 0 to about 99 (% by weight) of carpet; from about 0 to about 99% by weight of hydrogen; from about 0 to about 99% by weight of polystyrene; from about 0 to about 99% by weight of polyethylene terephthalate; from about 0 to about 99% by weight of polyethylene terephthalate; from about 0 to about 99% by weight of high density polyethylene; from about 0 to about 99% by weight of low density polyethylene; from about 0 to about 99% by weight of polypropylene; from about 0 to about 99% by weight of polyurethane; from about 0 to about 99% by weight of nylon 6.6; from about 0 to about 99% by weight of nylon 6; from about Q to about 99% by weight of polyvinyl chloride; and from about 0 to about 99% by weight of tire rubber, in which the blends can function as fuels in the process and apparatus of the present invention. Preferably, the solids are mixed with other solids, the liquids are mixed with other liquids, and the gases are mixed with other gases.

Definitions As used in the present invention, the terms "comprises", "comprising", "includes", and "including" are intended to be open, non-limiting terms, unless otherwise expressly indicated. The phrase "back end" as used in the present invention in relation to the hydrocarbon combustion gas generator, or any other component thereof, means that end of the gas generator, or a component thereof, which is closest to the location in which the flue gas exhaust product leaves the gas generator. When observing the accompanying figures, the rear end will be the right end of the combustion gas generator, or the component thereof. The terms "austenitic steel" and "austenitic stainless steel" as used in the present invention refer to steels which are generally non-magnetic and which can not be treated with heat, and which are generally hardened and work in cold, they generally have excellent qualities of resistance to heat and corrosion with suitable mechanical properties over a wide range of temperatures. Austenitic steel grades include CH-20, CK-20 and CN-7M. The abbreviation "kCal" as used in the present invention means kilocalories. The term "co-generation" as used in the present invention means the simultaneous production of thermal energy and electrical or mechanical energy from the same fuel in the same installation. This is also known as "combined power and heat", and can be produced using a combined heat and power (CHP) system. With a thermoelectric power plant driven by co-generation fuel, it is possible to capture and take advantage of the initial energy contained within the fuel used in the plant that is not converted into electrical energy and that could otherwise be disposed of as waste heat, for example , using a boiler for residual heat recovery. The phrase "combustion efficiency" (nc or Ec) as used in the present invention means a measurement (in%) that indicates the ability of an apparatus or system to convert a particular fuel into usable thermal energy over a period of time. specific operating period. For systems that use fuel, this phrase is defined as the quotient of the fuel energy input less the losses by combustion gas (dry combustion gas, incomplete combustion and humidity formed by the combustion of hydrogen) with respect to the input of fuel energy. In the United States of America, combustion efficiencies that use fuel are reported based on the highest caloric value of the fuel. However, other countries report combustion efficiencies that use fuel based on the lower caloric value of the fuel. The combustion efficiency of a system that uses fuel will generally be higher than thermal efficiency. A complete combustion efficiency (100%) is one in which all the energy (100%) available in a fuel is extracted. Combustion efficiency calculations assume complete combustion of the fuel. The phrase "air pollutant by titration" as used in the present invention means a common air pollutant that can damage health, endanger the environment, and / or cause property damage, and which is regulated by the EPA using criteria (scientific guidelines based on the health and / or environmental effects of the air pollutant) as the basis for establishing permissible levels. Air pollutants by titration include CO, NOx, S02, and particulate matter. The phrase "downstream" as used in the present invention means that it leads to the rear end of a hydrocarbon combustion gas generator.

The phrases "environmentally clean" or "environmentally cleaner" as used in the present invention in relation to the methods, apparatuses and fuels of the present invention mean that, without requiring contamination control equipment, one or more (by example, all) products that are produced using such processes, appliances, and / or fuels, such as superheated steam products, dry saturated steam products, and / or flue gas exhaust products: (1) no produce or contain environmental contaminants or hazardous materials; (2) they do not produce or contain hazardous materials, and only produce or contain the environmental pollutant C02 (that is, they do not produce or contain any other environmental contaminants); (3) produce smaller quantities of hazardous materials compared to plants or nuclear power systems that produce the same amount of energy or electrical power; and (4) produce or contain smaller amounts of one or more environmental contaminants and / or hazardous materials compared to the amounts of environmental contaminants and / or hazardous materials produced by, or contained in, one or more products that are produced by one or more procedures, devices and / or systems that use fuel to produce steam, energy or electrical power that i) use air in them or allow the air to come into contact with the fuel, oxidant and / or water used in them, with the combustion gases produced in this way, and / or with the components thereof (such as systems and steam production plants by conventional coal combustion, systems and plants for the production of electrical energy by conventional coal combustion, systems and steam production plants by conventional natural gas combustion and energy production systems and plants ctrica by conventional combustion of natural gas; and ii) they can produce the same amount of superheated steam product, dry saturated vapor product, other forms of steam, thermal electric energy or power or other electric power or power, and / or use the same fuel and the same amount of gas. The phrases "environmental pollutants" and "contaminants" as used in the present invention mean materials that can contaminate or damage any part of the environment (air, water, soil and the like), and include air pollutants, such as air pollutants. air by valuation, water contaminants, and soil contaminants. Environmental contaminants may or may not also be hazardous materials.

Environmental contaminants include sulfur oxides (S0X), such as sulfur dioxide (S02), nitrogen oxides (N0X), such as nitric oxide (NO), nitrogen dioxide (N02), nitrous oxide (N20), monoxide carbon (CO), carbon dioxide (C02), hydrochloric acid (HCl), methane (CH4), volatile organic compounds (VOCs), dioxin, ammonia (NH3), benzene, hydrogen fluoride, hydrogen sulfide, polyaromatic hydrocarbons ( PAH), hexachlorobutadiene, ethylene dibromide, mercury, arsenic, uranium and thorium, and isotopes thereof, and radioactive products produced by the degradation of uranium and thorium, such as radium, radon, polonium, bismuth and lead, particulate matter and other radioactive chemicals or products. The phrase "exhaust system" as used in the present invention means one or more components of an apparatus through which one or more exhaust products of combustion gas are discharged., with or without other products (to the atmosphere, or to another system or apparatus, such as a C02 recovery system). The phrases "terrific steel" and "terrific stainless steel" as used in the present invention mean magnetic steels containing chromium but not nickel, and whose structure consists mainly of ferrite. These steels usually have good resistance to heat and corrosion and good resistance to corrosion cracking caused by mechanical stress. The grades of ferritic steel include CB-30 and CC-50. The phrase "front end" as used in the present invention in relation to the hydrocarbon combustion gas generator present, or with any of the components thereof, means that end of said generator or component closest to the location in the which enters the fuel inside the generator. When looking at the attached figures, the front end is the extreme left of said generator or component. The phrase "rich in fuel" as used in the present invention means that a mixture of fuel and oxidant contains more fuel than can be 100% burned by the available oxidant. The phrase "hazardous material" as used in the present invention means any solid, liquid and / or gaseous substance or combination thereof, such as entrained particles or slurries, which present a health risk (e.g. of disease, discomfort, injury, or death) or any other danger to humans, animals, aquatic life forms (eg, fish, whales, sea turtles), and / or aerial life forms (eg, birds, bats), including dangerous air pollutants, chemical warfare agents (VX, Tabun, Sarin, Soman, mustard gas, etc.), VOCs, infectious medical waste, needles and other items that have come into contact with infectious diseases, anthrax spores, biological weapons, carcinogens, mutagenic agents and / or radioactive agents. Hazardous materials can be environmental pollutants. The abbreviation "HCGG" as used in the present invention means a hydrocarbon combustion gas generator of the present invention. The term "hydrocarbon" as used in the present invention means the inclusion of any or both of the carbon and hydrogen elements and, optionally, containing other elements, such as nitrogen, chlorine, sulfur, oxygen and other elements. The phrases "hydrocarbon material" and "hydrocarbon-based material" as used in the present invention mean any solid, liquid or gaseous chemical compound, substance or material, or mixture or other combination thereof, including waste materials. and of non-waste, which includes a hydrocarbon. The phrase "interface" as used in the present invention means a surface, or portion thereof, that forms a common boundary between adjacent regions, bodies or substances or in some other way connected (i.e. the location in which the two items touch or meet). The term "interior" as used in the present invention means a part or surface that is, or is facing, the interior (away from the exterior). For example, the interior surface of a side wall of a combustion chamber or area faces the interior of the combustion chamber or area. The term "ignition device" as used in the present invention means a device, assembly or system that releases heat and, thus, initiates a reaction of one or more fuels and one or more oxidants. The phrase "lower portion" as used in the present invention in relation to a hydrocarbon combustion gas generator of the invention, or with a component thereof, means that portion of the hydrocarbon combustion gas generator., or a component thereof, which is closer to the chambers or combustion areas present in the hydrocarbon combustion gas generator. The abbreviation "LOX" as used in the present invention means liquid. The term "dispenser" as used in the present invention means a structure, such as a tube or chamber, that contains one or more feed routes or other openings separated or connected together, which can produce any of a series of numerous different patterns (such as a snowflake), and which may have a variety of different shapes (circular or ring-shaped, oval-shaped, square-shaped, rectangular, triangular, etc.), to receive a gaseous, liquid and / or solid substance or material (in a reduced size form), such as a fuel, an oxidant, water, vapor or the like, directly or indirectly from one or more supplies or other sources, such as a storage tank for fuel, oxidant, water, steam or other storage tank, and / or for distributing or otherwise supplying the substance or material to an appliance, or a component of the Such as to a combustion chamber of the hydrocarbon combustion gas generator of the present invention. The phrase "dose" as used in the present invention means allowing a substance or material, whether a solid, liquid, gas, or a combination or other sample thereof, to flow or otherwise travel from a site. to another site and / or from a component of an apparatus or system to another component of an apparatus or system, at a specific speed, for example, at 4,536 kg / second. The phrase "mixed plastics" as used in the present invention includes intermixed plastics (a combination of two, three or more types of plastics), mixed materials, laminates, and other multi-component materials. The phrases "0 / F ratio" and "0 / F mixing ratio" as used in the present invention mean the ratio of oxidant to fuel in a mixture of oxidant and fuel that is used in a particular area or component of the HCGG. , such as a first combustion chamber, a second chamber or combustion area, a third chamber or combustion area or a fourth chamber or combustion area, in a firing device or system, or in a particular passage of a method. The 0 / F ratio can be varied in a manner known to the person skilled in the art to make a mixture of oxidant and fuel "fuel-rich", "fuel-poor" or "stoichiometric" in any one or more chambers or combustion areas of an HCGG. The phrase "particulate matter" as used in the present invention means solid particles (or a mixture of solid particles and tiny liquid droplets or other materials or substances) that generally vary in size from fine particles (approximately less than 2.5. μm in diameter) to coarse particles (greater than 2.5 μm in diameter), which are environmental pollutants and / or hazardous materials. Particulate matter, such as PM-10 (fine particulates) and PM-2.5 (ultrafine particulates), is usually emitted from electric power plants that use coal and other fuels, and often carry heavy metals and / or compounds Organs that cause cancer to the lungs of humans and animals, which increases the incidence and severity of respiratory diseases. Particulate matter includes dust, smoke, soot, ash (coal ash, volatile ash and other types of ash), non-combustible material present in coal and other small pieces of solid materials that are released inside, and / or they move around in, the air. The ultrafine particulate materials are mainly nitrates and sulphates formed from the NOx and SOx emissions. The term "plastic" as used in the present invention means any of a wide variety of complex organic compounds that are generally produced by polymerization, and which can be molded, extruded, cast in various shapes and / or films and / or stretched as filaments used as textile fibers, and includes thermoplastic and thermosetting polymeric materials obtained from petroleum products or from biologically derived polymers. Representative examples include polyethylene (for example LDPE and HDPE), polypropylene, polybutylene, polystyrene, polymethylpentene, polyurethanes, polyvinyl chloride, unsaturated polyesters or epoxies, polycarbonate, nylons, polyethylene terephthalate (PET), and acrylonitrile-butadiene-styrene. The phrases "fuel designed for processing" and "PEF" as used in the present invention mean a combustible product that is manufactured from paper and second-hand plastics obtained from residential, commercial and industrial sources, which are used as an industrial fuel, and which usually contain 70-90% paper and the remaining percentage is plastic. PEF is usually present in a dense form, such as granules, and is often obtained from reserve materials from separate sources. In comparison with the fuel obtained from waste, the PEF is more refined, has a lower ash content, has a lower moisture content and has a higher caloric power, which is due to its plastic content. The PEF can be used in general in existing energy installations, without the need for dedicated plants. Therefore, there is a large reserve of potential oxidizers for fuel designed for processing than for fuel obtained from waste. In addition, when PEF is used, the investment in significant capital for existing facilities has generally already been made, which should improve the economic aspects of the use of PEF. Additional information regarding PEF, and its manufacture, is presented at www. plasticsresource. com. The terms "waste derived fuel" and "RDF" as used in the present invention mean a fuel that usually consists of very poorly processed municipal solid waste material, and which is generally in a crumbled form. As used in the present invention, the term "old rim" refers to a rim that is no longer appropriate for its original purpose, including worn, defective, or damaged rims. The term "source" as used in the present invention means any place or object, such as an electric power plant, a chemical plant, or a motor vehicle, from which one or more environmental contaminants are released.

The phrase "stainless steels" as used in the present invention means high alloy steels which generally have superior corrosion resistance compared to other steels because they contain large amounts of chromium (usually from 4 to 30%, and normally around 10%). Stainless steels can be divided into three basic groups based on their crystalline structure in: austenitic, ferritic, and martensitic. The phrase "vapor purity" as used in the present invention means the amount of solid, liquid or vapor contamination (non-aqueous components) that is present in a vapor, and is generally reported as total solids in parts by weight. one billion (ppb). Steam contamination can cause overheating, corrosion and / or failure of the superheater, steam pipe and cracking expansion joints, turbine control valve clogging, deposits and erosion of the turbine blade, cracking of the turbine disc, and the contamination of products and air conditioning. Operating pressures of up to 105 kg / cm2 and vapor temperatures of up to 590 ° C can be provided by providing a vapor purity as low as 5 ppb of entrained solids. Steam cleaning equipment that can provide the desired vapor purity for a particular application can be obtained from ABCO Industries (Abilene, TX). The phrase "vapor quality" as used in the present invention means the amount of moisture that is present in the vapor. This is the weight of dry steam in a mixture of steam and water droplets, generally reported as a percentage. If the steam does not contain moisture, the steam is 100% in terms of quality. Steam quality refers to the purity of the vapor because the liquid droplets that may be present in the steam often contain dissolved solids, potentially causing vapor contamination. Humidity by itself can also be harmful. The company AECL Research (Manitoba, Canada) has an instrument that can measure steam quality and mass flow velocity. The phrases "stoichiometric ratio" and "ratio of oxidant mixture to stoichiometric fuel" as used in the present invention mean that, in a combustion process, an ideal ratio of oxidant to fuel is obtained. An oxidant to stoichiometric fuel ratio can be used to produce a stoichiometric combustion reaction, in which this ratio depends on the particular fuel and the particular oxidant that are chosen for use. For example, if the fuel is methane and the oxidant is oxygen, a ratio of oxidant to stoichiometric fuel could be two to one gaseous volume (or four to one by weight). The person skilled in the art can easily determine an oxidant-to-stoichiometric fuel ratio for a particular oxidant and fuel. The phrase "thermal efficiency" as used in the present invention means the ratio of heat absorbed by water (or by water and steam) or air with respect to the thermal value of the energy consumed. This is a measure of the speed at which heat exchange surfaces transfer heat to the transfer medium (usually water or air). The thermal efficiency is calculated by determining the losses of combustion gas as one percent of the fuel burned [Ec = 1 - losses by combustion gas]. It is often not possible to obtain full thermal efficiency due to reserve losses, losses from the boiler shell and similar factors. Different types of heat movement have an effect on thermal efficiency. Convection / convection heating surfaces (also known as secondary or indirect heating surfaces) include all surfaces exposed only to hot combustion gases. Radiant heating surfaces (also called direct or primary heating surfaces) consist of heat exchanger surfaces exposed directly to radiant heat from a flame. In general, radiant heat transfer is more effective than conduction / convection heat transfer, and this is the type of heat transfer that occurs in a boiler or forced air system. The terms "tire derived fuel" and "TDF" as used in the present invention mean fuel that is obtained from complete or processed old tires. These include the rubber portions of the tires that have been ground, shredded, or crushed, for example, to a size of 5.08 cm or smaller. In general terms, the TDF is a compact and consistent composition, and has a low moisture content. The term "tri-generation" as used in the present invention means the simultaneous production of three different forms of energy from the primary energy source, specifically, heating, cooling and generation of electrical energy. This is also known as "combined generation of heat, cooling and power". A typical trigeneration facility consists of a cogeneration plant and a vapor absorption chiller that produces cooling using a certain amount of heat recovered from the cogeneration system. The products of a tri-generation system are usually steam, hot water, cold water and electricity. The phrase "upper portion" as used in the present invention with respect to a hydrocarbon combustion gas generator of the invention, or with a component thereof, means that portion of the hydrocarbon combustion gas generator, or a component thereof, which is furthest away from any of the chambers or combustion areas present in the hydrocarbon combustion gas generator. The phrase "upstream" as used in the present invention means that it leads to the front end of a hydrocarbon combustion gas generator of the present invention, or of a component thereof. The phrase "wet steam" as used in the present invention means vapor that contains water molecules (ie, fog, moisture) that has not evaporated. As a result of the liquid water in it, wet steam is often corrosive to metal parts, such as metal blades in a steam turbine or other turbine. Wet steam also has lower thermal transfer efficiency compared to super-heated steam. To improve steam quality, the wet steam can be superheated to create super-heated steam using a conventional circulation heater. The term "zone" as used in the present invention means a point, line or area in which the oxidant and fuel intersect, mix, ignite and / or travel together, for example, in or through a chamber and / or combustion area.

Fuel One or more fuel supply control means allow the initiation, termination and / or regulation of one or more fuel supplies, which may be the same or different, which may be solid, gaseous, liquid or a combination or other. mixing of more than one solid, gas and / or liquid, and which may be compatible or incompatible, with the apparatuses of the present invention. The fuel supply control means may include a fuel line that is attached to a fuel source and a pump, or any other suitable system to achieve the same results. Any hydrocarbon material or combination of such materials, whether solid, liquid, gaseous, or a combination thereof, can be used which can be burned in any percentage by weight (from 0% to 100%) as a fuel, or as a component in a combination of fuel or other mixture, in the methods and apparatus of the present invention. Such materials include fuel designed for processing, designed fuel, fuel obtained from waste, fuel obtained from tires, hydrocarbon materials and other materials that are not waste, and hydrocarbons and other waste materials. Said materials may be hazardous or non-hazardous materials, may contain sulfur and / or nitrogen, and may contain one or more additives, such as antifungal substances or agents or antifreeze substances or agents. Examples of non-waste materials that may be used include wood, coal, methane, other natural gases, gasoline, diesel fuel, kerosene, fuel oils (any of the different grades), hydrogen, ethane, butane, propane, alcohol, plastic articles, mixed plastics, or combinations thereof. Examples of hydrocarbon waste materials include the non-metallic components of used tires, carpet waste and discarded carpet material, household or residential waste, styrene foam articles, commercial waste, municipal waste, industrial waste, cooking oils used, used manufacturing oils, used motor oils, wood waste, agricultural waste (both of vegetable and animal origin), human and animal excrement, paper and paper mill waste, wood mill waste, mill waste of sugarcane (for example bagasse), oil refinery waste, automotive industry waste (plastic vehicle fenders, carpets and the like), mud and dredged waste from beaches, and mixtures thereof. In particular, plastic beverage bottles and plastic packaging material can be used as the hydrocarbon waste material. The energy or caloric value values of different materials are known or can easily be determined. The fuel preferably has an energy value ranging from about 1,665 kcal / kg to about 30,525 kcal / kg (3,000 to 55,000 BTU / lb), more preferably from about 4,440 kcal / kg to about 22,200 kcal / kg (8,000 to about 40,000 BTU / lb), with 17,760 kcal / kg (32,000 BTU / lb) being most preferred. In order to minimize or eliminate the amount of environmental contaminants and / or hazardous materials in the flue gas exhaust products produced by the methods and apparatus of the present invention, the combustible materials preferably do not contain (1) substances (for example, sulfur, sulfides and / or nitrogen) that can form environmental contaminants or hazardous materials (for example N0X, NO, N02, N20, S0X, S02, HCl and CO), or (2) metals (for example, arsenic, lead, mercury, plutonium, radon or uranium), and preferably do not produce particulate matter, such as ash, when burned. Therefore, it is preferable that hydrocarbon materials other than carbon, nylon 6, nylon 6,6 or rubber from old tires be used as a fuel component, given the nitrogen content of these materials. These non-preferred components can be removed by one or more fuel cleaning or separation processes prior to combustion. However, if the flue gas exhaust products produced by the methods and apparatus of the present invention contain nitrogen and / or sulfur, these components of the flue gas exhaust products can be removed (eg, cleaned) using equipment. of known pollution control. A variety of wood types can be used as fuels. Many types of wood do not contain sulfur or nitrogen. Typical residential solid waste may also include only small amounts of nitrogen and / or sulfur. The methods and apparatus of the present invention preferably use a fuel comprising one or more waste materials, due to the following advantages: this reduces the space in landfills that could otherwise be occupied by the waste materials.; These are usually available in a plentiful supply; These can often be obtained without cost; and unlike most fuels, they must provide an additional source of income (for example in the form of waste disposal fees, recycling fees, unloading fees and / or end user fees (fees paid to the user for accepting, remove, remove and / or otherwise recycle waste materials.) Solid fuels (in a small-sized form) are preferred for use in the methods and apparatus of the present invention Examples include discarded carpets, waste carpet, plastic beverage container, and a mixture of tire rubber and carpet and / or carpet material waste.The tires used consist primarily of hydrocarbons and steel scrap, and usually contain low amounts of nitrogen. 80% of used tires are usually made of carbon and oxygen, and used tires usually have a higher percentage. s low sulfur than most coals. The sulfur present in the used tires varies from 1.24 to 1.30% by weight, while the sulfur present in the coal varies from 1.1 to 2.3% by weight or more, depending on the type and quality of the coal. When used tires are used as fuel, it is preferable to use the hydrocarbon material present in the used tires, which can be processed by conventional methods such as ground rubber (or other forms of reduced size), and not waste steel, so such that heavy metals (such as arsenic, barium, cadmium, chromium, lead, mercury, selenium and / or silver) are not present in flue gas exhaust products or other products that are produced by these procedures and appliances. The resulting hydrocarbon material can generally be vaporized using the methods and apparatus of the present invention to its most basic molecular or atomic structures, namely the non-polluting, non-hazardous hydrogen, carbon and oxygen gases, and water vapor. Various forms of tire derived fuel can be commercially available. Plastics have a high energy content, typically the highest energy value in modern waste energy incineration processes and apparatuses. Therefore, plastics are preferred solids for use as fuels and fuel components in the methods and apparatus of the present invention. Carpet material, which may include woven and nonwoven carpets (mixed textiles), typically include nylon, polypropylene (olefin), polyester and wool, with other fibers including cotton and acrylic. The yarn used to form the hair of a cushioned carpet can be made of nylon, acrylics, wool, cotton and the like, nylon 6 and nylon 6, 6 being the fiber material most commonly used for the face of the carpet itself . Carpet pads are produced from styrene foam, fiber (synthetic or man-made) and rubber, for example reprocessed pads, which are made from styrene foam waste used in carpentry. Most carpets have a primary backing and secondary backing, which are typically made from plastic. The latex-based glue is usually placed between the backs of the carpet to keep the strands of the carpet fiber together. The automotive carpet generally contains fiber-forming polymers, predominantly nylon 6 and nylon 6,6, polypropylene, polyethylene, polyester, acrylics, ethylene-vinyl acetate copolymer, ethylene-vinyl acetate-filled copolymer and BaS04. The waste of carpet usually contains more than one polymeric material. The ethylene-vinyl acetate copolymer is a major component of carpet waste. A typical carpet waste that can be used as fuel for use in the methods and apparatus of the present invention has an energy value of approximately 8.614.7 kcal / kg (15,522 BTU / lb) and comprises: (a) from 339,056 g / m2 approximately up to approximately 813.73 g / m2 (10 to 24 ounces per square yard) approximately of the nylon 6 or nylon 6,6 surface component; (b) from about 101.72 g / m2 to about 135.62 g / m2 (3 to 4 ounces per square yard) of the primary polypropylene or polyester backing; (c) from about 271.24 g / m2 to about 406.87 g / m2 (8 to 12 ounces per square yard) of the poly (ethylene-vinyl acetate) precoat or low density polyethylene; e (d) from approximately 1017.17 g / m2 to approximately 4,611.16 g / m2 (30 to 136 ounces per square yard) of the polyethylene co-vinyl acetate-backed backing. A preferred fuel formulation obtained from carpet waste material for use in the methods and apparatus of the invention comprises from about 0 to about 35% nylon 6 and / or nylon 6,6, from about 0 to about 55% polypropylene, from about 0 to about 35% polyester, from about 0 to about 18% polyethylene, from about 0 to about 36% ethylene-vinyl acetate copolymer, and from about 0 to about 60% filler . The fuels for the methods and apparatus of the present invention that are produced from one or more solid materials preferably have particle sizes ranging from about 37 to about 2000 μm., and preferably range from about 149 to about 400 μm. In the granulation or other size reduction of the solid materials, the particle size of the resultant granulated materials is important because this influences the quality of the combustion processes that occur in the methods and apparatuses of the present invention, and allows particles reduced in size to be reformulated as a fuel, a fuel combination or a fuel mixture that may contain one or more other substances. It has been determined that materials that have particle sizes of approximately 30 μm and smaller are often explosive (they burn spontaneously). Therefore, materials having such particle sizes for use in the methods and apparatus are generally not recommended. Mesh particle sizes that are greater than approximately 2300 μm should also be avoided because they can cause supply problems in the fuel injectors of the appliances. Therefore, plastic, rubber and other solid materials should be granulated to fine particle sizes having the particle sizes described above to allow small particles to be appropriately reformulated as a fuel. The following table shows the approximate particle sizes (in US mesh, inches and microns) of one or more solids, and the approximate percent distribution of said one or more solids having the indicated particle sizes, which are preferred for use. in the fuels or fuel components that are used in any combination in the methods and apparatuses of the present invention: Particle sizes and distribution in solid fuels or fuel components The size of the solid materials can be reduced using known methods, and the resulting particles can be separated into the desired size ranges by screening. The following table shows the approximate particle sizes of one or more solids, and the approximate percent distribution of said one or more solids having the indicated particle sizes, which are more preferred for use as fuels and fuel components for the methods and apparatus of the present invention.

Particle sizes and distribution in solid fuels or fuel components The fuels (or fuel mixtures) that are most preferred for use in the processes and apparatuses, are fuels or fuel combinations that are generally obtained from solid materials, for example, rubber from used tires, material for carpets or other plastics, and sometimes combined with a separate hydrogen component, which has a higher energy content and, therefore, which can raise the energy value of the final fuel product. These fuels or fuel blends are designated as "designed fuels" or "EF fuels" in the present invention. The following table shows the formulations (the approximate weight percent range of the individual components) for 18 different EF fuels (called EF-1 to EF-18), and the energy content of each of the 18 EF fuels (in terms of the largest and smallest possible number of kcal / kg of fuel generally present, depending on the percentage of specific weight of each component used in the fuel). For EF fuels that do not contain a separate hydrogen component, the fuel can be fed into the apparatus through at least one fuel inlet. However, for those designed fuels, such as EF-10 and EF-11, that contain a separate hydrogen component (which may be additional to the hydrogen contained in other fuel components), the separated hydrogen component must be fed into of the apparatus through a fuel inlet that is separated from the fuel inlet in which the other fuel components are fed into the interior of the apparatus. However, separate fuels or fuel components are usually present together in the first combustion chamber of the apparatus. Example 2 indicated later in the present description provides an analysis of the components of the separate flue gas exhaust products that are produced using these EF fuels in one of the apparatuses of the present disclosure. The term "carpet" as used in the table indicated below refers to the typical carpet waste described above in the present description, but may also include any other type of carpet waste or other carpet waste. The other components listed, such as polypropylene and nylon 6.6 are additional to any of the components, such as polypropylene and nylon 6.6, which may be present in the carpet component of the fuel, fuel combination or other mixture. The phrase "tire rubber" as used in the table refers to the non-metallic components of used tires that have been reduced in size. The following percentages by weight are the preferred values.

Eighteen fuels designed As a result of its high energy content, the most preferred designed fuel for use in procedures and apparatus is EF-10 fuel. Manufacturers of hydrocarbon materials that subsequently become waste products that are difficult to dispose of, such as carpet manufacturers and automotive manufacturers, can conveniently use one or more of the apparatus of the present description to generate electrical energy. on the site, using its own waste products such as fuel sources, or fuel components. These manufacturers can also sell the excess electric power that is generated back to the local power distribution networks.

Preparation of fuels and fuel components from solid materials The designed fuels of the present invention and other fuels obtained from solid hydrocarbon materials are generally constituted by one or more solid hydrocarbon materials, freeing them from glass and / or metal components and then reducing their size to smaller particles which preferably have a uniform size using the known methods of grinding, grinding at room temperature, cryogenic grinding, shearing, granulation, tabletting, dicing, spraying, fragmentation by impact at high speed or other methods. If desired, the raw materials used to produce the fuels or fuel components can be dried to reduce or otherwise control the moisture content. A second shredder can be used to further process these materials. The solid fuels used in the methods and apparatuses of the present description may involve the use of intermingled rubbings with plastic rubber of production of material and carpet having different order specifications. The product that is recycled can consist of several different materials, such as plastics with electroplated metal or plastic reinforced with fabric. These materials are preferably released from each other, so that they can be separated as individual materials for use in a fuel. Different types of manufacturing processes known specifically for processing intermixed plastics have been developed. These procedures are generally classified as extrusion processes and cryogenic milling procedures and at room temperature. Each of these processes can produce products from a wide variety of homogeneous mixtures of plastics and waste rubbers.

Cryogenic Grinding Procedures In most cryogenic grinding operations, liquid nitrogen is used to cool a material during size reduction. Through grinding, thermoplastic materials at cryogenic temperatures usually produce plastics that are sufficiently brittle to be ground to very fine particle sizes. The use of liquid nitrogen in cryogenic grinding procedures controls and regulates the heat of the mill, and allows higher material yields. Organic materials usually have an increased risk of explosion when very fine particles are combined. The use of nitrogen to render the atmosphere inert during the milling process minimizes the safety risks associated with explosions. The temperature of the liquid nitrogen used in cryogenic milling processes is usually approximately -195.56 ° C at atmospheric pressure. Most plastics and rubber compounds freeze at their glass transition temperature of approximately -62.22 ° C. At temperatures below the glass transition temperature, plastics and rubber change from an elastic material to one that is sufficiently brittle and easy to grind using impaction methods. The use of cryogenic temperatures can be applied at any stage of size reduction for most plastics and rubber. The choice of the supply material for a cryogenic stage depends on the available supply material and the characteristics of the desired products. Typically, the size of the supply material is that of a piece of 5.08 cm, or smaller in size. The pieces of supply material are supplied at a constant speed inside a heat exchanger in which they are cooled by direct contact with liquid nitrogen. The most efficient pre-cooler uses countercurrent heat exchange in which the liquid nitrogen is sprayed onto the plastics and / or rubbers near the outlet end of the pre-cooler. Liquid nitrogen evaporates as it cools the plastics and / or rubber, and the cold nitrogen vapor is passed back to the feed end where it is further heated by the plastics and / or rubbers. The hot nitrogen gas is vented to a safe site while the plastics and / or frozen rubbers are supplied to a grinder mill. The temperature of the plastics and / or frozen rubbers coming out of the pre-cooler is usually controlled to a temperature ranging from about -101.11 ° C to about -195.56 ° C. The choice of temperature depends on the intensity of the grinding to be carried out in a later step. The particle size of the product is usually a little thinner when cooler temperatures are used. The plastics and / or cold rubbers are milled, for example, with a hammer mill, which produces a product of plastics and / or rubbers ranging from approximately 4 mesh to a very fine powder. Preferred granulators employed in cryogenic grinding processes typically use the cutting principles by high speed shear and impact fragmentation to reduce the size of the starting solid material. Any metallic remnants in the product with reduced size can usually be separated from the product using magnets or other known methods. Any fiber that can be trapped with the metal can be detached in a mill and removed by suction and sieving. The remaining plastics and / or rubbers can be dried and then separated to the desired particle size ranges by sieving. If additional fine powder, usually 30 mesh or smaller, is desired, a secondary high intensity grinding method can be used. The feeding material for this process is preferably plastic particles and / or rubbers with a clean mesh size of 4. The procedure described above can generally also be used for clean industrial waste and post-consumer waste, except that metal or fiber removal steps are generally not necessary, and only one stage of cryogenic milling is generally needed. . The liquid nitrogen requirements for these materials are approximately 0.75 kg of nitrogen per kg of material and larger, depending on the mesh size desired for the resulting particles. Nowadays, new mills are being developed to economically produce particles with a mesh size of 80 and finer. In order to further reduce the size of plastics and / or rubber, milling technologies can be used at room temperature and / or wet after a cryogenic milling of the material. The performance from the cryogenic grinding procedures varies, depending on the size of the mill, the particle mesh sizes produced, and the cooling procedures used. Typical yields of approximately 1,360.8-2,721.60 kg / hour (3000-6000 pounds / hour) are typical. In general terms, cryogenic grinding equipment includes a material cooler, typically an endless screw conveyor, liquid nitrogen flow controls, a data acquisition system and mill controls. There are several advantages of using a cryogenic grinding process, including cleaning the process and effective separation of fiber and steel from plastics and / or rubbers. Although the cost of plastics and / or rubbers subjected to cryogenic milling is usually 0.022 to 0.066 dollars / kg (0.01 to 0.03 dollars / pound) approximately the same at equal particle mesh sizes compared to plastics and / or rubber subjected to milling at room temperature, the particle sizes of the plastics and / or rubbers milled at room temperature are normally limited to 40 mesh or larger. Key benefits in the use of cryogenic grinding procedures to produce the products described above compared to other procedures include improved production performance rates, improved quality (due to reduction in history or thermal distortion), finer particle sizes (due to the ease of particle fracture), cleaner and easier release and separation of waste from mixed components, and reduced specific energy consumption (grinding energy per unit of processed product) in relation to the size reduction step. The benefits of cryogenic milling processes also include smaller particles, regular particle size, process efficiency, improved surface morphology, effective temperature control and an inert atmosphere. Cryogenic grinding procedures produce surfaces with almost smooth fracture, and generate little or no heat. This results in less degradation of the resulting plastic and / or rubber products. In addition, when the tires used are reduced in size using this method, almost all of the fiber and steel is conveniently removed from the rubber, which results in a high yield of usable product with little loss of rubber. In addition, the price of liquid nitrogen has recently been reduced significantly, which results in this size reduction procedure being more cost effective.The use of liquid nitrogen to cool a material takes advantage of the cooling achieved by the liquid nitrogen (a) to remove the grinding heat to prevent melting, distortion, or discoloration of polymeric materials during processing; (b) to brittle a polymer to allow it to be reduced in size more effectively, or to obtain selective brittleness when there are two or more components; or (c) to release multi-component materials using different rates of thermal expansion / contraction caused by exposure to low temperatures of liquid nitrogen.

Grinding procedure at room temperature In the milling process at room temperature, a high-power plastics and / or rubber mill is used to shear and grind plastics and rubber to small particles. It is common to produce material with a particle size of 10 to 30 mesh using a relatively large lump. Frequently several grinding mills are used in series. The typical yields of ground material are approximately 907.2-997.92 kg / h (2000-2200 lbs / hr) for material with 10 to 20 mesh particle size, and approximately 544.32 kg / hr (1200 lb / hr) for material with a particle size of 30 to 40 mesh. The finer the desired particle, more time is left to the plastics and / or rubber run in the mill. In addition, multiple grinds can be used to reduce the particle size of plastics and / or rubber. The practical lower limit for the procedure is the production of material with a 40 mesh particle size. Any fiber and foreign material must be removed using an air table, and the metal is removed using a magnetic separator. The resulting material is quite clean. The process of grinding at room temperature produces a material having a particle configuration cut into an irregular shape. In addition, the process generates a significant amount of heat in the material supplying plastics and / or rubbers (or others) during processing. Excessive heat can degrade the product from plastics and / or resulting rubbers, which, if not properly cooled, can ignite during storage. Grinders for milling at room temperature usually contain a primary shredder, a secondary shredder, a granulator, a releaser and a classifier. When the size of the used tires is reduced by a grinding procedure at room temperature, the tires used are usually shredded and then supplied to a grinding mill. The ground product is then separated into steel, textile materials and rubber granules. The granulation can be classified into different particle sizes. The following table compares the physical properties of materials subjected to size reduction with cryogenic procedures compared to milling procedures at room temperature: The following table compares the approximate distribution of particle size in percent by weight that results from the reduction in size of two different samples of ground rubber, in which a sample is subjected to size reduction with a cryogenic grinding procedure and the another sample is subjected to size reduction using a milling procedure at room temperature: Once the various solids to be used in a fuel have been subjected to size reduction to the desired particle sizes, the particles subjected to size reduction can be mixed together in any commercially available mixer. It is preferred that the mixture of the different plastics, rubbers and / or other materials, and the different particle sizes thereof, be as homogeneous as possible. However, if one or more of the plastics, rubbers or other materials that are to be used in a fuel can not be mixed in a homogeneous way, these can be separated into two (or more) groups and injected from two different areas into the apparatus to achieve a homogeneous mixture in a combustion chamber of the apparatus. Likewise, any liquid or gaseous hydrocarbon fuel (or other fuel having the characteristics described in the present description) can be used with fuel components obtained from solid materials to achieve a higher energy value of the total fuel used in the methods and apparatus of the present invention (a value of kcal / kg higher). When these are compatible with each other, fuels or fuel components obtained from plastics, rubber or other solid materials can be mixed with a fuel or liquid, gaseous, gelled or other fuel component before entering the combustion apparatus . However, even if several fuels or fuel components are not compatible with each other, they can still be used together in the methods and apparatuses of the present invention. For example, incompatible fuels or fuel components can be kept separate from each other outside and inside the apparatus, and then injected separately into a first combustion chamber present in the apparatuses, where these can be mixed together, and with the oxidant chosen for the use. The person skilled in the art can determine which different fuels and fuel components are compatible.

Oxidant One or more same or different oxidants are used in the methods and apparatus of the present invention to cause and / or maintain the combustion of a fuel, when ignited and in the presence of fuel. The oxidants help in the conversion of the energy present in the fuel to caloric energy. One or more oxidant supply control means allow the initiation, termination and / or regulation of one or more oxidant supplies, which may be the same or different, to the apparatus. The oxidant supply control means may include an oxidant line that is attached to an oxidant source and a pump, or any other suitable system. When air is used as an oxidant in a combustion process, the nitrogen present in the air can be combined with the oxygen that is present in the combustion gases and / or exhaust products of flue gas, or in the air in which the exhaust products of the combustion gas are released, which results in the release into the atmosphere of significant quantities of environmental contaminants, such as the air pollutant by NOx titration, as well as NO, N02 and N20. Therefore, the methods and apparatuses of the present invention do not use air as an oxidant (and generally in no way allow air to come into contact with fuels, oxidants, water, other refrigerants, flue gases or other substances that may be present in the systems, or that enter the systems). Preferably, the oxidant used in the methods and apparatus of the present invention does not contain nitrogen. In contrast to the use of air as an oxidant, the use of an oxidant with no or reduced nitrogen present in the procedures and apparatus eliminates or reduces the amount of air pollutant by N0X titration, as well as NO, N02, N20 and other nitrogenous environmental pollutants that are produced in the exhaust products of the flue gas, thereby producing steam or electric power with little or no nitrogen emissions. Liquid or gaseous oxidants that are not air, and that preferably do not contain any nitrogen, are used as the oxidants in the methods and apparatus of the present invention. These oxidants have a purity that preferably ranges from about 90% to about 100% (these contain only from about 0% to about 10% of impurities), and more preferably ranging from about 95% to about 100%, by approximately 95.5% or approximately 99.9%, and more preferred is approximately 100%. Preferred are liquid oxidants, such as LOX, O, 03 (ozone), hydrogen peroxide (H202) and hydroxylamine nitrate (HAN). However, the oxidants may be gaseous oxidants or compressed oxygen. Due to their low costs and clean nature, the most preferred oxidants are LOX and hydrogen peroxide. The most preferred oxidant is pure LOX (100%). Because the oxidant entry into the apparatus of the present invention at any one or more entry points can be regulated by the user, the oxidant entry into these devices at any of the sites can be completed at any time. This feature conveniently provides the user with the ability to finish the combustion process of the fuel in the appliances, either in the first combustion chamber, in the second combustion chamber, and / or in any chamber or combustion area, in any moment. The electrical energy that is produced using the methods and apparatus of the present invention can be used to produce liquid 02 cheaply and in large quantities (thousands of kilograms per day). Alternatively, Air Products (Allentown, PA) manufactures PRISM® Oxygen Vacuum Swing Adsorption systems for on-site oxygen generation. Appropriate oxidants can also be obtained from Airgas, Inc. (Radnor, PA), Praxair, Inc. (Danbury, CT), and other commercial sources. The amount of oxidant that is introduced into each of the chambers and / or areas of the apparatuses of the present invention will affect the amount of heat generated therein, wherein more oxidant usually results in higher heat. The amount of oxidant that is introduced into each of the chambers and / or areas of the present apparatus other than the chamber and / or final area of preference is an amount of oxidant that keeps the mixture of oxidant and fuel in a "rich" mixture. in fuel. " The amount of oxidant that is present in, or that is introduced into, the last chamber or combustion area of the apparatus of preference is an amount of oxidant that produces a stoichiometric combustion reaction.

Mixing the fuel and oxidant in the chambers and / or combustion areas Oxidants and particular fuels, or fuel components, chosen for use in the methods and apparatus of the present invention may result in variations in characteristics such as relative chemical reactivity , the ease and speed of vaporization of the fuel, the ignition temperature, the diffusion of hot gases, the volatility and / or surface tension. However, the person skilled in the art can choose combinations of one or more oxidants and one or more fuels or fuel components with which the desired results are achieved. In order to cause the oxidants and fuels or fuel components that enter the interior of a first combustion chamber of the present apparatus to mix well, instead of remaining in separate receptacles or in some other separate way, it is preferable that the oxidants and fuels are subjected to swirling action in the first chamber or combustion area, whereby oxidants and / or fuels or fuel components (and preferably both) are rotated. This swirling action also allows oxidants and fuels or fuel components to remain in the first chamber or combustion area for a longer residence time, and allows fuels or fuel components to absorb more thermal energy from the reaction of combustion than what would happen in the absence of the swirling action. The swirling action of the oxidant and fuel in the first combustion chamber (or in others), can be achieved, or increased, in a variety of different ways. Said swirling action can be achieved, for example, by injecting flows of an oxidant into a first combustion chamber at one or more of the same angles or at different angles (in any direction that causes the oxidant to travel into the interior of the first combustion chamber). Said angles of preference vary from more than about 0 degrees to less than about 180 degrees relative to the surface of a plate (or other component) in which holes are bored or otherwise injected from the oxidant injector, which otherwise it injects the oxidant in a straight direction into the interior of the first combustion chamber, and more preferably varies from about 10 degrees to about 90 degrees, more preferably about 70 degrees. Alternatively, or additionally, streams of a fuel or fuel component can be injected into a first combustion chamber (or other) at one or more of the same angles or at different angles (in any direction that causes the fuel trip to the first combustion chamber). Said angles of preference also range from more than about 0 degrees to less than about 180 degrees relative to the face of the plate (or other component) in which the holes of the fuel opening are drilled or otherwise placed. , and most preferably from about 10 degrees to about 90 degrees, with about 70 degrees being most preferred. It is preferred that both the oxidant and the fuel are injected into the first chamber or combustion area in inclined shapes, which results in one or more collision points between the fuel and oxidant streams (one or more points, lines and / or areas of intersection of oxidant and fuel streams within the first combustion chamber). As a result of the angles at which the fuel and oxidant streams enter the first combustion chamber, the fuel and oxidant streams can form a variety of different flow patterns, for example, a double-collision flow pattern ( one or more separate intersections of a fuel stream and an oxidant stream), a triplet impact current pattern (one or more separate intersections of a fuel stream and two oxidant streams), as shown in Figure 4 and in Figure 11, a self-impaction current pattern (one or more separate intersections of two fuel streams or two oxidant streams) or other flow patterns. Alternatively, the fuel and / or oxidant can be injected into the first combustion chamber in a "shower-type" flow pattern that does not present a collision (in which both the fuel and the oxidant are injected in a straight stream within of the first combustion chamber, such as the way in which water flows out of a shower in a bathroom). These various patterns can be achieved, for example, by drilling or otherwise by placing holes of the oxidant injector into an oxidizer distributor at the desired angles, and / or by boring or otherwise placing the holes in the fuel opening inside. of a fuel meter block at the desired angles. The parameters that can be varied widely and easily by the person skilled in the art in connection both with the injection of one or more oxidants as well as the fuel or fuel components inside the first combustion chamber (and into other chambers or combustion areas) of the apparatuses of the present invention in order to achieve the desired results include sizes of injector orifices, patterns formed by the injector orifices, impact angles, angles of the resulting moment, the distance of the shock locus from the surface of the injector, the number of injector orifices per unit area of face of the injector, the flow per unit of injection orifice and the distribution of the orifices along the surface of the injector (in a non-collision manner, in a collision way or similar or in a similar collision way). Oxidizer and / or fuel injector configurations that can be used include non-collision, non-similar collision and similar collision configurations. The oxidant and fuel injector elements of the non-collision type include: (a) coaxial or concentric injection elements, which usually have a slower central flow of liquid oxidant movement surrounded by a concentric sheath of higher speed gaseous fuel; (b) sprinklers, which provide flows of reactants directly axial, or almost axial, that do not present an impact; (c) fan formers, which provide aspersions of reagents in cones or fans; and (d) slots and sleeves, which contain two-dimensional narrow slots. The oxidizer and fuel injector elements of low probability of collision type include: (a) non-similar doublets, which direct a current of one reagent against a different current of another reagent, which produces a fan-type aspersion constituted by the mixture of two streams that collide; (b) unlike triplets, in which a symmetrical non-similar injection element consists of an axial central current of one of the reactants (either the fuel or the oxidant) and two external currents that collide symmetrically of each other reactant; (c) quadruplets; (d) Pentacles (or any other grouping of currents). The oxidizer injector and similar collision fuel elements include: (a) similar doublets, with two streams of the same reagent being inclined to each other to an impact point, resulting in a fan-shaped spray of tiny droplets; (b) similar imminent triplets, in which three streams of the same reactant are tilted together toward a common collision point; and (c) larger groupings of similar flows. Orifices, and orifice sizes for different fuel and / or oxidant can be used to achieve the injection pressures, injection rates, flows and / or oxidant to fuel ratio desired. For a given impulse F, and a given escape velocity c, the total reactant flow m = F / c. The types of holes that can be used include holes with pointed edges, short tubes with rounded entry holes, short tubes with tapered inlet holes, short tubes with spiral-shaped holes, and / or holes with a pointed edge cone. With these (and other) types of orifices, the orifice diameters generally vary depending on the size of the apparatuses, and preferably range from about 0.0381 mm to about 15.24 cm, and most preferred range from about 0.254 mm to about 2.54 cm. . In order to make the additional oxidant, and the unburned fuel present in the incomplete combustion product produced in the first combustion chamber, enter a second chamber or combustion area of the apparatuses of the invention so that they mix well (instead of being separated), it is preferable that the oxidant and the unburned fuel are subjected to swirling action in the second chamber or combustion area, whereby the oxidant and / or the unburned fuel is made (and preferably both) turn. This swirling action also allows the oxidant and unburnt fuel to remain in the second chamber or combustion area for a longer residence time, and allows the unburned fuel to absorb more thermal energy from the combustion reaction than the that could happen in the absence of the swirling action. The swirling action of the oxidant and unburned fuel in the second chamber or combustion area (and in any additional chamber and / or combustion areas optional) can be achieved, or increased, in the same modes, and at the same angles , described above in connection with the first combustion chamber. It is preferable that both the oxidant and the combustion product produced in the first combustion chamber are injected into the second combustion chamber at an angle. This can be achieved by boring or otherwise placing oxidant injector holes into an oxidizer distributor at the desired angles, and boring or otherwise placing fuel opening holes into a fuel wear plate in the desired angles. Although it is preferable that the swirling processes described above, which employ turbulence and / or diffusion to achieve that the mixing of fuel with oxidant, is present in each of the chambers and / or combustion areas used in the apparatus of the present invention, said swirling action is not necessary.

Water One or more water supply control means allow the initiation, termination and / or regulation of one or more water supplies to the appliances. The water supply control means may include one or more water supply pipes that are attached to one or more water sources and to a pump, or to any other suitable system. The supplied water enters the apparatus in one or more places and circulates around, but not in, the chambers and / or combustion areas of the apparatuses. In general, water does not enter the interior of the chambers and / or combustion areas of the appliances. The temperature of the water in each of these locations preferably varies from room temperature to about 126.66 ° C, and more preferred ranges from about 100.00 ° C to about 121.11 ° C, most preferably about 121.11 ° C. The water works to cool the various components of the appliances, such as the side walls of the chambers and / or combustion areas, which are hot, so that these components maintain their structural integrity while being exposed to high temperatures. In the absence of this water (or other cooling agents or methods), some of the components of the appliances may lose their structural integrity at the high temperatures used. During this cooling process, the circulating water is transformed into a superheated steam product or a saturated saturated steam product. Because the superheated steam product or saturated dry steam product is usually collected for use in the generation of electrical energy (with an electrical generating device or system), additional water is usually added (water of replacement) to the devices to replace the water that is transformed into the product of super-heated steam or dry saturated steam product. A certain amount of the water originally used in the appliances (condensed and / or water that is not transformed into steam) can be collected and re-routed to the appliances for additional use in them. The water used in the apparatus preferably circulates through a plurality of tubes forming one or more tube assemblies, which preferably form the side walls (or a portion of the side walls) of each of the chambers and / or combustion areas of the appliances. The tubes are preferably circular or oval, but can be square, rectangular, triangular or in any other appropriate form. The more tubes used for water circulation, the larger the surface area of these tubes that will be present in the devices. The larger the surface area of these tubes that is present in the devices, the faster the water cools the various components of the devices in which the water is near (eliminating heat from the components), or with which It comes into contact, allowing the various components of the appliances to be exposed to more heat than would otherwise be possible without losing their structural integrity, and faster water is transformed into a superheated steam product or into a dry saturated steam product that can be used to produce electrical energy (or for some other use). The number of tubes that are preferably present in each of said one or more tube assemblies in the apparatuses is generally based on the outer diameter of the tubes and the internal diameter of one or more external housings which are generally they are adjacent to the outside of the tube assemblies. The outer diameter of the tubes in each tube assembly usually determines the number of tubes that can be assembled around the inner circumference of a corresponding outer housing. For example, if an outer housing that is adjacent to a tube assembly has an internal diameter of approximately 37.40 cm, and if the individual tubes in the tube assembly have an outer diameter of approximately 1588 cm, approximately 58 tubes are used in the tube assembly. tube assembly (to cover the inside diameter of the outer housing). The number of tubes that is preferably used in a particular tube assembly in connection with a particular combustion chamber or area of the apparatus can be readily determined by one skilled in the art. The pH of the water used in the process and apparatus of the invention preferably ranges from about 8.5 to about 12.7, more preferred from about 10.5 to about 11.5. An external treatment of the water used in the processes and apparatuses to improve its quality before use may include clarification, filtration, softening, de-alkalization, demineralization, deaeration and / or heating as is known in the art. Depending on the type of water (hard water, soft water, fresh water, seawater, and the like) that is available at the site of use of the procedures and appliances, it may be desirable to add commercially available chemicals, such as phosphates, chelates , carbonates, sulphites (sodium sulfate and the like), alkalinity improvers, amines (diethylhydroxylamine and the like) and / or polymers, to water before use in an amount, as is known in the art, to reduce or eliminate impurities, such as such as calcium and iron minerals, chemicals and organic matter, water and, thus, reduce or prevent the corrosion of the components of the appliances. The hardness of calcium and magnesium, migratory iron and copper, colloidal silica and other contaminants should preferably be reduced or eliminated. It is also preferable to remove oxygen, carbon dioxide and other non-condensable gases from the supply water, to avoid the formation of deposits in the water transport tubes, which causes the water passages to narrow. Over time, water passages can be blocked, it. that causes a loss of efficiency (for example, that a higher amount of pressure is required to produce the same amount of heat), malfunction or loss of function. Solv (Lancaster, TX) sells industrial water treatment compounds that can be used to inhibit scale and corrosion or otherwise treat the water prior to use in the methods and / or apparatus of the present invention.

Combustion processes The combustion process is an exothermic reaction between fuels and oxidants. Combustion chemistry relates potential chemical energy to the heat that results from chemical reactions, and thermodynamics relates heat to work. Perfect combustion ("stoichiometric combustion") is obtained by mixing and burning exactly the right proportions of fuel and oxygen in such a way that no reactants remain (so that there is a complete combustion reaction in which there is no excess of oxidant or gas) . If too much oxidant is supplied (or not enough fuel), the mixture will be "poor in fuel". If a lot of fuel is supplied (or not enough oxygen is supplied), the mixture will be "fuel rich". A fuel-rich mixture usually results in "incomplete combustion" because all the fuel particles combine with a certain amount of oxygen, but oxygen can not get enough oxygen to burn completely. The environmental contaminants that are often generated in combustion processes include CO, S02, NOx, SOx, N02, N20, VOCs, hydrocarbons and particulate matter. CO and hydrocarbons are usually the products of incomplete combustion. S02 and SOx are usually emitted as a consequence of burning fuels containing sulfur compounds. The NOx, N02 and N20 are generated from the reaction of nitrogen compounds contained in a fuel with oxygen, or from a fuel with air. The formation of particulate matter can be a consequence of a high ash content in the fuel.

In procedures and apparatus, the mass flow rates of the reactants multiplied by the combustion time usually provide the total mass required of each reactant. The 0 / F mixing ratio (the ratio of oxidant to mass flow rates of fuel) can be determined using the following equation: m0 r = pif in which the "•" above the m indicates the speed of m, or dm / dt, in kg / second. From the 0 / F mixing ratio, the total mass flow rate of the reactant can be calculated: • • • m = m0 + nif The fractional flow rates of each component can be calculated using the following equations: The volumetric flow rates can be calculated from the mass flow rates by dividing their densities, which are known. For example, LOX has a density of 1.2 g / cm3.

Cameras and / or combustion areas The chambers and / or combustion areas used in the apparatuses, in which one or more combustion reactions occur, preferably have an interior and an exterior facing away from the empty interior. These chambers and combustion areas are preferably round, elongated, cylindrical, hollow tubes having an open front end and an open rear end, and having side walls formed by tube assemblies. However, these may be in any other appropriate form, such as with an oval, round, triangular, square or conical shape. In addition, the front and / or rear end of the combustion chambers and / or areas may be closed by one or more other components of the apparatuses, as shown in figures 1 to 3. For example, in figures 1 and 2, the front end of the first combustion chamber is closed with a first transfer injector plate and a first oxidant distributor plate, and the rear end is closed with a fuel wear plate and a first distributor plate Water. During the procedures, and in the apparatuses, of the invention there are presented at least two, and preferably three (or more), separate combustion processes, of which a first partial combustion of fuel is presented in a first chamber (or area) of combustion, a second partial (or a complete first) combustion of fuel occurs in a second chamber (or area) and, optionally, when a complete combustion reaction does not occur in a second chamber (or area), a third complete combustion is presents in a third chamber (or area) of combustion. It is possible to add additional combustion chambers (or areas) to the apparatuses of the invention, or add additional combustion reactions to the methods of the invention. Because the fuel used in the methods and apparatuses of the invention is likely to be more dissociated into its constituent atoms, thereby reducing the amount of environmental contaminants in the outgoing combustion gas exhaust products, such as CO, whose production it is reduced when a more complete combustion of a fuel occurs, when three (or more), instead of two, separate combustion processes occur, it is preferable that the three (or more) separate combustion reactions occur during such use. The last combustion reaction (in the last chamber or combustion area used) should result in the complete combustion of the fuel, and each previous combustion reaction (in each chamber or pre-combustion area) should result in incomplete combustion of the combustion. gas. As discussed above in the present invention, it is preferred that the fuels, or fuel components, and oxidants that are used in the methods and apparatus of the invention are introduced into the first chamber or area and into the additional chambers or areas of combustion of the apparatus at angles that tend to induce a whirlpool effect in the chambers or combustion areas, which promotes the mixing of fuels or fuel components, and oxidants that is more complete than would otherwise occur otherwise (without swirling action). When appliances and methods are used, it is preferred that combustion, which occurs first in the first combustion chamber, occurs along the entire length of the appliances (in each of the chambers and / or combustion areas). present), instead of being present only in some of the chambers or combustion areas of the appliances. It is also preferred that, in each of the two or more combustion chambers (or areas) of the apparatuses, the combustion reaction occurs along the entire length of the combustion chambers (or areas), rather than it happens along smaller portions of them. Also, it is preferred that at least about 97% of the fuel (or mixture of fuel or other mixture) is burned, and most preferably all (100%) of the fuel, which is used in the methods and apparatus of the invention. , and the high temperatures used in these processes and devices allow the fuel to be dissociated from molecules to atoms, such as H and O, with the remaining molecules H20 and C02 (so that the exhaust product of combustion gas that exits of the last chamber or combustion area of the apparatus contains atoms and molecules that are preferably not environmental contaminants and / or hazardous materials, such as CO, NOx, N02, N20, SOx and / or S02. which results in a reduction in the amount of emissions of environmental pollutants, and used in the manner described in the present invention.It is recommended that precautions be taken in the processing of the exhaust product of combustion gas that is produced in the last chamber or combustion area of the apparatuses of the present, which can be extremely hot (at a temperature that frequently varies from about 1371.11 ° C to about 3037.77 ° C, and most commonly vary from 2037.77 ° C to 2760.00 ° C). This product of combustion gas exhaust can be allowed to escape into the atmosphere. Alternatively, it could be subjected to a cooling process, for example, in a steam generator for recovering residual heat (or another generator), or in a similar apparatus. The atoms of the combustion gas exhaust product (depending on the type of fuel or fuel components used), when cooled to a temperature below approximately 110 ° C, can be re-associated as molecules. Some of these molecules, such as carbon monoxide, can be dangerous. Others may cause corrosion to metal components. Therefore, it is preferred that the temperature of the flue gas exhaust product is maintained at a temperature of 110 ° C or higher. The combustion reactions that occur in each of the chambers and / or combustion areas of the appliances release large amounts of heat. Therefore, in order to avoid damage to the various chambers or combustion areas (the potential melting of the metal and / or loss of structural integrity), it is preferable that the side walls of each of the chambers and combustion areas employed in the apparatuses they are cooled in an active way, for example, using water or another refrigerant or appropriate method. In appliances, it is preferable that water be used as a coolant to achieve this result. However, the water is not injected into any of the combustion chambers or areas, and does not come into contact with the fuel or oxidizer reactants, or with the flue gas exhaust product. In contrast, water may be present in tubes contained in tube assemblies which generally form the side walls (or portions thereof) of the chambers and / or combustion areas.

Ignition Devices In the methods and apparatus of the invention one or more means may be used to initiate a combustion reaction of a fuel mixture of one or more fuels, or fuel components, and oxidants to produce heat release, the which may be the same or different. The release of chemical energy stored in fuels, or fuel components, with the use of one or more oxidants can be initiated by a number of different methods, or by using a number of different ignition devices, known to the person skilled in the art. technique. The selection of one or more appropriate ignition systems depends on the nature and phase of the fuels, or fuel components, and oxidants used, the safety of the system and similar considerations. However, all ignition methods and devices have a common priority objective, which is the rapid and reliable ignition of fuels, or fuel components, and incoming oxidants prior to the accumulation of reactive material. Fuels and oxidants entering one or more of the combustion chambers or areas that do not ignite rapidly can cause explosive mixtures to form and explode. The ignition devices used in the processes and apparatuses can obtain energy from an external source, or from an amount of energy stored internally. Once ignited, fuel and oxidants usually remain in ignition. Therefore, although it is possible, it is not necessary to maintain the operation of an ignition source throughout the entire operation of the methods and apparatus. Ignition devices that may be used in the methods and apparatus of the invention, with or without the use of catalysts, and which may be incorporated in, assembled or otherwise attached to the apparatus include: (a) devices for pyrotechnic ignition (electrically initiated slow burning pyrotechnic torches typically having a burn duration in the range of about 2 to about 10 seconds); (b) hyperbolic ignition devices (ignition devices that spontaneously burn when the fuel and oxidant meet for the first time); (c) spark plugs (ignition devices that produce a spark); (d) spark ignition ignition devices (devices in which small amounts of fuel and oxidant are supplied to the interior of a combustor of ignition devices, and that are ignited by electric sparks, and the exit of the flame is grooved towards the required area and, in turn, ignites the fuel and oxidant used in the main combustion processes); (e) combustion wave ignition devices (ignition devices having branch outlets that provide multiple point ignition sources from a single pre-combustor, and having an electrical spark that initiates combustion in a premix chamber ); and (f) resonance ignition devices (ignition devices that use a pressurized gaseous fuel flow to create resonance heating that can ignite reagents in the ignition device, which causes the ignition device to escape, with or without an increase of the oxidant, which are used to ignite the oxidant fuel as they enter a combustor).

Non-polluting products Conveniently, the methods and apparatuses of the present invention produce products, such as a super-heated steam product, a dry saturated vapor product and / or a flue gas exhaust product, which usually They are environmentally clean. Each of these products usually does not contain (0% by weight), or contains low amounts (preferably less than about 40% by weight), more preferred less than about 30% by weight, even more preferred less than about 20% by weight, more preferred even less than about 10% by weight, and even more preferably less than about 5% by weight) of environmental contaminants and / or hazardous materials. When one or more of the products produced by the methods and appliances contain some amount of one or more environmental contaminants and / or hazardous materials, such as C02, the amount of these one or more environmental contaminants and / or hazardous materials is generally reduce significantly compared to procedures and appliances that use fuel to produce steam or electric power that use air, or that allow air to come in contact with the fuel, oxidant or water used in them, with the combustion gases or combustion gas products produced in this manner, and / or with components thereof (combustion chambers and the like), including conventional methods for producing steam or electrical energy, such as methods of production of electric power and steam production that they use carbon and natural gas, when: (a) the same fuel is burned, and the same amount e fuel; (b) the same fuel is burned, and the same amount of steam, power or electrical energy is produced; or (c) one of the fuels of the invention is used in the processes or apparatuses. In situation (c), emissions of environmental contaminants and / or hazardous materials will generally be lower than in situations (a) and (b) as a result of the use of one of the fuels of the invention. However, in each of the situations (a), (b) and (c), the amount of said one or more environmental contaminants and / or hazardous materials is generally reduced by at least 50% approximately, and most commonly by at least 75% approximately, and even more commonly at least in 90% approximately. Example 1, which is indicated below in the present invention, shows a 97% reduction of C02 when EF-15 and LOX are employed in an apparatus of the invention as compared to the use of coal in a conventional coal-burning plant .

The type and amount of any environmental contaminants and / or hazardous materials that are produced by the methods and apparatus of the present invention generally depend on the purity of the fuels, or fuel components, and the oxidants used, the type of the fuels, or fuel components used, the number and type of combustion reactions (incomplete or complete) that arise and the characteristics of the particular method or apparatus employed, and can be readily determined by the person skilled in the art. Without taking into account the above variables, the amount of environmental contaminants and / or hazardous materials that are produced by the methods and apparatus of the present invention will generally be significantly lower than the amount of environmental contaminants that are produced by methods and apparatus. that use fuel to produce steam or electrical energy that uses air, or that allow the air to come into contact with the fuel, oxidant or water used in them, with the combustion gases or with the products of combustion gas that are produced in this way, and / or with components thereof (combustion chambers and the like). The super-heated steam product or dry saturated steam product that can be produced by the methods and apparatus of the present invention, which are generally two of the main products that can be produced in this manner, usually do not contain (0%) none of the environmental contaminants or hazardous materials. In addition, the combustion gas exhaust product that is produced by the methods and apparatus of the present invention, which is generally the other of the two separate products produced by these methods and apparatuses, often contains only water and dioxide of coal and, possibly, some metals (if metals are initially present in the fuel or fuel components). The combustion of fuels, or fuel components, and oxidants at high temperatures, and in the multiple combustion reactions, generally described in the present invention, cause environmental contaminants that are otherwise present in the exhaust products of combustion gas that will be eliminated (or that will be reduced significantly). For example, if rubber from old tires is used as the sole fuel in the methods and apparatus of the invention, rubber usually becomes water and carbon dioxide. Also, the additional (separate) steam that can be generated through heat transfer from the exhaust product of combustion gas that is produced by the procedures and appliances, for example, if they are allowed to enter a boiler or steam generator for recovery of residual heat, as shown in figure 14, instead of being released into the atmosphere, they generally do not contain (0%) environmental contaminants. This is because, in contrast to many other methods and apparatuses for producing steam, power or energy, the flue gas exhaust product produced by the methods and apparatus of the invention does not generally come into contact with the product. steam. If any of the environmental contaminants and / or hazardous materials are produced by the methods and / or apparatuses of the invention, these usually exist in the flue gas exhaust product that is produced in the last chamber or combustion area, for example in the second combustion chamber if a third combustion area is not used, and usually depend of the elements present in the particular fuels used. In general terms, the amount of said environmental pollutants and / or hazardous materials will be less than the amount of environmental contaminants and / or hazardous materials present in a flue gas exhaust product that is produced by combustion of the same fuel (or a different fuel), and the same amount thereof, in a conventional apparatus, installation or method that uses fuel, such as a conventional power plant or a conventional coal-burning boiler, many of which use air as the oxidant and / or burn fuel incompletely, as measured in kg of contaminant per million standard cubic meters, in tons per year, in the nominal value of the emission factor, or by any other appropriate method. Said amount generally ranges from about 0 to about 5% by weight, and preferably ranges from about 0 to about 3% by weight, and even more preferably ranges from about 0% to about 1% by weight. For example, if natural gas is used as the fuel in a process or apparatus of the invention, the only components that are generally present in the combustion gas exhaust product produced will be water vapor (H20) and C02 molecules. Water vapor is not hazardous and is not a contaminant, and C02, which is not an air pollutant by titration, can be captured and used as described in the present invention. Furthermore, depending on the fuels or fuel components used, the methods and apparatus of the present invention generally do not produce, or significantly reduce the amount of NOx or mercury (in the exhaust product of flue gas leaving the last chamber or combustion area of the appliances). These methods and devices can generally achieve up to 100% reduction in emissions of these environmental pollutants or hazardous materials compared to conventional methods to produce energy, electricity or steam (any type) that generate environmental contaminants and / or hazardous materials , such as power plants that use coal. Also, depending on the fuels or fuel components used, the methods and apparatus of the invention generally do not produce, or significantly reduce the amount of other environmental contaminants and hazardous materials (in the flue gas exhaust product that it leaves the last chamber or combustion area and elsewhere), including NO, N02, N20, NH3, SOx, S02, CO, HCl, CH4, VOCs, benzene, hydrogen fluoride, hydrogen sulfide, poly- aromatics, hexachlorobutadiene, ethylene dibromide, dioxin, arsenic, uranium, thorium, radium, radon, polonium, bismuth and lead, other carcinogenic, mutagenic and / or radioactive substances and particulate matter compared to other methods and devices for producing energy, electricity or steam (any type) that generate environmental pollutants and / or hazardous materials, such as conventional power plants that use coal. For example, compared to a conventional coal-burning power plant, the methods and apparatus of the present invention generally reduce the emissions of the above environmental pollutants and hazardous materials by at least about 50%, preferably at least 75% approximately, and even more preferred at least 90% approximately up to 100% approximately. Therefore, the amount of air pollution that is produced by the methods and apparatus of the present invention is generally significantly reduced or eliminated in comparison with air pollution caused by conventional energy production., electricity or steam, such as the methods used by conventional power plants that use coal. The combustion gas exhaust product that is produced in the final (ultimate) combustion chamber or area by the methods and apparatus of the present invention is generally environmentally clean, and preferably contains a quantity of environmental contaminants and / or hazardous materials ranging from about 0 to about 30% by weight, most preferably from about 0 to about 7%, and even more preferably from about 0 to about 1% by weight of the flue gas exhaust product. In addition, some environmental contaminants, such as C02 and S02, that could be produced, depending on the fuel or fuel components used, can be recovered using conventional methods and equipment. For example, when hydrogen is used as the fuel in the methods and apparatus of the invention, the only products that are usually present in the flue gas exhaust product are heat and water. Therefore, the flue gas exhaust product usually has 0% environmental contaminants and hazardous materials. The super-heated steam product or dry saturated steam product usually also has 0% environmental contaminants and hazardous materials. Many energy producing companies use coal as fuel in their procedures and appliances. A typical 500 MW power plant that uses coal produces 3,500 million kilowatt hours of electric power per year. To produce this amount of electrical energy, the power plant needs to burn approximately 1.43 million tons of coal per year. The following table compares the amounts of environmental pollutants and / or hazardous materials sulfur dioxide, nitrogen oxides, carbon dioxide, carbon monoxide, arsenic, bromine, cadmium, small particles (in particulate matter), ash and slag produced by year for a power plant that uses coal that burns 1.43 million tons of coal per year and that in theory can be predicted to be produced by one of the apparatuses of the present invention that produces the same amount of electric energy using the designated fuel EF-10, which can have an energy value of approximately 17582.4 kcal / kg.

Contaminants from the combustion of 1. 3 million tons of fuel This table shows that, when the same amount of electrical energy is produced, the methods and apparatus of the present invention do not produce sulfur dioxide, nitrogen oxides, carbon monoxide, arsenic, lead, cadmium, or matter. in particular, neither ash, nor slag, and approximately 15 times less carbon dioxide, which reduces the total amount of environmental pollutants and / or hazardous materials produced by approximately 94%, compared to a conventional coal-burning power plant. In contrast to many conventional methods for producing electrical power, the apparatuses of the invention usually do not require the use of any devices or systems for contamination control, such as an air pollution control device, to maintain the products of the appliances (for example one or more steam products and flue gas exhaust products) environmentally clean.

Capture, separation and use of C02 Optionally, up to 90% (or more) of the C02 produced by the methods / apparatuses of the invention can be captured and separated from the other components, such as H20, using conventional methods and equipment. Methods for this include chemical absorption techniques using a solvent, such as a monoethanolamine, physical absorption, cryogenic distillation and / or membrane separation. For example, Wittemann Company, LLC (Palm Coast, FL) sells systems and equipment for C02 recovery that extracts C02 from products, such as malodorous gases, and cleanses C02 to a desired or required level of purity using techniques such as sulfur removal, activated charcoal and N0X techniques, depuration, dehydration, liquefaction and washing, the resulting C02 can then be liquefied and used in the cryogenic grinding process described in the present invention, or it can be sold to a variety of end users.

Conversion of water to a superheated or saturated saturated steam product The methods and apparatus of the present invention convert the water that is introduced into the apparatus out of the chambers and / or combustion areas into a superheated steam product or saturated dry which may contain super-heated steam, dry saturated steam and / or both types of steam in one or more places. The super-heated steam, dry saturated steam and / or combination of the two vapors may leave the apparatus at one or more sites (through one or more superheated steam outlet means) and travel to a central collection device. of super-heated steam product or other device. The super-heated steam and the dry saturated steam can be separated, optionally, using conventional steam separation equipment, and can be used (each separately or together) to produce electrical energy, for example, in a steam turbine. Generally speaking, when superheated steam and dry saturated steam travel to a turbine (or other electrical generating device) together, the metal passages leading to the turbine draw a certain amount of energy away from the superheated steam. heated and dry saturated steam, which causes both types of vapors to drop their temperatures. However, super-heated steam usually gives its energy back to dry saturated steam. Steam often carries tiny drops of water with it. Steam quality is described by its "dryness fraction", which is the proportion of completely dry steam in the steam that is being considered. The steam becomes "wet" if the droplets of water in suspension are present in the vapor space, without having specific vaporization enthalpy. "Wet steam" has a caloric content substantially lower than that of dry saturated steam at the same pressure. The tiny drops of water in the wet steam have weight, but they occupy an insignificant space. The dryness fraction of the steam usually depends on the design and capacity of the particular steam production apparatus. The super-heated steam has several important properties that make it ideal for work and for mass transfer. First of all, the super-heated steam is totally dry steam, which is beneficial because, when the carrying of water occurs in a combustion apparatus, for example a boiler or generator, although the water can be removed from the steam (with steam separators and / or steam traps), the separation of water from steam remains complex. However, if a small amount of overheating is added to the steam, the hauled water can be vaporized to absolutely dry steam. This eliminates the potential for wet steam to damage turbines and other energy generating equipment. Secondly, although the superheated heat presents a drop in temperature as it gives up its super heat, the superheated steam can lose heat without condense. When the super-heated steam yields a certain amount of its enthalpy, it does so by virtue of a drop in temperature. No condensation occurs until the saturation temperature of the steam is reached. In contrast, saturated steam can not lose heat without condense. Saturated steam easily condenses on any surface that is at a temperature lower than that of saturated steam, and yields evaporation enthalpy, which is the highest proportion of its energy content. Therefore, as saturated steam passes through the long distribution mains, it loses some heat through the pipe and insulating material, which results in a certain amount of saturated steam condensing therein. The resulting water, if not removed, can cause erosive damage to pipes, valves, heat exchange equipment, turbines, and similar equipment. In contrast, there are no condensates in the distribution mains that contain superheated steam. In addition, heat that is slightly super-heated can be transported through long pipes without losing enough heat to condense, thereby eliminating the danger of damage. As the vapor pressure rises, the total available heat rises. If the pressure is reduced through the valves, additional heat is available in the lower pressure steam. The pressure reduction generates a small amount of super-heat in this vapor.

The primary reason for producing super heat in the procedures and apparatus is to achieve a safe and efficient transfer of work energy in a wide variety of applications that require the generation of powerful forces, such as pumps, turbine engines and other generating equipment. of power. As the steam enters a turbine, it is allowed to expand to work through an increased speed while releasing its heat. In contrast, saturated steam condenses as its heat is lost. The material condensed in a turbine reduces the space available for steam to enter. This reduces the availability of energy for work, and can damage the turbine, especially when it comes out at a high speed. Therefore, in these applications, superheated steam is preferred, because it can expand, yielding its excess heat without condense. Depending on the desired working energy efficiency and energy requirements, the superheat may or may not be allowed to condense in the turbine. In high-speed light rotor turbines, the fragility of rotor blades, and steam flow rates, often require dry steam operation. In any case, the operation of the turbine using superheated steam is more efficient than using dry saturated steam. Because the superheated steam may not be present in the apparatus of the invention at start-up, valves that are opened manually (or other valves) at this point in operation to remove the water may be used (because usually there is time to open and close the valves). However, emergencies such as loss and deviation of superheater could require operation with saturated steam. During such unscheduled potential stoppages, there is no time to manually open the valves. Therefore, steam traps can be used instead to drain the condensate. In the system shown in Figure 14, these steam traps can be placed in one or more places, as is known in the art, to ensure the production and transport of the highest quality of steam. For superheat conditions an appropriate inverted bucket steam trap is preferred. During start-up, large pipes can be started from cold conditions. At low pressures in the pipes and water pipes there can only be saturated steam (until the temperature of the pipe is increased). This is preferably achieved through a time interval (for example less than about 5 minutes) to avoid stresses on the lines. Typical start loads can be calculated as follows in which: C = amount of condensate (in kg); W = total weight of the tube (in kg); ti = vapor temperature (in ° C); t2 = room temperature (in ° C); and H = latent heat of the vapor (in kcal / kg). With respect to the variable H, for extended heating times, the total heat of the saturated steam must be used at the supply pressure of the superheated steam minus the sensible heat of the saturated steam at the average pressure during the heating time involved. The chemical energy contained in the hydrocarbon or other fuels, or fuel components, which are used in the apparatuses of the invention is converted into heat energy when fuels are burned. The thermal energy is transmitted through the side walls of the chambers and / or combustion areas to the water that is preferably in the tube assemblies. The temperature of the water increases from the thermal energy until the saturation point of the water is reached (that is, until it boils). This thermal energy that raises the water temperature is the "enthalpy of liquid". At the boiling point, the water is called "saturated water". The heat transfer continues from the side walls of the chambers and / or combustion areas to the water. The additional enthalpy ("evaporation enthalpy") produced by this heat transfer does not generally increase the water temperature, but evaporates the water, converting it into steam. As a result of the release of a super-heated or saturated dry high-energy and high-quality steam product that is produced by the high temperature combustion processes that occur in the different chambers and / or combustion areas of the apparatuses of the invention, and of the water circulating near each of these chambers and / or combustion areas, the apparatuses transform the water into a super-heated or saturated dry high vapor product. energy and high, efficient purity, generally at least at the sites of each of the different chambers and / or combustion areas, as shown in Figure 1. The temperatures used in the methods and apparatuses of the present invention are high that steam usually becomes a super-heated or saturated saturated steam product in an essentially instantaneous manner. The superheated or saturated saturated steam product is then piped through one or more superheated steam product outlet means to one or more superheated steam product collection devices. From these collection devices, the steam product is usually transported to electrical energy generating devices, such as steam turbines, where the energy in the form of super-heated steam and / or dry saturated steam is converted into mechanical energy . Mechanical energy drives the energy generating device, which, in turn, produces electricity. The amount of steam produced by the methods and apparatus of the present invention may vary, depending on the size of the particular apparatus used. An apparatus such as the one described in example 1 can produce from about 853.52 kg / h to 16571 kg / h of dry saturated steam, and from about 7409.28 kg / h to about 14119.4 kg / h of superheated steam, to the temperatures and pressures described in the example. This preferably produces approximately 16555.5 kg / h of dry saturated steam, and approximately 14102.1 kg / h of superheated steam, which can generate approximately 10 MW of electricity per hour. The per hundred by weight of superheated steam and dry saturated steam in each superheated or saturated saturated steam product that is produced by the methods and apparatus of the invention usually depend on the particular temperatures and pressures used, and may to be easily manipulated by the person skilled in the art using, for example, temperature and / or conventional pressure relief valves in one or more diverse locations in the apparatuses. The vapor product produced by the methods and apparatus of the present invention generally contains from about 0 to about 100% by weight of dry saturated steam, and from about 0% to about 100% by weight of superheated steam. Preferably, the vapor product contains 100% by weight of superheated steam. If the superheated or saturated saturated steam product that is produced using the methods and apparatus of the invention contains dry saturated steam, it is preferred that the weight percent of the dry saturated steam in the superheated steam product be no greater than 76% by weight approximately (the remainder being generally super-heated steam), and more preferably not more than about 30% (the remaining usually being super-heated steam). The dry saturated steam can be separated from the super-heated steam using conventional steam separation equipment. If any amount of water and / or wet steam is initially present in the products that are produced using the methods and / or apparatus, the water and / or wet steam can be separated from the saturated saturated steam and / or superheated steam using equipment conventional, such as desiccators.

Production of steam using the combustion gas exhaust product The exhaust product of hot combustion gas leaving the last chamber or combustion area of the apparatus of the invention is preferably attached to another source of water, such as a boiler conventional, or a residual heat recovery steam generator, as shown in Figure 14 in which the flue gas exhaust product can be cooled to a temperature of about 110 ° C or higher and thus produce a separate vapor product (separate from the super-heated or saturated saturated steam product produced by the apparatus), which may contain any combination in any percentage by weight of the above types of vapor. The various types of vapor in this vapor product can then be separated from each other in such a way that different types of steam can be used separately in various applications. Any super-heated steam or dry saturated steam produced is usually used as described above. Any wet steam that is produced preferably is transported to an overflow area and condenses. This can then be discharged to a containment basin or recirculated to the hydrocarbon combustion gas generator and used as make-up water. The thermal energy produced using the methods and apparatus of the present invention can also be used for steam absorption, water cooling, drying, heating and the like, including quadri-generation (simultaneous or consecutive generation of energy, steam, cold water and / or hot water, etc.). The purity of the vapor product (vapor purity) that can be produced using the flue gas exhaust product leaving the final combustion chamber or area of the appliances of preference is less than about 1.0 ppm total solids, and more preferably it is less than about 0.1 ppm total solids. A combustion gas exhaust product that is produced using the present apparatus having a configuration as shown in Figure 1, and which is an independent unit with dimensions of approximately 3,048 to 4,267 meters in length, 0.610 to 0.914 meters wide and 1,524 meters high, and having a bypass to a steam generator for recovery of waste heat, such as that shown in Figure 14, can generate from approximately 10 to approximately 15 MW of electricity (in addition to the electricity that can be generated by the steam that is produced using the apparatus). The exhaust products of combustion gas that is produced by larger appliances, and that have a bypass to steam generators by recovery of waste heat, can produce quantities of electrical energy greater than approximately 10 to approximately 15 MW of electricity (in addition to the electricity that can be generated by the steam produced by the apparatus).

Size, type and transport capacity of the appliances The appliances can be produced in any size and / or desired or convenient way that can produce the desired results, and their size can be scaled to suit a wide variety of industrial applications. , such as the generation of electric power independent of the distribution network of electric power, emergency electric power in standby state, for example, during a network failure of power distribution, use during peak usage times, portable far-site electrical power, electric power for steam trains, electric power for boats and similar applications. The devices can be used to provide electrical power to factories and hospitals, in power parks, and inside and / or outside buildings. The apparatuses of the invention, which preferably do not have, or have a few moving parts, can be compact, and conveniently can be autonomous generating systems (independent) or complementary generation systems (complementary to, or integrated with, some other type of a system or appliances) for the efficient production of a sufficient quantity of reliable electric power for maximum power demand and uninterrupted electrical users. The devices can be installed and serviced easily, in which removable parts that can be easily replaced are compatible with conventional power generation systems, and can be re-adapted into existing power generation systems that have boilers exhausted or obsolete. A preferred hydrocarbon combustion gas generator of the invention, which can generally produce from about 5 to about 30 MW of electricity per day, is an independent unit having dimensions of approximately 3048 to 4,267 meters in length, 0.610 a 0.914 meters wide and 1.524 meters high (including legs of 0.1914 meters), and which is placed on a concrete slab (or other durable material) that has approximate dimensions of 3,048 meters long by 3,048 meters wide. Said hydrocarbon combustion gas generator may require from about 3.75 to about 100 times less space than that of conventional electric power plants, while producing approximately the same amount of electrical energy as conventional power plants. For example, in order to produce around 25 MW of energy per day, power plants that use coal, natural gas, nuclear, wind, and geothermal can require several times more surface than a plant that includes the generator of combustion gas described above. Optionally, two or more of the apparatuses can operate together in parallel. For example, three 15 MW combustion gas generators can be positioned and run together to produce 45 MW of energy.

The sizes of the various components of the appliances can vary widely, depending on the sizes of the complete appliances. Conveniently, the apparatus can be easily transported from one site to another site using, for example, trucks, trains, or boats. Because most of the mechanical parts of vessels, such as their engines, are powered by steam energy, the apparatus of the present invention can be used on boats to allow vessels to remain off shore for periods of time. of time longer than what might otherwise be possible. Likewise, all the hydrocarbon waste materials generated in the vessels can be used as a fuel in the apparatus, which provides means to reduce these hydrocarbon waste materials without returning to the mainland or emptying them in the sea, and eliminating or reduce the need for fuel to be taken to the boat from the mainland.

Absence of corrosion Because the exhaust products of combustion gas that is produced by the methods and apparatus of the present invention usually do not leave towards (or otherwise come into contact with) turbines, condensers or other generating equipment of electrical energy, and because the methods and apparatus of the invention generally produce from about 90 to about 99% by weight of dry steam (dry saturated steam and / or super heated steam), instead of wet steam, these methods and apparatuses conveniently do not generally cause corrosion (dissolution and / or wear of parts, such as metal blades, and / or the production of an accumulation of substances, such as rust, in or on the parts ) or other damage or destruction to the turbines, condensers and other electrical energy generating equipment, or to the components thereof.

Ease and speed of start-up Many systems or power plants and / or steam generators, conventional that use fuel, such as nuclear power plants, require prolonged periods of start-up, for example of at least 24 hours, and complex procedures, so that they are fully operational after their operation begins, either initially and / or after a scheduled or emergency stoppage of operations. In contrast, the apparatuses of the present invention usually only require a range of about 30 minutes or less, and more commonly a range of about 5 minutes or less, and often a period of about 10 seconds or less, and of procedures that are not complex, to be fully operational after startup. Therefore, the devices can produce products that can be used in the generation of electrical energy and at the same time virtually do not have, or have small intervals only, interruption of the electric power service, probably saving money, time and / or inconveniences for users of electric power.

Amount of electrical energy produced The apparatuses of the invention are preferably independent generators with continuous operation capacity (24 hours / day, 7 days / week). In addition, more than one device operates in one place at the same time. The methods and apparatus of the present invention preferably produce from about 5 to about 600 MW of electric power per day, more preferably producing from about 100 to about 200 MW of electric power per day. Therefore, for example, working at a cycle of approximately 60% (a capacity of 60%), a 10 MW device can produce approximately 6 MW / day of electrical energy. When more than one device is operated in one place at the same time, increasing the performance of the other devices, the remaining device or apparatus can keep the entire system running at 100% if one of the devices does not work. To maximize efficiency and produce the cleanest possible products with the methods and apparatus of the present invention, air is preferably not allowed to enter the system and heat losses from the system are minimized. The processes and apparatuses have a combustion efficiency that generally varies from approximately 50% to approximately 100% (producing thermal energy using at least 50%, and up to 100%, of the kcal present in the particular fuel or components of fuel used therein), more preferably from about 70% to about 100%, even more preferred from about 90% to about 100%, even more preferred from about 95% to about 100%, and even more preferred from 97% approximately up to 100%. In other words, for every 25.2 kcal present in the fuels used in these processes and apparatuses, preferably at least about 12.6 kcal, more preferred at least about 25.2 kcal, they are converted into thermal energy (and the remainder is converted into heat). residual). In contrast, the combustion efficiency of conventional power plants that use coal reaches a maximum of about 33% with approximately 67% of the potential energy of the coal that is lost as waste heat. The combustion efficiency of power plants that use conventional natural gas is approximately 35-50%, with approximately 50-65% of the potential energy of the gas lost as waste heat. The methods and apparatus have a thermal efficiency that generally ranges from about 50% to about 87%, most preferably from about 65% to about 87%., still more preferred from about 75% to about 87%, even more preferred from about 80% to about 87%, and even more preferred from about 84% to about 87%. In contrast, the thermal efficiency of power plants is approximately 34%. The thermal performance of these plants is approximately 2520 kcal of heat of fuel burned per kilowatt hour (kWh) of electricity produced. Also, in contrast to the apparatuses of the present invention, those plants are generally slow at startup or to change the performance while they are in operation.

Electricity production costs When waste materials are used as fuels or fuel components, and dumping fees and / or other revenue generating fees are obtained by the user of waste materials, such cost is usually reduced additionally, and they are reduced significantly compared to the costs of producing electricity through other methods, such as through power plants that use conventional coal, natural gas, fuel cells or nuclear energy. Under these circumstances, the methods and apparatus of the present invention can produce electric power at a total cost ranging from about 0.003 F of dollar to about 0.009 of dollar per kilowatt hour. The total low costs to produce electrical energy that can be achieved using the procedures and appliances are generally less than the total costs to produce electricity through other methods and appliances, due to: (a) the high combustion efficiency that can be achieved with the methods and apparatus of the invention; (b) the use of fuels such as carpet waste, which can be obtained easily at no cost; (c) receipt of waste disposal fees (recycling) for the use of certain hydrocarbon waste materials, such as old tires, as fuels; (d) the income generated by the sale of electricity; (e) the income generated by the sale of components of waste materials, such as metal from old tires, to other markets; and / or (f) the income generated by the sale of components of the exhaust gas product, such as ash, nitrogen, C02 or S02, to other markets.

Co-generation, tri-generation and quadri-generation The methods and apparatus of the invention can be used in a co-generation system, in a tri-generation system, in a quad-generation system and in similar systems, or they can be used in a conventional way to generate heat and electric power separately.

Temperatures, pressures and times Procedures and appliances produce a superheated steam product or a saturated steam product under conditions (eg, flow rates, temperature and pressures of fuel oxidant and water in different places) that can vary, depending of, for example, the size of the particular appliance, whether or not one or more appliances are used together, the desired combustion efficiency, the diameters of the inlets and outlets for water, fuel and oxidant, the diameters of the outlets for the steam product, etc. The conditions can be varied to achieve the desired objectives as is known in the art.

Purging the apparatus It is preferable that before and after operating the apparatus, it is purged with an inert gas, such as nitrogen. The purge must provide safety checks that: (a) none of the components of the appliances, such as the fuel supply or oxidizer pipes, are clogged; (b) all the components of the appliances are functioning properly; (c) the interiors of the appliances are clean (free of residues, such as fuel or oxidant residues, residual vapors and the like); and / or (d) there are no leaks.

Destruction of hazardous materials Depending on the type of hazardous materials, procedures and appliances can also be used to safely, quickly, inexpensively, efficiently and completely destroy some hazardous materials. (converting said materials into non-hazardous materials) either without producing unwanted environmental contaminants, or with the production of said contaminants at a level that is below the level of contaminants that are produced by conventional methods to destroy hazardous materials, and without placing hazardous materials in landfills, bodies of water, or other receptacles. When hazardous materials are used as fuels or fuel components in the methods and apparatus of the present invention, hazardous materials are generally completely destroyed by dissociation to non-hazardous components. For example, when using polyvinyl chloride as a fuel, the resulting products (a flue gas exhaust product and / or a separate vapor product that is produced using the flue gas exhaust product) usually does not contain any carcinogen. The transformation of hazardous materials into non-hazardous materials by the methods and apparatuses of the invention appears to be the result of a combination of the use of high temperatures and pressures, and of the absence of air in the processes and apparatuses. (The procedures and appliances use temperatures that are approximately twice as hot as the temperatures used in most power plants that use coal). Therefore, the procedures and apparatus can be used, for example, by the military and health industries, to transform hazardous materials into non-hazardous materials. Hazardous materials that are to be transformed into non-hazardous materials in accordance with the procedures and appliances can serve as fuel or fuel components in these procedures and appliances, without the need for additional fuels or fuel components. However, one or more fuels, or additional fuel components may also be optionally used.

Materials The various components of the apparatus can be manufactured using a wide variety of different metals or ceramic materials. However, the metals and ceramic materials used preferably have suitable mechanical characteristics, ability to resist oxidation, corrosion and stress, and the ability to withstand the high temperatures described in the present invention. Unless otherwise specified in the present invention, all the various components or other parts of the apparatus are preferably made from ferritic and / or austenitic steel. The chambers and / or combustion areas and heat exchangers used in the processes and apparatuses may be formed from any suitable, high conductive, high temperature metals, such as nickel, chromium, cobalt, or alloy alloy steel. nickel or copper, such as BeCu, Cu, Ag-Cu, or a combination thereof, or can be coated with a refractory material, such as molybdenum, tungsten, tantalum, or the like, for elevated vapor temperatures. All the materials, components and equipment used to carry out the present procedures or to manufacture the devices can be obtained commercially. Sources for these items include, for example, Pechiney Chemicals Division (Stamford, CT), Praxair, Inc., (Danbury, CT), and Airgas, Inc. (Radnor, PA).

DETAILED DESCRIPTION OF THE INVENTION Preferred Modes of the Invention For the purpose of illustrating the methods, apparatuses, uses and methods of manufacture of the present invention, the drawings show various views of a preferred embodiment of the apparatus and its use in a tri-generation system. The various components or parts of the preferred embodiment of the apparatuses may be arranged generally in the manner shown in the drawings, or described later in the present invention, or in some other way. The invention is not limited to the arrangements, configurations, dimensions, instrumentation, components, angles, reactants or directions of product flow or precise conditions shown in the drawings or described in the present invention. These arrangements, configurations, dimensions, instrumentation, components, angles, reactants or directions of product flow and / or conditions may differ as circumstances require or as desired. For example, you can use a few inputs, or additional inputs, fuel and fuel chambers, tubes, orifices, etc. Also, these components can be arranged differently. One, two, three, four or more additional chambers and / or combustion areas may also be included. It is also possible to vary the location of the various components of the apparatus and the means to secure the parts together. Likewise, several components can be formed integrally for a unitary structure, instead of joining two parts together. For example, the sixth inlet of superheated steam product can be attached to the third superheated steam product outlet distributor by any suitable means for joining these two components of the apparatuses together. Alternatively, the sixth inlet of superheated steam product and the third superheated steam product outlet distributor can be manufactured in one piece from a piece of material. Even several components, parts and / or areas of the apparatus may be permanently or removably attached with other components, parts and / or areas of the apparatus, and may be movable or immovable. Compounds and parts attached in removable form are often preferred because said components and parts can generally be replaced more easily and cost-effectively as needed.

Description of a preferred apparatus A preferred embodiment of the combustion apparatus of the present invention is described with reference to the drawings. In these drawings, all references, numbers and descriptions referring to superheated steam products can be applied in the same way to dry saturated steam products. In Figures 1 to 3, there is shown a hydrocarbon combustion gas generator ("generator") 8. The generator has two separate combustion chambers (a first combustion chamber 70 and a second combustion chamber 100), as well as a third combustion area 120, in which three separate combustion reactions occur (a first incomplete combustion reaction, a second incomplete combustion reaction and a third complete combustion reaction). The oxidant and the fuel reactants generally flow from left to right in the generator shown in these figures (from upstream to downstream, and from the front end to the rear end of the generator). The generator has no moving parts. Figures 4-13 show cross-sectional and / or detailed views of some of the individual components of the generator 8 shown in Figures 1 to 3. As shown in Figures 1 to 3, many of the components, parts and / or areas of the generator 8 are preferably present in more than one site in, or on, the generator 8, both above and below the various chambers and / or combustion areas. Therefore, any description in the present invention concerning a component, part and / or area of the generator must refer to all the same types of components, parts and / or areas that may be in or on the generator. For example, any description of a first water dispenser 51 applies to both of the first water dispensers 51 shown in Figure 1 (one shown above and one shown below the first combustion chamber 70). The first combustion chamber 70 and the second combustion chamber 100 are each preferably hollow cylindrical tubes having side walls formed by tube and / or tube assemblies and open front and rear ends. The forward ends of the first combustion chamber 70 and the second combustion chamber 100 are defined by other components of the generator 8 (a first oxidant distributor plate 40 and a second transfer injector plate 84, respectively). The rear end of the first combustion chamber 70 is formed by another component of the generator 8 (a fuel wear plate 63). The rear end of the second combustion chamber 100 is open (it has no wall or other barrier), and is connected to the open front end (which does not contain a wall or other barrier) of the third combustion area 120. The third area of combustion 120 is also preferably a cylindrical hollow tube. The rear end of the third combustion area 120 is also open (it does not contain a wall or other barrier), which allows the exhaust product of the combustion gas that is produced in the generator 8 to come out of the generator 8 (e.g. to the atmosphere, a boiler, or a steam generator for recovery of exhaust heat), and is positioned in a manner that forms an angle in the opposite direction to the forward end of the third combustion area 120 (towards the outside environment), and far from the generator 8. One or more fuels or oxidants are injected at the front end of the first combustion chamber 70 at appropriate 0 / F mixing ratios, and under conditions of temperature, pressure and other conditions effective to produce a stable first combustion. partial (incomplete) of the fuels found in it. The combustion gas product that is produced in the first combustion chamber 70 as a result of the first combustion reaction flows under pressure into the second combustion chamber 100, in which additional oxidant is injected into the interior of the second combustion chamber 100, in an appropriate 0 / F mixing ratio, and under conditions of temperature, pressure and other conditions effective to produce a second partial (incomplete) stable combustion of the fuels that are in it. The product of combustion gas that is produced in the second combustion chamber 100 as a result of the second combustion reaction flows under pressure into the third combustion area 120, in which additional oxidant is injected into the interior of the third area of combustion 120, in an appropriate 0 / F mixing ratio, and under conditions of temperature, pressure and other conditions effective to produce a stable and final complete combustion of the fuels in the third combustion area 120 of the generator 8. The side walls of the first combustion chamber 70, the second combustion chamber 100 and third combustion area 120 are formed by separate pipe assemblies or tubes (a first tube assembly 71, a second tube assembly 101, a tube 121 and a third tube assembly 146, respectively) containing (with the exception of tube 121) one or more tubes, and preferably multiple tubes, containing circulating water ion (or other appropriate fluid). Preferably, the water circulation is conducted in a heat exchange relationship with each of the combustion gas products that are produced during the three different combustion reactions. The heat present in the combustion gas products generated during the three separate combustion processes is transferred through the tube and tube assemblies forming the side walls of the first combustion chamber 70, the second combustion chamber 100 and the third combustion area 120, thereby transforming the water into circulation in a super-heated or saturated saturated steam product (preferably in a plurality of different locations of the generator 8). The superheated or saturated saturated steam product that is produced is then collected in a conventional, and preferably central, collection device (not shown) or other utilization device. The superheated or saturated saturated steam product collection device can be connected to a steam turbine, or other electric power generating device or system (or other), for the subsequent production of electrical energy using the super steam product. -heated or saturated dry. An exhaust product of the hot combustion gas that is produced in the third combustion area 120 leaves the third combustion area 120, where it can be released into the atmosphere, or used for the production of an additional vapor product, separated. Conventional vapor separation equipment can be used to separate the various types of vapor that may be present in this separate vapor product.

One or more liquid, solid and / or gaseous fuels, fuel components or fuel mixtures, such as tire rubber subjected to reduction in size obtained from the grinding of the rubber from used tires to a fine powder, is extracted at starting from one or more fuel sources, such as a fuel storage tank, through one or more appropriate fuel supply control means, such as a flow control device regulated by a pump, or other appropriate device , inside a fuel inlet distributor 12, or inside other means to receive one or more fuels, fuel components or fuel mixtures. The flow control device used may be a pressure regulator, a venturi control of fluid in cavitation, a temperature sensing transducer, a pressure sensing transducer or other similar device known to the person skilled in the art. At its front end, the fuel inlet manifold 12 preferably has a flange or other means for securely connecting the fuel inlet manifold 12 with the flow control device. The means for connecting the fuel inlet manifold 12 with the flow control device is preferably a flank, which preferably contains one or more bolt holes, preferably spaced at equal distance, which allows uniform distribution of the pressure through the fuel inlet manifold 12. A person skilled in the art can easily determine the size, number and spatial distribution of the appropriate bolts / holes for a particular fuel inlet manifold 12 and a particular generator 8. Other secure connection means may be used, including welding, socket head screws, pressure, bolt fastening, riveting, epoxies or other adhesives, chemical bonding, heat sealing, and other methods / devices known in the art. The flow velocity of the fuels into the fuel inlet distributor 12 or entering the generator 8 in one or more other locations usually depends on several variables, including fuel density, mixing ratios 0 / F used, the diameter of the fuel flow control device used, the fuel pressure, and the amount of thermal energy produced by the generator 8. The 0 / F mixture ratio employed in the first combustion chamber 70 also depends on several variables, such as fuels, fuel components or mixtures of fuel and particular oxidants used, because certain fuels require more or less oxidant to consume the fuel. However, the flow velocity of fuels, fuel components or fuel mixtures entering the interior of the fuel inlet manifold 12 must be a velocity that allows a "fuel-rich" mixture of fuel and oxidant to be present in the fuel. the first combustion chamber 70. The skilled in the art can easily determine said speed, and a desirable 0 / F mixing ratio. As shown in Figures 1 and 2, one or more additional fuels, fuel components or fuel blends can be extracted from one or more fuel sources and travel to one or more fuel inlets 9, separate, optional , or other means for receiving one or more fuels, fuel components or fuel blends. The fuel inlets 9 preferably have one or more passages, or other means to allow the flow of fuels, fuel components or fuel mixtures, which are separate from the fuels, fuel components or fuel mixtures present in the distributor fuel input 12, and that lead to, and are adjacent to, the forward ends of one or more fuel chambers 10, separate, optional, or other means for housing and maintaining these fuels, fuel components or fuel mixtures separated from the other fuels. , fuel components or fuel mixtures in the fuel inlet distributor 12. Said configuration allows double, but separate, storage and injection (simultaneous or at different times) inside the first combustion chamber 70 of the generator 8 of one or more fuels, fuel components or mixtures of additional hydrocarbon fuel or other fuels, fuel components or fuel mixtures, which may be incompatible or compatible, and in the same or a different state (solid, liquid, gas, slurry, mixture, etc.), in which the fuels, fuel components or mixture s of fuel are chosen for use in the fuel inlet distributor 12. A second, third or other fuel, fuel components or additional fuel mixture that can increase the energy value of the first fuel, fuel component or fuel mixture. Additional fuels, fuel components or fuel blends can enter the interior of the fuel inlets 9, and can be injected into the first combustion chamber 70 of the generator 8, in the same manner or in a different manner from that of fuels, fuel components or fuel mixtures that enter the interior of the fuel inlet 12. For example, if you want to use two fuels or fuel components in the generator 8, and the fuels or fuel components chosen to be used are gasoline and styrene foam particles, the two fuels or fuel components are usually not compatible because gasoline can melt the styrene foam particles, which prevents the particles from being injected properly into the first combustion chamber 70. However, the configuration of the generator 8 shown in figures 1 and 2 it may allow the above incompatible fuel and / or fuel components to be used in the generator 8 at the same time. In another example, plastic particles can be used as a fuel or fuel component in the fuel inlet manifold 12 while the hydrogen gas is used as a second fuel or fuel component in the fuel inlets 9 and fuel chambers 10, providing the combination of fuel or fuel components in the first combustion chamber 70 having an energy value of approximately 22,200 kcal / kg of fuel, which is higher than the energy value that could be present if the plastic particles They are used as the only fuel. Alternatively, a liquid, gaseous or solid refrigerant, such as water, a fuel, an oil, vapor, a powder or any other substance or material, or a combination thereof, having appropriate cooling properties can enter into a more of the fuel inputs 9 from a coolant source. A conventional "film cooling" technique can be used by injecting the refrigerant from the fuel inlets 9 into one or more fuel chambers 10 in a radial manner, which causes the refrigerant to flow into the first fuel opening tubes. 36 in the generator 8, whereby the first fuel opening pipes 36 are cooled. Said one or more fuel chambers 10, which function as a second fuel distributor inside the fuel inlet manifold 12, can be drilled inside the fuel inlet distributor 12, preferably at the rear end, or can be placed inside the fuel inlet manifold 12 in another appropriate manner. The fuel inlets 9 can be connected to a fuel source as described for the fuel inlet manifold 12. These can be attached to the fuel inlet manifold 12 by any appropriate means for securing them to the fuel inlet manifold 12, as described in the present invention with respect to the union of the fuel inlet manifold 12 with the flow control device. The rear end of the fuel inlet manifold 12 is preferably attached to the forward end of a fuel meter block 30 with means for securely joining these two areas of the generator 8 to each other, such as one or more first attachment devices. Alternatively, the rear end of the fuel inlet manifold 12 can be welded to the front end of the fuel meter block 30. Any means or device for securely attaching the fuel inlet manifold 12 to the meter block can be used. of fuel 30, including the methods and devices described above in the present invention for the union of the fuel inlet manifold 12 with the flow control device. Preferably, the rear end of the fuel inlet manifold 12 contains a connecting device, such as the connection device described above in the present invention for the front end of the fuel inlet manifold 12, which preferably has one or more bolt holes therein (as described above in the present invention for the flange of the fuel inlet manifold 12). The first attachment devices 14 may be any suitable devices for securely joining the two components of the generator 8 together, such as high strength bolts with nuts and accompanying lock washers as required, socket head screws and other similar devices. known in the art. The first attachment devices 14 can be varied to provide a secure connection of the fuel inlet manifold 12 to the fuel meter block 30. The rear end of the fuel meter block 30 is preferably attached to a first oxidant distributor 41, a first oxidant distributor plate 40 and a first water distributor 51 with means for securely attaching these four areas of the generator 8 to each other, such as one or more second joining devices 31. The second joining devices 31 can be any devices that are suitable for securely joining or otherwise securing these generator areas 8 to each other, such as those described above in the present invention for the first attachment devices 14. Preferably, the trailing end of the meter block of fuel 30, the first oxidant distributor 41, the first oxidant distributor plate 40 and the front end of the first water distributor 51 each have one or more bolt holes therein. Those skilled in the art can choose the type and number of second attachment devices 31 to provide a secure connection of the fuel meter block 30 with the first oxidant distributor 41, the first oxidant distributor plate 40 and the first water distributor. 51. The rear end of the fuel meter block 30 is attached to the forward end of the first oxidant distributor 41, and the rear end of the first oxidant distributor 41 is attached to the forward end of the first oxidant distributor plate 40. The end of the first oxidant distributor plate 40 is attached to the forward end of the first water distributor 51. As shown in Figure 2, the fuel meter block 30 has a receptacle preferably machined at its front end. This receptacle must be of a size (length and width) that allows an injector wear plate 32 to fit securely within the front end of the fuel meter block 30. The fuel meter block 30, a first oxidant inlet 42 and the first oxidant distributor plate 40 preferably each have one or more flare tube mounting holes 29a present therein, preferably at an angle (at an angle leading from one or more means for start combustion of fuel and oxidant that are dosed into the first combustion chamber 70 (such as one or more ignition devices 20) towards the center of the first combustion chamber 70). The flare tube mounting holes 29a preferably have approximately the same diameter as that of one or more flare tubes 29 which are preferably inserted into these flare tube mounting holes 29a, and extending from the end of the mixing chamber 28 through the fuel meter block 30, the first oxidant inlet 42 and the first oxidant distributor plate 40, which allows the flames to travel from the ignition devices 20 to the first chamber of combustion 70. Flame tubes 29 are inserted into these flare tube mounting holes 29a, and preferably are equally spaced (with equal distances between these) through these generator components 8. However, these may be Space or position in any other appropriate way. Preferably, packages or similar devices are placed between the rear end of the fuel inlet manifold 12 and the front end of the fuel meter block 30, and between the rear end of the fuel meter block 30 and the front end of the first fuel tank plate 30. oxidizer distributor 40 to prevent leakage of gases, heat or other substances in these areas. Optionally, a "0" ring groove can be machined in one or more of these components, such as the rear end of the fuel meter block 30, which allows the insertion of an "O" ring therein. The depth and width of the "0" ring should be based on the maximum allowable operating pressure (MAOP). The "O" rings and / or gaskets used throughout the generator 8 are preferably suitable for high temperature and pressure applications as is known in the art. The injector wear plate 32 is preferably designed to allow one or preferably a plurality of first fuel opening tubes 36, or other means for measuring the fuel into the first combustion chamber 70, can be inserted in removable form within one or preferably a plurality of first fuel openings 34. The size of the first fuel openings 34 and of the first fuel opening pipes 36 can be varied as desired, depending on for example the type of fuels and particle sizes used in solid fuels. The first fuel openings 34 are drilled, or otherwise processed, using conventional methods through the injector wear plate 32, the fuel meter block 30, the first oxidant distributor plate 40 and the first plate of transfer injector 44, providing a series of hollow holes (first fuel openings 34) extending through each of these generator components 8, leading from the rear end of the fuel inlet manifold 12 towards the front end of the first combustion chamber 70. The forward end of the first transfer injector plate 44 is attached to the trailing end of the first oxidant distributor plate 40. Any means or device for joining safely can be used., but preferably removable, the first transfer injector plate 44 to the first oxidant distributor plate 40, which includes the methods / devices described above in the present invention for the union of the fuel inlet manifold 12 with the device of flow control. The number of first fuel openings 34 used in the generator 8 is preferably the same as the number of first fuel opening tubes 36 used, and can be varied as is known in the art in accordance with the type of fuel and the ratio of mix 0 / F selected. The diameter of the first fuel openings 34 must be a diameter that allows the first fuel opening tubes 36 to be easily removably inserted within the first fuel openings 34, and which can be securely fitted within the first fuel openings 34 during the operation of the generator 8. The first fuel opening tubes 36 inserted within the first fuel openings 34 must allow an oxidant to fuel ratio (ratio 0 / F) that allows the mixture of said one or more fuels and one or more oxidants that are mixed in the first combustion chamber 70 is rich in fuel. Because the oxidants preferably circulate through the fuel meter block 30 around the first fuel opening pipes 36, the first fuel openings 34 and the first fuel opening pipes 36 (and other components of the generator 8 that come into contact with oxidants) should preferably be made from austenitic steel, which is compatible (not deteriorated by) with most oxidants. The first fuel opening tubes 36 are inserted into the front end of the injector wear plate 32, and through the fuel meter block 30, the first oxidant distributor plate 40 and the transfer injector plate 44. As As a result of the pressure applied to the fuel, the fuel is dosed from the front end towards the rear end of the fuel inlet distributor 12, and then from the front end towards the rear end of each of the first fuel opening pipes. fuel 36 in the generator 8, wherein the pressure causes the fuel to be injected from each of the first fuel opening pipes 36 into the front end of the first combustion chamber 70. One or more oxidants, such as LOX , are extracted from one or more sources of oxidant, for example, storage tanks of oxidant, through control devices d and appropriate flow by means of a pump or other appropriate device, into a first oxidant inlet 42, or into other means for receiving oxidant, which are preferably made from austenitic steel. The flow control device may be the same type of flow control device described above in the present invention for fuel sources. The flow rate of the oxidant entering the first oxidant inlet 42 can be varied as is known in the art to achieve a fuel-rich mixture of oxidant and fuel in the first combustion chamber 70. The oxidant entering the first oxidant inlet 42 preferably has a temperature ranging from about -183 ° C to about 27 ° C, more preferred from about -120 ° C to about -101 ° C, even more preferred about -46 ° C. The oxidant flows into the first oxidant inlet 42 under pressure, and this pressure causes the oxidant to flow upwardly into the interior of the first oxidant distributor 41, or into other means to measure the oxidant into the interior of the oxidant. the first combustion chamber 70. The first oxidant distributor 41 is located between the fuel meter block 30 and the first oxidant distributor plate 40. The first oxidant distributor 41, which is preferably made from austenitic steel, directs the oxidant through one or more first oxidant injector ports 46 at the rear end of the first oxidant distributor 41, and around the first fuel opening tubes 36 preferably in a radial form. The first fuel opening tubes 36 and / or the first oxidant injector orifices 46 are preferably oriented in the generator 8 in an angled manner which causes the fuel and oxidant being measured into the first chamber of combustion 70 form one or more collision points, as shown in Figures 4, 5 and 11. The pressure causes the oxidant to be injected from the first oxidant injector ports 46 through the aligned holes in the first plate. of transfer injector 44 towards the interior of the first combustion chamber 70, in which the oxidant is mixed with said one or more fuels that are also dosed therein for the first combustion reaction. A triplet collision current pattern can be formed from the fuel and oxidant being injected into the first combustion chamber 70 by the first fuel opening tubes 36 and the first oxidant injector ports 46 shown in Figures 4 and 11. The first oxidant injector orifices 46 are also preferably made from austenitic steel. The number of first oxidant injector orifices 46 used in the generator 8 may depend on the type of oxidant used and the desired 0 / F mixture ratio. The optimum number of first oxidant injector ports 46 for a particular oxidant and a particular 0 / F mixing ratio can be readily determined by one skilled in the art. The oxidant has a dual purpose when it is in the first oxidant distributor 41. It travels into the first combustion chamber 70 for a first partial combustion reaction of the fuel, and the latter cools the rear side of the first plate. transfer injector 44, which is heated from the first combustion reaction in chamber 70. The first transfer injector plate 44, which is also preferably made from austenitic steel, transfers the heat generated by the first combustion process to the excess oxidant that does not enter the first oxidant injector orifices 46, causing this excess oxidant to heat up (generally vaporizing a liquid oxidant). The excess hot oxidant preferably flows under pressure into an oxidant transfer tube 49, or into other means to receive the excess oxidant, which are also preferably made from austenitic steel, and then from Preferably, it is directed under pressure to the third combustion area 120. Alternatively, the oxidant flowing in the oxidant transfer tube 49 may be vented (released into the atmosphere) or may flow into another combustion chamber or area. The oxidant flowing into the third combustion area 120 is usually in a semi-liquid / gas state (if the oxidant used is a liquid) or in a gaseous state (if the oxidant used is a gas) as a result of the heat transfer from the first transfer injector plate 44 to this oxidant. The fuel is dosed through the first fuel opening tubes 36, and the oxidant is dosed through the first oxidant injector ports 46, at a desired 0 / F mixing ratio, and each preferably at a angle, which allows a vortex to form from the fuel flow and oxidant flow. The incoming fuel and oxidant, which cause a fuel-rich mixture of oxidant in the first combustion chamber 70, it is then ignited by one or more ignition devices 20 (two are shown in figure 1), causing the first partial combustion of the fuel in the first combustion chamber 70. Although the order can be varied, it is preferred that the ignition 20 is working, which produces a spark that causes a fireball to extend from the front end of the ignition device 20 through the flame tube 29 into the first combustion chamber 70, before dosing the fuel and oxidant to the interior of the first combustion chamber 70. It is also preferable that the fuel be dosed into the first combustion chamber 70 before dosing the oxidant into the first combustion chamber 70. Said one or more devices of ignition 20 which preferably are used in the generator 8 have an ignition device housing 26 which is preferably attached to the n securely to the front end of the fuel meter block 30 by suitable means for joining these two components of the generator 8 together, such as by welding or other means of attachment described in the present invention. Said one or more ignition devices 20 used in the generator 8 are preferably electronic ignition device systems comprising: (a) an ignition device housing 26 for housing the various components of the ignition device 20; (b) a fuel inlet of the ignition device 22 to allow fuel from a fuel source to enter the interior of the ignition device 20; (c) an oxidant inlet of the ignition device 24 to allow the oxidant from an oxidant source to enter the interior of the ignition device 20, and which is preferably made from austenitic steel; (d) a mixing chamber 28 for mixing the fuel and oxidant used in the ignition device 20; and (e) a flame tube 29 for a flame to propagate from the ignition device into the interior of the first combustion chamber 70. The flame tube 29 preferably extends from the front end of the ignition device 20 to the front end of the first combustion chamber 70. The rear end of the ignition device housing 26 is preferably attached to the front end of the fuel meter block 30. The fuel inlet of the ignition device 22 and the oxidant inlet of the ignition device 24 are preferably each connected to one or more fuel and oxidant sources, respectively, such as fuel storage tanks and oxidant (not shown), and each are securely attached to the front end of the fuel housing. ignition device 26. One or more fuels or oxidants for use in ignition devices 20 are pumped (or from some ot the flow of fuel into the fuel inlet of the ignition device 22 and into the oxidant inlet of the ignition device 24, respectively. The fuels or oxidants used in the ignition device may be the same or may be different from the primary oxidant fuels described in the present invention. Preferably, two to four electronic ignition devices 20 are used, and each ignition device preferably causes a flame to propagate from the front end to the rear end of the flame tube 29, and the flame then enters the inside of the flame. first combustion chamber 70. Preferably, the flow of oxidant and the fuel flow used in the ignition devices 20 intersect in the central area of the mixing chamber 28. Preferably, the flames flowing from the various tubes of Flame 29 intersects at one or more points, pipes or common areas in the first combustion chamber 70. The fuel and oxidant flowing within the mixing chambers 28 of the ignition devices 20 are preferably ignited by an electronically generated spark. in ignition devices 20. Flames that are produced by igniting the fuel and oxidant mixture are propagated Then, the flame tubes 29 are received inside the first combustion chamber 70. Once the fuel and oxidant are metered into the first combustion chamber 70 by the first fuel opening tubes 36 and the first injector orifices of oxidant 46, respectively, the resulting mixture of fuel and oxidant in the first combustion chamber 70 is ignited, initiating the first partial combustion process in the first combustion chamber 70. Once the combustion reaction in the first combustion chamber begins. combustion 70, preferably the operation of the ignition devices 20 is terminated, so that sparks no longer occur, and the flow of oxidant to the interior of the mixing chambers 28 is terminated. One or more thermal detectors may be used. internal or external, or other similar devices known to the person skilled in the art, in various places in / on the generator 8 to detect the start of the combustion process in the first combustion chamber 70, and to deactivate the ignition devices 20 and stop the flow of oxidant and / or fuel into the mixing chambers 28.

The temperature and pressure used in the first combustion chamber 70 are regulated to allow an incomplete combustion of said one or more fuels present therein. The oxidants and fuels entering the first combustion chamber 70 are preferably mixed and burned at temperatures and pressures which cause each of these to vaporize at least partially to a gaseous state, or in some other way remain in a gaseous state, during this first combustion process. The temperature in the first combustion chamber 70 can be easily controlled by those skilled in the art by selecting a 0 / F mixing ratio that corresponds to the particular types of fuels used therein to achieve this result. The pressure in the first combustion chamber 70 can be regulated by controlling the pressures of the fuels and oxidants that are dosed into the first combustion chamber 70 from the first fuel opening tubes 36 and the first oxidant injector orifices 46. , respectively, and the diameters of the orifices from which they are dosed into the interior of the first combustion chamber 70. The temperature in the first combustion chamber 70 preferably ranges from about 1200 ° C to about 5800 ° C, and most preferred way ranges from about 1400 ° C to about 1500 ° C. The pressure in the first combustion chamber 70 preferably ranges from about 35 kg / cm2 gauge to about 105 kg / cm2 gauge, and more preferably ranges from about 42 kg / cm2 gauge to about 63 kg / cm2 gauge. Using commercially available computer programs, and other readily available information, one skilled in the art can easily vary the temperatures and pressures used in each of the various components and / or areas of the apparatuses of the present invention, such as the first chamber. of combustion 70, the second combustion chamber 100 and the third combustion area 120, to achieve a desired result (e.g., incomplete or complete combustion of the fuel). Information describing various aspects of the combustion and heat transfer processes (including information on the relationships between pressures and temperatures of the fuel, oxidant and combustion chamber, fuel and oxidant flow rates and mixing ratios 0 / F) , and about various metals generally suitable for use in combustion apparatuses, is known in the art. See, for example, Huzel et al., Modern Engineering for Design of Liquid Propellant Rocket Engines (Vol. 27, Progress in Astronautics and Aeronautics, American Institute of Aeronautics and Astronautics, Washington, D.C. 1992); Sutton, Rocket Propulsion Elements, an Introduction to the Engineering of Rockets (6th Ed., John Wiley &Sons, Inc., New York, 1992). The information describing the operation of conventional industrial steam generators and boilers is known in the art. See, for example, Ganapathy, Industrial Boilers and Heat Recovery Steam Generators Design Application and Calculations (Marcel Dekker, Inc., New York, NY, 2003); Ganapathy, Steam Plant Calculations Manual, second edition, Revised and Augmented (Marcel Dekker, Inc., New York, NY, 1994). Commercially available computer thermochemical software, such as GUIPEP software, CQE ™ software, GNOCIS ™ software, PEOA GNOCIS ™ software, CET software (Chemical Equilibrium with Transport Properties, NASA TM4557), Smart software, can be used. ® (Emerson, St. Louis, MO), the POWERlinkRTU software (Abbey Systems, Salt Lake City, UT), the FASTFLOW and CONDENS computer programs (MPR Associates, Inc., Alexandria, VA) to determine the various temperatures, pressures, and flow rates of fuel and oxidant to be used in the methods and apparatus of the present invention for one or more fuels., fuel components or mixtures of fuel and particular oxidants. These computer programs can also provide analysis of the exhaust product of combustion gas that exits the exhaust system of the appliances when particular fuels and oxidants are used. The amount of time that said one or more fuels remain in the first combustion chamber 70 is an amount of time that allows them to experience incomplete (partial) combustion, which often occurs in a period ranging from about 0.025 to about 10 seconds. However, the period in which the fuels, fuel components or fuel blends (or mixtures with oxidants) remain in any of the chambers or combustion areas of the generator 8 may vary depending on the temperature in a particular combustion chamber or area. , the speed at which fuels are injected into the chamber or area, the length of the chamber or area and the amount of swirling action that fuels experience in the chamber or area. The higher the temperature, the faster the speed of the fuels, the shorter the length of the chamber or area and the lower the swirling action of the fuel, the shorter the time period of the fuel (or fuel components) or mixtures of fuel and oxidant) generally remain in a particular combustion chamber or area. All the materials in the first combustion chamber 70 are generally maintained under turbulent conditions, and are caused to pass to a flow state by the combustion reaction that occurs in the first combustion chamber 70. When a fuel or component The fuel used in the first combustion chamber 70 is a solid, the fuel or solid fuel component will generally be at least partially converted to a combustion gas therein by this process. The swirling action that preferably occurs in the combustion gas product that is generated in the first combustion chamber 70 generally, and conveniently, allows the fuels, fuel components or fuel mixtures to have a more homogeneous mixing with said one or more oxidants, and the combustion gas product remaining longer in the first combustion chamber 70 than would happen without said swirling action, or what would typically happen in a conventional boiler or steam generator. In the first combustion chamber 70, the hydrocarbons of said one or more fuels will generally be more complex than what they are in the second combustion chamber 100, where they experience another incomplete (partial) combustion reaction, or in the third combustion area 120, where they experience even a third combustion reaction. For the same reasons, the hydrocarbons in said one or more fuels will also generally be more complex in the second combustion chamber 100 than they are in the third combustion area 120, where they are also dissociated (degraded). A combustion gas product that is produced in the first combustion chamber 70 is the result of an incomplete combustion of fuel in the first combustion chamber 70. The amount of fuel burned in the first combustion chamber 70 preferably varies from more from about 0% to less than about 100%, and more preferably ranges from about 20% to about 70%, and even more preferred is about 50%. This usually contains combustion gases and partially burned fuel, which is still rich in fuel, and which may contain environmental contaminants and / or hazardous materials (depending on the type of fuels used) in this stage of the process as products of this Incomplete combustion reaction (because only incomplete fuel combustion occurs at this stage of the procedure), as well as oxidant. A fuel wear plate 63, which is shown in detail in Figure 2, which is adjacent to the rear end of the first combustion chamber 70 is preferably designed to allow one or preferably a plurality of second orifice tubes of fuel 66, or other means for dosing fuel within the second combustion chamber 100, can be removably inserted within one or preferably a plurality of second fuel ports 65, which are shown in detail in figures 6 at 10 and 12. The fuel wear plate 63 is preferably made from a hard metal, such as one of the commercially available metals A-2, A-7, H-13, or S-7, which They allow resistance to wear and abrasion, as well as resistance to tempering at elevated temperatures. This generator component 8 is designed to be removed and replaced as necessary. Using conventional methods, the second fuel openings 65 are pierced through, or in some other way placed within, the fuel wear plate 63, a first water distributor plate 60 having its front end attached to the end. rear of the fuel wear plate 63, a supply water dispenser 64 having its front end attached to the rear end of the first water distributor plate 60, a second oxidant distributor 82 having its front end attached to the end rear of the supply water distributor 64, a second transfer injector plate 84 having its front end attached to the rear end of the second oxidant distributor 82, and a second oxidant distributor plate 80 having its front end attached to the end of the second transfer injector plate 84, supplying one or more hollow holes (second openings). fuel 65) extending through each of these generator components 8, and leading from the rear end of the first combustion chamber 70 towards the front end of the second combustion chamber 100. The size and number of the second fuel openings 65 and the second fuel opening tubes 66 can be varied widely in the manner described above in the present invention for the first fuel openings 34 and the first fuel opening pipes 36. The number of second holes of fuel 65 is preferably the same as the number of second desired fuel orifice tubes 66, and can be varied in a manner known to the person skilled in the art in accordance with the type of fuel, fuel components or fuel mixtures and the 0 / F mixture ratio used. The diameter of the second fuel openings 65 must be a diameter that allows the second fuel opening tubes 66 to be inserted in an easily removable form within the second fuel openings 65, and to remain secure in the second fuel openings 65 during operation of the generator 8. The second fuel orifice tubes 66 inserted within the second fuel openings 65 must also allow a 0 / F ratio that allows the mixture of said one or more fuels, fuel components or mixtures of fuel and said one or more oxidants that are mixed together in the second combustion chamber 100 is fuel rich. Because the oxidant is preferably circulated around the second fuel opening tubes 66, the second fuel openings 65 and the second fuel opening tubes 66 must also be made from austenitic steel. The second fuel port tubes 66 are inserted removably into the front end of the plate of fuel wear 63 and extend through the various components described above through the second transfer injector plate 84. The first water distributor plate 60 preferably has a flange containing holes for bolts spaced at equal distances for its connection to the second oxidant distributor plate 80. The combustion gas product produced in the first combustion chamber 70 is moved by the pressure present therein., which is caused by the combustion process that occurs therein, from the front end to the rear end of the first combustion chamber 70. This is then dosed from the front end to the rear end of the second tubes of fuel opening 66 and the interior of the second combustion chamber 100. The second fuel orifice tubes 66 preferably cause the product velocity of the combustion gas that is produced in the first combustion chamber 70 to increase, depending on the diameter of the second fuel opening tubes 66. However, the fuel-rich combustion gas product entering the interior of the second combustion chamber 100 often enters the second combustion chamber 100 at a higher linear velocity of 2199.44 m / s-kg (3280 ft / s-lb). The combustion gas product entering the second combustion chamber 100 is preferably supplied and mixed with one or more additional oxidants, which may be the same as or different from the oxidants entering the first combustion chamber 70, and which are ready to cause another combustion reaction, this time in the second combustion chamber 100 (by the spontaneous combustion of the fuel that is present in the combustion gas product), in an amount that causes a second incomplete combustion (partial ) of the fuel present in the second combustion chamber 100, and that preferably keeps the fuel and oxidant in a fuel rich mixture. The 0 / F mixing ratio used in the second combustion chamber 100 also generally depends on several variables, such as the particular fuel and oxidant employed. Depending on the chemical composition of said one or more fuels, fuel components or particular fuel mixtures used, some fuels require more or less oxidant to consume the fuel. The amount of additional oxidant that is mixed with the fuel entering into the second combustion chamber 100, and a desirable 0 / F mixing ratio, can be readily determined by one skilled in the art. The additional oxidant, such as LOX, which is added in the second combustion chamber 100 is extracted from an oxidant source, such as an oxidant storage tank, through an appropriate flow control device by a pump or another device within the second oxidant inlet 81, or within other means for receiving additional oxidant, which is preferably made from austenitic steel. The flow control device may be one of those described above in the present invention for the fuel inlet manifold 12, or a similar device known in the art. The flow rate of the additional oxidant entering the second oxidant inlet 81 can be varied to achieve a fuel-rich mixture of oxidant and fuel in the second combustion chamber 100. The additional oxidant that enters the second oxidant inlet 81 also preferably has a temperature comparable to that of the oxidant entering the first oxidant inlet 42. The additional oxidant enters the second inlet of oxidant 81 under pressure, and this pressure causes the oxidant to flow into the second distributor of the oxidant. oxidant 82 (in detail in Figure 9), or within other means for dosing additional oxidant into the interior of the second combustion chamber 100, which is located between the water supply distributor 64 and the second transfer injector plate 84 (in detail in Figure 10), and preferably around the second fuel opening tubes 66 in a radial manner. The second oxidant distributor 82, which is preferably made from austenitic steel, directs the additional oxidant through one or more of the second oxidant injector orifices 85 located at the rear end of the second oxidant distributor 82. The pressure causes the additional oxidant to be injected from the second oxidant injector orifices. , which are also preferably made from austenitic steel, inside the second combustion chamber 100, where this is mixed with the fuel present therein (or entering the interior of the second combustion chamber 100) for the second combustion reaction. The number of second oxidant injector orifices 85 desired depends on the types of oxidants the 0 / F mixture ratio used inhibits. The optimum number of second oxidant injector orifices 85 for one or more particular oxidants, and for a particular O / E ratio, can be readily determined by one skilled in the art. The second fuel ports 65, the second fuel opening tubes 66 and the second oxidant injector ports 85 are shown in greater detail in Figures 7 to 10 and / or in Figure 12. The second oxidant injector orifices 85 are shown in detail in Figure 13. The oxidant has a dual purpose when it is present in the second oxidant distributor 82. This provides oxidant to the second combustion chamber 100 for a second partial fuel combustion reaction. Additionally, it cools the rear side of the second transfer injector plate 84, which is heated from the second combustion reaction that occurs in the second combustion chamber 100. The second transfer injector plate 84 it is also preferably made from austenitic steel, and transfers the heat generated by the second combustion process to the excess oxidant that does not enter the interior of the second oxidant injector orifices 85, heating this excess oxidant ( generally vaporizing a liquid oxidant). This hot excess oxidant flows under pressure into the oxidant transfer tube 49, and is then directed under pressure into the third combustion area 120. Alternatively, the oxidant flowing in the oxidant transfer tube 49 is can ventilate or direct to a different chamber or combustion area (when more than three chambers or combustion areas are used in generator 8). The oxidant flowing into the third combustion area 120 is usually in a semi-liquid / gas state (if the oxidant used is a liquid) or in a gaseous state (if the oxidant used is a gas) as a result of the heat transfer from the second transfer injector plate 84 to this oxidant. A second superheated steam product outlet 67, or other means for a saturated superheated or dry steam product to exit the generator 8, is preferably aligned with the supply water distributor 64, or with other means for circulating water around the second fuel opening tubes 66 and providing cooling of the front and rear ends of the second fuel openings 65, and with a second water inlet 62, or with other means for receiving water in the generator 8 The cooling water is transformed into a super-heated or dry saturated steam product, and then exits the generator 8 through the second super-heated steam product outlet 67, or through other means to allow the steam leave the generator 8. The second outlet of superheated steam product 67 is joined to the water distributor plate 60 by any suitable means for securely joining to these generator components 8 together, such as by welding, or using a JTC or AN trim with flange, and preferably by welding. The rear end of the water distributor plate 60 is preferably attached to the forward end of the second oxidant distributor plate 80 with means for securely joining these areas of the generator 8 to each other., such as one or more third joining devices 61, which may be the same as those described above in the present invention in connection with the first connecting devices 14. The first water distributor plate 60 and the second distributor plate oxidizer 80 preferably have each, one or more bolt holes drilled therein (in the manner described above in the present invention in connection with the flange of the fuel inlet manifold 12) that are aligned with one another. The third attachment devices 61 can be any devices that are suitable for securely joining the anterior areas of the generator 8 together, for example, high strength screws with nuts and accompanying locking washers. The number of third joining devices 61 can be varied as is known in the art to provide a secure connection of these areas of the generator 8 to each other. The combustion gas product produced in the first combustion chamber 70 is dosed through the second fuel opening tubes 66. As shown in Fig. 9, the additional oxidant entering one or more of the second fuel inlets. oxidizer 81 is preferably dosed in a manner that allows a radial distribution of the additional oxidant around the second fuel opening tubes 66, and then through the second oxidant injector ports 85 (preferably at the same speed and volume for all the second oxidant injector orifices 85) at a desired 0 / F mixing ratio, and each preferably at an angle, which allows a vortex to be formed from the fuel flow and oxidant flow. The incoming fuel present in the combustion gas product is mixed with the additional oxidant, and preferably results in a fuel-rich mixture of oxidant and fuel in the second combustion chamber 100. The fuel then undergoes a second partial combustion in the second combustion chamber 100 at the specified 0 / F ratio (but preferably more complete compared to the first combustion process that occurs in the first combustion chamber 70). (If a third combustion process is not used during the processes, the second combustion process may alternatively be a complete combustion process (described later in the present invention)). Although the order can be varied, it is preferred that the product of combustion gas containing the fuel is dosed into the second combustion chamber 100 before dosing the oxidant into the second combustion chamber 100. The combustion gas that is produced in the second combustion chamber 100 as a result of this second combustion reaction preferably remains rich in fuel, and preferably contains a smaller amount of environmental contaminants and / or hazardous materials compared to the combustion gas product produced in the first combustion chamber 70 (as a result of the fuel undergoing a second separate combustion reaction). The combustion gas product resulting from the second incomplete (but almost complete) combustion process occurring in the second combustion chamber 100 then moves under pressure from the forward end towards the rear end of the second combustion chamber 100. This then flows into the third combustion area 120. The temperature and pressure used in the second combustion chamber 100 are regulated to allow a second incomplete combustion (a separate, additional, partial or incomplete combustion) of the fuel present therein. (in the combustion gas product). The additional oxidant and fuel are mixed and burned at temperatures and pressures that cause each of these to vaporize in a additional (they vaporize to a greater degree than the vaporization that occurs in the first combustion chamber 70) during this second combustion reaction. The temperature in the second combustion chamber 100 can be easily controlled by those skilled in the art by selecting a 0 / F mixing ratio that corresponds to the particular type of fuel used therein. The pressure in the second combustion chamber 100 can be regulated by controlling the pressure of the fuel and oxidant that are dosed into the second combustion chamber 100., and the diameters of the second fuel opening tubes 66 and the second oxidant injector orifices 85, respectively, from which they are dosed into the second combustion chamber 100. The temperature in the second chamber of combustion 100 preferably ranges from about 1650 ° C to about 3200 ° C, more preferred from about 2200 ° C to about 2500 ° C. The pressure in the second combustion chamber 100 preferably ranges from about 21 kg / cm 2 gauge to about 105 kg / cm 2 gauge, and more preferably ranges from about 35 kg / cm 2 gauge to about 70 kg / cm 2 gauge. The combustion reaction that occurs in the second combustion chamber 100 will preferably be close to the stoichiometric (from about 85% to about 95% of the stoichiometric) in its combustion pressure, but preferably does not reach the stoichiometric combustion (100 %) at this stage of the procedure. Using commercial computer programs or other available information, one skilled in the art can easily vary the temperatures and pressures used in the second combustion chamber 100 to achieve additional incomplete combustion of the fuel contained therein. The amount of time the fuel remains in the second combustion chamber 100 preferably is an amount of time that allows the fuel to experience additional incomplete (partial) combustion in the second combustion chamber 100, usually a varying period. from about 0.025 to about 10 seconds. However, the amount of time the fuel remains in the second combustion chamber 100 can vary depending on the temperature that is present in the second combustion chamber 100 and the speed at which the fuel is injected into the interior of the second combustion chamber 100. The higher the temperature, and the faster the fuel speed, the shorter the period of time in which the fuel remains in the second combustion chamber 100. All the materials present in the second chamber of combustion 100 also usually remain under turbulent conditions, and are caused to pass into a state of flow by the combustion reaction occurring therein. When one or more of the fuel or fuel components is a solid, the solid is usually additionally converted to a combustion gas therein using this procedure. The swirling action that preferably occurs in the combustion gas product that is present in the second combustion chamber 100 preferably, and conveniently, allows the fuel in the combustion gas product to have a more homogeneous mixing with the fuel. additional oxidant (and other oxidants), and that the combustion gas product remains in the second combustion chamber 100 more than would otherwise be the case, or that what would typically happen in a boiler or industrial steam generator conventional. In the second combustion chamber 100, substances that may be present in the fuel that is usually contained in the combustion gas product (together with one or more combustion gases) will generally be more complex than these they would be in the third combustion area 120, where they even experience a third combustion reaction and are further dissociated. A combustion gas product that is produced in the second combustion chamber 100 is the result of another incomplete (partial) combustion of the fuel that entered the interior of the second combustion chamber 100. (the percentage of the total fuel used that was not burned in the first combustion chamber 70). The amount of fuel that is burned in the second combustion chamber 100 generally ranges from more than about 0% to less than about 100%, preferably from about 20% to about 70%, and most preferably about 40%. For example, if 50% of the total fuel used in the generator 8 is burned in the first combustion chamber 70, it is preferred that 40% of the remaining 50% of fuel be burned in the second combustion chamber 100 (leaving 20% of the total fuel used in generator 8 without burning). The combustion gas that is produced in the second combustion chamber 100 preferably contains partially burned fuel, which is still rich in fuel, and may contain some environmental contaminants and / or hazardous materials in this stage of the process as products of a incomplete combustion (due to the fact that a complete combustion of the fuel is not present at this stage of the procedure), depending on the type of fuels or oxidants used. (If a third combustion area 120 is not used in the apparatus, the percentage of fuel burned in the second combustion chamber 100 will generally be higher than it would be if a third combustion area 120 is employed, and preferably is the same as described later in the present invention in connection with the third combustion area 120). The combustion gas product that is produced in the second combustion chamber 100 is moved by the elevated pressure (present and caused by the combustion process therein) from the forward end to the rearward end of the second combustion chamber 100. This is then moved by the elevated pressure into the interior of the third combustion area 120, where it moves from the forward end towards the rear end of the third combustion area 120. The fuel-rich combustion gas product which enters the interior of the third combustion area 120 preferably enters at a linear velocity greater than about 0.12 m / s-kg (0.178 ft / s-lb). The combustion gas product entering the interior of the third combustion area 120 after preference is supplied, and mixed, with one or more additional oxidants, which may be the same as or different from the other oxidants used in the generator 8, and which are ready to cause a third combustion reaction, this time in the third combustion area 120 (by spontaneous combustion of the fuel present therein), in an amount that works to cause a third combustion, and Preferably a final and complete combustion of the fuel that is present in the third combustion area 120. The third combustion area 120 operates in a manner similar to that of a "rear burner" of an aircraft with a jet engine. The 0 / F mixture ratio used in the third combustion area 120 usually also depends on several variables, such as the particular fuel (s) and oxidant (s) used. Depending on the chemical composition of said one or more fuels, fuel components or particular fuel mixtures used, some fuels require more or less oxidant to consume the fuel. The person skilled in the art can easily determine the amount of additional oxidant that is mixed with the fuel in the third combustion area 120, and a desirable 0 / F mixing ratio. The additional oxidant supplied to the third combustion area 120 is preferably the excess oxidant which does not flow into the first oxidant distributor 41 or into the second oxidant distributor 82, and which enters the interior of the oxidant transfer tube. 49, and it is not ventilated. However, additional oxidant may be supplied to the third combustion area 120 (or to other areas or components of the generator 8) in a different manner, as described above in the present invention for the first oxidant inlet 42 and the second inlet Oxidant 81. The additional oxidant preferably has a temperature ranging from about -120 ° C to about -12 ° C. This can be heated by absorbing the heat from the first transfer injector plate 44 and the second transfer injector plate 84, where it functions as a coolant for these plates, and is usually at least partially in a gaseous form. The additional hot oxidant is pressurized to the rear end of the oxidant transfer tube 49, which is present within a third outer housing 130. The lower portion of the third outer housing 130 is adjacent to the outside of a tube 121, the which is preferably hollow, and which preferably forms the side walls of the rear end of the second combustion chamber 100 and the forward end of the third combustion chamber 120. The additional oxidant then passes under pressure from the rear end of the tube oxidant transfer 49, which is preferably pierced or otherwise machined within the third outer housing 130, towards a hot oxidant distributor 136, or other means for dosing additional oxidant into the interior of the third combustion area 120 , which is also present in the third outer housing 130. The additional oxidant preferably flows in a radial shape inside the hot oxidant distributor 136, which is preferably made from austenitic steel and preferably secured inside or machined within the third outer housing 130. The upper portion of the hot oxidant distributor 136 is positioned adjacent to the rear end of the oxidant transfer tube 49, and the lower portion of the hot oxidant distributor 136 is positioned adjacent to the outside of the tube 121. The pressure causes the additional oxidant to be injected by the hot oxidant distributor 136 and flow from preferably in a radial shape about one, or preferably a plurality of hot oxidant orifices 122 that are preferably uniformly separated in one or more rows (or other configurations) in the tube 121. The hot oxidant orifices 122 are preferably aligned with the hot oxidant distributor 136. The number and diameter of the holes in the Hot oxidant 122, which can be drilled / machined, within tube 121, depends on the 0 / F mixture ratio of selected final combustion gas product. The optimum number, diameter, and special orientation of the hot oxidant orifices 122 for a particular oxidant and 0 / F mixing ratio can be readily determined by one skilled in the art. The pressure then causes the additional oxidant to enter the interior of the hot oxidant orifices 122. The additional oxidant is then injected (preferably by spray) under pressure from the heated oxidant orifices 122 into the interior of the third combustion area 120 ( in a straight or angled way), where it is mixed with the fuel contained therein, causing a third combustion reaction (by spontaneous combustion of the fuel), and a final complete combustion that occurs in the third combustion chamber 120. The flow rate of the additional oxidant can be varied within the distributor 136 to achieve a stoichiometric combustion reaction in the third combustion area 120. The incoming fuel present in the combustion gas product that is produced in the second chamber of combustion 100 is mixed with the additional oxidant, preferably resulting in a stoichiometric mixture of fuel and oxidant in the third combustion area 120, and causing a vortex to form from the fuel flow and oxidant flow in the third combustion area 120. The fuel then a third combustion is experienced, and preferably a complete combustion of the fuel remaining in the third combustion area 120 at the specified 0 / F ratio. Although the order can be varied, it is preferred that the product of combustion gas containing the fuel is dosed into the third combustion area 120 before the additional oxidant is dosed into the interior of the third combustion area 120. A product The combustion gas produced in the third combustion area 120 results from a complete (or almost complete) combustion of the fuel that entered the third combustion area 120 (the percentage of the total fuel used that was not burned in the first combustion chamber 70 or in the second combustion chamber 100). The amount of fuel that is burned in the third combustion area 120 generally ranges from more than 0% to about 100%, and preferably ranges from 50% to about 100%, with 100% being more preferred. The objective is to have from about 95% to about 100%, and preferably 100%, of the fuel that is used in the generator 8 burned by this point in the process (when the third combustion area 120 is the last chamber or area of combustion used in the generator 8). For example, if 50% of the total fuel used in the generator 8 is burned in the first combustion chamber 70, and 40% of the remaining 50% of fuel is burned in the second in the second combustion chamber 100, it is preferred that all the remaining fuel is burned in the third combustion area 120 (leaving 0% of the total fuel used in the generator 8 unburned, and achieving a combustion efficiency of 100%). The combustion gas product that is produced in the third combustion area 120 preferably contains fully burned fuel (100%) and, therefore, preferably has none of the incomplete combustion products, such as environmental contaminants and / or hazardous materials (or have small amounts of such products). The temperature and pressure used in the third combustion area 120 are regulated to allow a final complete combustion (one burned, separate, additional, complete) of the fuel present therein, which is present in a combustion gas product. The additional oxidant and fuel are mixed, and burned, at temperatures and pressures that cause each of these to vaporize additionally (they vaporize to a greater degree than the vaporization that occurs in the second combustion chamber 100) during this third combustion reaction. The temperature in the third combustion area 120 can be easily controlled by selecting a 0 / F mixing ratio that corresponds to the particular types of fuels used therein to achieve this result. The pressure in the third combustion area 120 can be regulated by controlling the pressure of the fuels or oxidants entering the interior of the third combustion area 120. The temperature in the third combustion area 120 preferably ranges from about 1650 ° C to about 3200 ° C, more preferred from about 2500 ° C to about 3000 ° C. The pressure in the third combustion area 120 preferably ranges from about 21 kg / cm 2 gauge to about 105 kg / cm 2 gauge, more preferred from about 35 kg / cm 2 gauge to about 63 kg / cm 2 gauge. The combustion process occurring in the third combustion area 120 is preferably presented at a stoichiometric ratio of the 0 / F mixture ratio. Using commercially available computer programs, and other information readily available, the person skilled in the art can vary the temperatures and pressures used in the third combustion area 120 to achieve complete combustion of the fuel that is therein. The amount of time the fuel remains in the third combustion area 120 is a period that allows the fuel to experience a final combustion and preferably complete combustion in the third combustion area 120, which usually occurs in a varying period. from about 0.025 to about 10 seconds. However, the amount of time the fuel remains in the third combustion area 120 may vary depending on the temperature in the third combustion area 120 and the speed at which the fuel is injected into the third combustion area 120. The higher the temperature, and the faster the speed of the fuel, the shorter the period in which the fuel remains in the third combustion area 120. All the materials present in the third combustion area 120 are also generally maintained under turbulent conditions, and is made to pass to a state of flow by the combustion reaction that occurs in it. When said one or more fuels or component thereof is a solid, the solid usually also becomes a combustion gas therein by this process. The swirling action that the combustion gas product preferably experiences in the third combustion area 120 generally, and conveniently, allows the fuel present in the combustion gas product to have a more homogeneous mixture with the oxidant (and other oxidants), and the combustion gas product remains longer in the third combustion area 120 than would happen without such a swirling action, or what would typically happen in a conventional industrial steam generator or boiler. In the third combustion area 120, the substances present in the fuel will generally be less complex than what they are in the second combustion chamber 100, where they even undergo a third combustion reaction and dissociate further. (If a fuel or solid fuel components are used in the generator 8, the particles are likely to be eroded in the first combustion chamber 70 further eroding in the second combustion chamber 100 even further eroding in the third combustion area 120 , usually vaporizing completely in the third combustion area 120). The exhaust product from the combustion gas resulting from the third combustion reaction is moved under pressure from the forward end towards the rear end of the third combustion area 120. Under the pressure caused by the third combustion reaction, the product of The combustion gas exhaust exits after the generator 8 flowing out of the rear end of the third combustion area 120, which is open (it does not have a wall or other closure at its rear end which causes the third combustion area 120 to be enclosed ). The exhaust product of the combustion gas can be released into the atmosphere, for example, through a conventional chimney with the emission of minimal amount or quantities of environmental contaminants and / or hazardous materials. Alternatively, it can be used in another sub-system or system, such as a boiler or steam generator by recovering exhaust heat to produce additional steam. The exhaust product from the combustion gas that leaves the third combustion area 120, which is usually hot, generally contains a smaller amount of environmental contaminants and / or hazardous materials compared to the combustion gas product. which occurs in the second combustion chamber 100 (as a result of experiencing a third combustion reaction, separate, and preferably complete), and more preferably does not contain environmental contaminants and / or hazardous materials. The temperature of the exhaust product of the combustion gas usually varies from about 1100 ° C to about 3000 ° C, usually from about 1500 ° C to about 2800 ° C. Due to this elevated temperature and as a result of the fuels used in the generator 8 having been subjected to three separate combustion reactions around this stage of the process, the flue gas exhaust product will generally be environmentally clean. This preference does not contain (0%) environmental contaminants and / or hazardous materials, or only minimal amounts of environmental contaminants and / or hazardous materials. Preferably, the flue gas exhaust product contains only non-contaminating and non-harmful atoms which have been dissociated from the molecules in which these are initially present in the fuels used in the generator, such as H, C, O and Cl , and / or molecules that are not environmental contaminants and / or hazardous materials, such as H20, instead of CO, NOx, N20, N02, SOx, S02, HCl, or particulate matter molecules. Depending on the type of fuel used, the exhaust of combustion gas that occurs after a complete combustion reaction in the methods and apparatus of the present invention may only contain water vapor (H20) and C02 (an air pollutant of the type). no criterion that can be caught and used as described in the present invention). Depending on the type of fuel used in the processes and appliances, the flue gas exhaust product may contain a certain amount of ash. The level of ash in the flue gas exhaust product preferably ranges from about 0% to about 2%, most preferably 0% (without ash). For example, if natural gas is the only fuel used in the process, the exhaust product from the combustion gas must not contain ash. Alternatively, if tire rubber particles are used as the sole fuel, a certain amount of ash is likely to be present in the exhaust product of the flue gas. As another example, if 453.6 grams of coal having an energy value of 7407.03 kcal / kg (13,346 BTU / lb) are burned in a conventional coal combustion process, the potential energy produced should be approximately 31,017 kJ / kg. , and the flue gas exhaust product must contain approximately 73.98% carbon, 4.85% hydrogen, 6.41% oxygen, 1.76% nitrogen, 1.59% sulfur, 6.23% ash and 5.23% moisture. In contrast, if 453.6 grams of TDF are burned in accordance with the methods and apparatuses of the present invention, then the potential energy that is produced must be about 36.023 kJ / kg, and the flue gas exhaust product must contain approximately 83.87% of coal, 7.09% of hydrogen, 2.17% of oxygen, 0.024% of nitrogen, 1.23% of sulfur, 4.78% of ash and 0.62% of humidity. As shown in Figure 14, the flue gas exhaust product can leave the third combustion area 120 (or other chamber or combustion area) of the generator 8 to a steam generator for exhaust heat recovery that it contains water that can cool the exhaust product of hot combustion gas, thereby converting water into a vapor product, which must also be environmentally clean. This vapor product may contain varying percentages of wet steam, dry saturated steam, or superheated steam, which may be separated from one another using conventional steam separation equipment, and may be used separately to perform various functions. The supply water is preferably supplied to the generator 8 at the front end of the first combustion chamber 70 from a water source (not shown), such as a water storage tank, through an appropriate flow control device using a pump to a first water inlet 52, or other means to receive water supply. The first water inlet 52 is attached to an upper portion of the first water distributor 51 using means for securing these two generator areas 8 to each other, such as by welding or other means known in the art, to an area between the front end. and the rear end of the first water distributor 51. The flow control device can be the same as those described above in the present invention in connection with the fuel inlet distributor 12. The water is preferably pre-heated, having a the temperature described above in the present invention (under the heading "water") and aid the first combustion chamber 70 in maintaining its structural integrity when exposed to elevated temperatures. The rate of water flow in this case in the process (and through all the methods and apparatus of the present invention) is generally dependent on several factors, such as the temperature in the generator 8, the water pressure, and the amount of steam to be produced in a selected range, for example 45.36 kg of super-heated steam product or saturated dry steam product per hour. The front end of the first water distributor 51 is preferably attached to the rear end of the first oxidant distributor plate 40 in the manner described above in the present invention. The front end of the first water distributor 51 preferably has one or more holes for bolts spaced at equal distances bored therein for attachment to the first oxidant distributor plate 40 using high strength bolts with the nuts and accompanying washers. The bolt holes can be drilled / machined into the numbers and spatial orientation described above in the present invention. The rear end of the first water distributor 51 is preferably connected to a first outer housing 50, by any suitable means, preferably welding. The first outer housing 50 functions as a frame or structure that protects the first tube assembly 71 (provides tangential mechanical strength to the first tube assembly 71), and provides a structure to which a flange or other joining device can be attached. Other outer housings described in the present invention, such as the second outer housing 90 and the fourth outer housing 140, function in a similar manner. Water flows under pressure through the first water inlet 52 into the interior of the first water distributor 51, or into other means for regulating a water supply to the first pipe assembly 71 and to control the water pressure. The first water distributor 51 allows a water supply to be readily available to and within the first tube assembly 71, and preferably maintains a constant water pressure. The other water dispensers described in the present invention function in a similar manner. The water is then forced to pass under pressure into the first combustion chamber 70, and then into one or more first water inlet passages 55 which are present in the first outer housing 50, and which are preferably drilled in radial in it. The number of first water inlet passages 55 in the first outer housing 50 should be the same as the number of first water inlet passages 55 in the first tube assembly 71. The first water inlet passages 55 in the first outer housing 50 are preferably located along the first combustion chamber 70 in an area located within the first water distributor 51. Water flows under pressure from the first water inlet passages 55 located in the first outer housing 50 and towards, and through, the first water inlet passages 55 located in said one or more individual tubes that are present in the first tube assembly 71, which form the side walls of the first combustion chamber 70. The first tube assembly 71, which is shown in detail in Figures 5 to 6, contains one or more hollow tubes which are preferably connected using means for securely connecting the tubes together, for example, by welding. It is preferable to have a plurality of hollow tubes in the first tube assembly 71 (and in all other tube assemblies) such that the apparatus can continue to function properly if a leak or obstruction occurs in one or more tubes. In general, the more hollow tubes are present in the first tube assembly 71 (and in all other tube assemblies used in the generator 8), the greater the surface area with which the water comes into contact, the faster the converts water into super-heated steam, and fewer problems will occur if one of the tubes develops a problem. Any suitable means or devices for connecting the hollow tubes to each other, which include the methods and devices described above in the present invention in connection with the junction of the fuel inlet manifold 12, can be used with the flow control device. These hollow tubes (and the other hollow tubes described in the present invention in connection with other tube assemblies) are preferably concentric; however, other configurations are possible. The tubes may be circular, oval, or otherwise appropriate. Alternatively, the outer surface of a piece of pipe can be grooved and slid into the first outer housing 50, which creates a water vapor passage (a channel wall configuration). The front end of each of the individual tubes constituting the first assembly tube 71 preferably has a first water inlet passage 55 which corresponds to, and is aligned with, one or more first water inlet passages 55 in the first outer housing 50, and the rear end of each of the individual tubes preferably has a first outlet passage of superheated steam product 56 corresponding to, and is aligned with, one or more first output passages of superheated steam product 56 in the first outer housing 50. The first tube assembly 71 is preferably in the form of a concentric tubular shell. The exterior of the first tube assembly 71 may, optionally, but preferably be covered or wrapped with a high temperature material to more evenly transfer the pressure load to the first outer housing 50 as is known in the art. This high temperature material must have the capacity to withstand a temperature of up to about 540 ° C, and thermally insulate the first outer housing 50 and the first tube assembly 71, which allows more efficient energy management of the gas energy produced in the first combustion chamber 70. The trailing end of the first oxidant distributor plate 40 preferably has a groove 71a machined therein, in which the leading end the first tube assembly 71 can be inserted. The slot 71a must be of a size that allows the front end of the first tube assembly 71 to fit securely therein. A central area of the front end of the first water distributor plate 60 also preferably has a machining slot 71b therein, in which the rear end of the first tube assembly 71 can be inserted. The slot 71b must be of a size that allows the rear end of the first assembly tube 71 to fit securely therein. Any suitable means or devices can be used to securely attach the first oxidant distributor plate 40 with the first tube assembly 71, and the first tube assembly 71 with the first water distributor plate 60, which includes the methods and devices described above in the present invention in connection with the union of the fuel inlet manifold 12 with the flow control device, and other similar methods or devices known to the person skilled in the art. The first tube assembly 71 is inserted into, and fits securely within, the first outer housing 50, preferably extending beyond both the leading and trailing ends of the first outer housing 50 to a length at the end. front that is equal to the depth of the groove 71a machining at the rear end of the first oxidant distributor plate 40 (to allow the first tube assembly 71 to be inserted therein), and to a length at the end which is equal to the depth of the slot 71b that is machined at the front end of the first water distributor plate 60 (to allow the first tube assembly 71 to be inserted therein). Each of these areas of preference is sealed with a similar package or devices. The first tube assembly 71, the second tube assembly 101, the third tube assembly 146 and tube assembly 121, preferably are removably attached to the generator 8, which allows these generator components 8 to be easily replaced, for example, by sliding them in and out of the generator 8. The heat from the hot combustion gas product that is produced in the first combustion chamber 70 (resulting from a first combustion process) is transferred from inside the first chamber. of combustion 70 towards the first adjacent tube assembly 71. This heat transforms the water present in the individual tubes present in the first tube assembly 71 into a superheated steam product or a dry saturated vapor product. The superheated steam product or dry saturated vapor product that is produced in the first tube assembly 71 (and which occurs in all other steps in the procedures and in all other areas of the apparatus) preferably has a pressure that varies from approximately 21 kg / cm2 gauge to approximately 320 kg / cm2 gauge, more preferred from about 180 kg / cm 2 gauge to about 250 kg / cm 2 gauge, and even more preferred about 211 kg / cm 2 gauge, and have a temperature which preferably ranges from about 260 ° C to about 621 ° C, and most preferred way ranges from about 400 ° C to about 590 ° C, even about 430 ° C being even more preferred. The superheated steam product or dry saturated steam product, which is present in the individual tubes present in the first tube assembly 71, flows under pressure to one or more first superheated steam product outlet passages. in the first assembly tube 71, and then out of the first tube assembly 71 towards one or more of the first superheated steam product outlet passages 56 that are preferably radially perforated, or placed from some other in the first outer housing 50, and which are aligned with the first superheated steam product outlet passages 56 in the first tube assembly 71. The first superheated steam product outlet passages 56 in the first outer housing 50 are preferably located along the first combustion chamber 70 in an area within the first superheated steam product outlet distributor 53. The pr The first passages of the superheated steam product outlet 56 which are drilled in the first outer housing 50 must be the same as the number of tubes, and the number of first outlet passages of the super-heated steam product 56, which they are present in a first tube assembly 71. The superheated steam product or dry saturated vapor product then flows under pressure in the opposite direction of the first combustion chamber 70 and into a first super product steam outlet distributor. heated 53, which preferably has its leading end attached to the rear end of the first housing 50 with means for securely joining these two areas of the generator 8 together, for example, by welding. Essentially, any suitable means or devices known in the art can be used to securely attach the first superheated steam product outlet distributor 53 to the first outer housing 50, including the methods and devices described above in the present invention. The rear end of the first superheated steam product outlet manifold 53 is preferably attached to the forward end of the first water distributor plate 60 with means for securely joining these two areas of the generator 8 together, e.g. , with one or more of the fourth attachment devices 57, such as high strength bolts and the accompanying nuts and washers as required. The fourth attachment devices 57 may be the same as those described above in the present invention for the first attachment devices 14. The rear end of the first superheated vapor product outlet distributor 53 preferably has a connecting device, such as those described above in the present invention for the fuel inlet manifold 12, having one or more bolt holes spaced at equal distance bored therein, which allow the insertion of the high strength bolts therein. The vapor product then passes under pressure from the first superheated steam product outlet distributor 53 in the opposite direction of the first combustion chamber 70 and towards a first superheated steam product outlet 54, which preferably it is positioned in an upper portion of the first superheated steam product outlet distributor 53, between its front end and its rear end. The super-heated steam product or dry saturated vapor product then flows out of the first outlet of the super-heated steam product 54 (and outside the generator 8) to a conventional superheated steam product collection device (not shown), such as a steam drum that can optionally contain centrifugal separators and / or cleaners, or other suitable device. The supply water is supplied from a water source (not shown), which may be the same or a different source of water used to supply supply water to the first water inlet 52, such as a second storage attack. of water, through a suitable flow control device by means of a pump to a second water inlet 62 that is preferably located below the second fuel port tubes 66 in a lower portion of a central area of the generator 8 The second water inlet 62 is preferably located between the fuel wear plate 63 and the second oxidant inlet 81. The flow control device may be the same day as that described above in the present invention in connection with the fuel inlet manifold 12. Water, which preferably has a temperature in the range described above in the present invention for the first mere water inlet 52, flows under pressure to an area of the generator 8 which is located between the first combustion chamber 70 and the second combustion chamber 100. The water flows under pressure to a supply water distributor 64, which Preferably it extends from the rear end of the first combustion chamber 70 to the front end of the second combustion chamber 100, and around the second fuel orifice tubes 66, which have hot combustion gas flowing from one side to the other. another one of them. This water functions to cool the fuel wear plate 63, whose front end is adjacent to the rear end of the first combustion chamber 70, which is heated from the combustion gas product leaving the first combustion chamber. and travels to the second combustion chamber 100. The mixture of water, wet steam and a super-heated steam product or dry saturated steam product resulting from this cooling process flows from the water supply distributor 64 to the serving portion. bottom of the generator 8 and outside the second outlet of the superheated steam product 67 (and outside the generator 8) to a conventional superheated steam product collection device (not shown). The second superheated steam product outlet 67 is preferably aligned with the second water inlet 62, and is located above the supply water dispenser 64 (in the upper portion of the generator 8). The superheated steam product collection device is preferably a superheated central steam product collection device that is used to collect the superheated steam product or the dry saturated vapor product from the first outlet of superheated steam product 54, and from all other parts of the generator 8 from which steam products leave. The supply water is supplied to the generator 8 preferably in an area near the front end of the second combustion chamber 100 from a water source (not shown), which may be the same source or a different source of water which is used to supply supply water to the first water inlet 52 or to the second water inlet 62, such as a third water storage tank, through an appropriate flow control device by means of a pump to a third inlet of water 92. The third water inlet 92 is preferably joined to an upper portion of a second water distributor 98 with suitable means for securing these two areas of the generator 8 to each other, such as by welding, in an area between the end front and the rear end of the second water dispenser 98. Essentially any appropriate means or devices known in the art for joining together can be used. Secure the third water inlet 92 to the second water distributor 98, including the methods and devices described above in the present invention. The flow control device can be the same type of device described for the fuel inlet distributor 12. The water, which preferably has a temperature in the range described hereinabove for the first water inlet 52, helps to the second combustion chamber 100 to retain its structural integrity. The front end of the second water distributor 98 is preferably attached to the rear end of the second oxidant distributor plate 80 with means for securely joining these two areas of the generator 8 together, for example, with one or more of the Fifth joint devices 91, such as high strength bolts and nuts and washers as required. The fifth attachment devices 91 may be the same as those described above in the present invention for the first attachment devices 14. The leading end of the second water distributor 98 preferably has a connection device, such as that described above in the present invention for the fuel inlet manifold 12, having one or more bolt holes spaced at equal distance, drilled therein, which allow the insertion of high strength bolts therein. The rear end of the second water distributor 98 is preferably joined to a second outer housing 90 with means for securely joining these two areas of the generator 8 together, preferably by welding. Essentially, any appropriate means or devices known in the art can be used to securely attach the second water distributor 98 to the second outer housing 90, including the methods and devices described above in the present invention. The water flows under pressure through the third water inlet 92 towards the second water distributor 98, or towards other means for regulating a water supply to a second tube assembly 101 and controlling the water pressure. The water is then forced to pass under pressure to the second combustion chamber 100, and then to one or more second water inlet passages 95 in the second outer housing 90, and preferably radially drilled therein. The number of second water inlet passages 95 in the second outer housing 90 must be the same as the number of second water inlet passages 95 that are present in the second tube assembly 101. The second water inlet passages 95 in the second outer housing 90 they are preferably located along the second combustion chamber 100 in an area located within the second water distributor 98. The second tube assembly 101 preferably forms the side walls of a portion of the second one. combustion chamber 100 (preferably approximately two thirds of the side walls, which leads from the second oxidant distributor plate 80 to the rear end of the second combustion chamber 100). The water flows under pressure from the second water inlet passages 95 located in the second outer housing 90 and towards, and through, the second water inlet passages 95 located in said one or more individual tubes that are present in the second. tube assembly 101. The second tube assembly 101 is shown in greater detail in Figure 8. The tubes in the second tube assembly 101 are preferably connected with means for connecting these tubes to each other, which may be the same as the tubes. those described above in the present invention for the first tube assembly 71. The tubes are preferably concentric in nature, but may be otherwise as desired, and may be circular, oval, or in any other appropriate form. Alternatively, the outer surface of a piece of pipe can be grooved and slid into the second outer housing 90., creating a water vapor passage (a channel wall configuration). The front end of each of the individual tubes constituting the second tube assembly 101 preferably has a second water inlet passage 95 corresponding to, and aligned with, one or more second water inlet passages 95 that are present in the second outer housing 90, and the trailing end of each of the individual tubes preferably has a second superheated steam product outlet passage 96 which corresponds to, and is aligned with, one or more second passages of output of superheated steam product 96 which are present in the second outer housing 90. The second tube assembly 101 is preferably in the form of a concentric tubular shell, but may be in any other appropriate shape. The exterior of the second tube assembly 101 is preferably adjacent to the interior of the second outer housing 90. The exterior of the second tube assembly 101 may optionally, but preferably, be covered or wrapped with a high temperature material as described above in the present invention for the first tube assembly 71, which allows a more efficient energy management of the gas energy that is produced in the second combustion chamber 100. The trailing end of the second oxidant distributor plate 80 preferably it has a slot 101a machined therein, into which the front end of the second tube assembly 101 can be inserted. The slot 101a must be of a size that allows the front end of the second tube assembly 101 to fit securely inside this one. A central area of the front end of a second water distributor plate 110 also preferably has a slot 101b machined therein, into which the rear end of the second tube assembly 101 can be inserted. The slot 101b must be of a size which allows the rear end of the second tube assembly 101 to fit securely therein. Essentially, any suitable means or devices known in the art can be used to securely attach the second oxidative distributor plate 80 to the second tube assembly 101, and the second tube assembly 101 to the second water distributor plate 110, including the methods and devices described above in the present invention. The second tube assembly 101 is inserted into, and secured securely within, the second outer housing 90, preferably extending beyond both the leading and trailing ends of the second outer housing 90 to a length over the leading end. which is equal to the depth of the slot 101a which is machined at the rear end of the second oxidant distributor plate 80 (to allow the second tube assembly 101 to be inserted therein, and a length over the rear end which is equal to the depth of the slot 101b which is machined at the front end of the second water distributor plate 110 (to allow the second tube assembly 101 to be inserted therein) .Each one of these areas of preference is sealed with a package or other appropriate device The heat from the hot combustion gas that is produced in the second combustion chamber 100 (which resulting from a second combustion process) is transferred from the interior of the second combustion chamber 100 and into the second adjacent assembly tube 101. This heat transforms the water into the individual tubes in the second tube assembly 101 into a superheated steam product or a dry saturated vapor product. The vapor product that is produced in the second tube assembly 101 preferably has a pressure and a temperature in the ranges described above in the present invention for the first tube assembly 71. The superheated vapor product or the product of saturated saturated steam, which is present in the individual tubes in the second tube assembly 101, flows under pressure to one or more second output passages of superheated steam product 96 in the second tube assembly 101, and then out of the second tube assembly. from tube 101 to one or more second output passages of superheated steam product 96 which are preferably radially perforated, or otherwise placed in the second outer housing 90, and which are aligned with the second passages of superheated steam product outlet 96 in the second tube assembly 101. The second superheated steam product outlet passages 96 that are present in the second outer housing 90 are preferably located along a portion of the second combustion chamber 100 in an area within the second super-heated steam product outlet distributor 93. The number of second product output passages of v Super-heated rod 96 drilled in the second outer housing 90 should be the same number as the number of tubes, and the number of second output passages of super-heated steam product 96 in the second tube assembly 101. The product of Superheated steam or the dry saturated steam product then flows under pressure in the opposite direction to the second combustion chamber 100 and towards a second super heated steam product outlet distributor 93, which preferably has its front end attached to an area between the front end and the rear end of the second outer housing 90 with means for securely joining these two areas of the generator 8 to each other, which may be the same as those described above in the present invention for the extreme front of the first super-heated steam product outlet distributor 53. The rear end of the second vap product outlet distributor or super-heated 93 is preferably attached to the forward end of the second water distributor plate 110 with means for securely joining these two areas of the generator 8 to each other, which may be the same as those described above in the present invention for the rear end of the first superheated steam product outlet distributor 53, for example, with one or more of the sixth connecting devices 97, such as high strength bolts and the accompanying nuts and washers as required. The sixth attachment devices 97 may be the same as those described above in the present invention for the first attachment devices 14. The rear end of the second superheated vapor product outlet distributor 93 preferably has a connecting device, such as that described above in the present invention for the fuel inlet manifold 12, having one or more bolt holes spaced at equal distance bored therein. The superheated steam product or the dry saturated steam product then passes under pressure from the second superheated steam product outlet distributor 93 in the opposite direction of the second combustion chamber 100 and towards a third product outlet of super-heated steam 94, which is preferably placed in an upper portion of the second super-heated steam product outlet distributor 93 between its front end and its rear end. The vapor product then flows out of the third outlet of the superheated steam product 94 (and outside the generator 8) to a conventional superheated steam product collection device (and outside the generator 8) to a device collection of conventional super-heated steam product (not shown). The supply water is supplied to the generator 8 at a site near the rear end of the second combustion chamber 100 from a water source (not shown), which can be the same source or a different source of water that is used to supply the water supply to the other water inlets (52, 62 and 92), such as another water storage tank, through a appropriate flow control device by means of a pump to a fourth water inlet 131. The flow control device can be of the same type of device as described above for the fuel inlet distributor 12. The fourth water inlet 131, a third water distributor 135, and a fourth superheated steam outlet 132 are preferably drilled, or otherwise machined, in a third outer housing 130, preferably at a location between the rear end of the second plate of water distributor 110 and the forward end of the hot oxidant distributor 136. The lower portion of the third water distributor 135 is preferably adjacent to the outside of a tube 121 that d Preferably it extends from the rear end of the second tube assembly 101 to the front end of a third tube assembly 146, and preferably forms the side walls of a rear end portion of the second combustion chamber 100 (preferably about one third of the second combustion chamber 100) and a portion of the forward end of the third combustion area 120 (preferably about one third of the third combustion area 120). The fourth water inlet 131 is located in an upper portion of the generator 8, and has its rear end leading to the upper portion of the forward end of the third water distributor 135. The upper portion of the rear end of the third water distributor 135 leads to the lower portion of the fourth outlet of superheated steam product 132. The rear end of the second water distributor plate 110 is attached to a portion of the forward end of the third outer housing 130 by means of securely joining these two areas of the generator 8 to each other, for example, using one or more of the seventh linkage devices 111, such as high strength bolts with the nuts and accompanying washers as required. The seventh attachment devices 111 may be the same as those described above in the present invention for the first attachment devices 14. Essentially, any suitable means or devices known in the art for securely joining the second distributor plate may be used. of water 110 to third outer housing 130, including the methods and devices described above in the present invention. The supply water, which preferably has a temperature in the range described hereinabove for the first water inlet 52, flows under pressure through the fourth water inlet 131 to the second combustion chamber 100 in the portion top of the front end of the third water distributor 135, which preferably is machined in the third outer housing 130. The water that is heated by heat transfer from the combustion gas that is produced in the second combustion chamber 100 and / or in the third combustion area 120 through the tube 121, the third outer housing 130 and the third water distributor 135, whereby the steam is transformed into a super-heated steam product or a dry saturated vapor product. The fourth water inlet 131 preferably has a baffle (not shown) which diverts the superheated steam product that is produced from the feed water to the rear side of the third water distributor 135, which allows the product Superheated steam or the saturated saturated steam product travel away from the tube 121 and exit from the fourth outlet of the superheated steam product 132 to a superheated steam collection device (not shown). The feed water circulates around the tube 121 preferably in a radial manner, and functions as a refrigerant to cool the tube 121, which is heated from the combustion gas product that is produced in the second combustion chamber 100 and / or in the third combustion area 120. The supply water is supplies the generator 8 at a site near the forward end of the third combustion area 120 from a water source (not shown), which may be the same source or a different source of water used to supply supply water to the other water inlets (52, 62, 92 and 131), such as another water storage tank, through an appropriate flow control device by means of a pump to a fifth water inlet 133. The control device of flow can be of the same type of device as described above in the present invention for the fuel inlet distributor 12. The fifth water inlet 133, a fourth water distributor 137 and a fifth one The superheated steam product 139 is preferably also drilled, or machined in some other way, in the third outer housing 130 at a location between the rear end of the hot oxidant distributor 136 and the forward end of a fifth distributor of water 147. The lower portion of the fourth water distributor 137 is preferably also adjacent to the upper portion of the tube 121. The fifth water inlet 133 is preferably located in an upper portion of the generator 8, and has its rear end leading towards the upper portion of the forward end of the fourth water distributor 137. The upper portion of the rear end of the fourth water distributor 137 leads to the lower portion of the fifth outlet of superheated steam product 139. The water, which preferably has a temperature in the range described above in the present invention in connection with the first input of water 52, flows under pressure through the fifth water inlet 133 towards the third combustion area 120 towards the upper portion of the forward end of the fourth water distributor 137, where it is heated because the heat transferred from the gas product of combustion that occurs in the third combustion area 120 through the tube 121, the third outer housing 130 and the fourth water distributor 137, whereupon the water is transformed into a vapor product. The fifth water inlet 133 preferably also has a baffle (not shown) which diverts the steam product that is produced from the water to the rear side of the fourth water distributor 137, which allows the steam product to travel in opposite direction to tube 121 and exit the fifth outlet of superheated steam product 139 to a superheated steam collection device (not shown). The feed water preferably circulates around the tube 121 in a radial fashion, and functions as a refrigerant to cool the tube 121, which is heated, as described above in the present invention. The supply water is supplied to the generator 8 at a site near the rear end of the third outer housing 130 from a water source (not shown), which may be the same or a different source from the water source used for supplying the supply water to the other water inlets (52, 62, 92, 131 and 133), such as another water storage tank, through an appropriate flow control device by means of a pump to a sixth inlet of water 149. The sixth water inlet 149 is preferably placed downstream of the fourth water distributor 137, preferably at a site where a flue gas exhaust product begins to exit from the third combustion area 120 (FIG. and the generator 8). The forward end of the sixth water inlet 149 is preferably joined to an area between the leading end and the trailing end of the fifth water distributor 147 by appropriate means for securely joining these two areas of the generator 8 to each other., such as by welding. Essentially, any suitable means or devices known in the art can be used to securely join the sixth inlet of water 149 to the fifth water distributor 147, including the methods and devices described above in the present invention. The flow control device can be the same type of device as that described above in the present invention in connection with the fuel inlet distributor 12. The water temperature is preferably as described in the present invention for the first water inlet 52. An upper portion of the fifth water distributor 147 is preferably attached to the rear end of the third outer housing 130 using means for securely joining these two areas of the generator 8 together, for example, using one or more of the eighth joining devices 141, such as high strength bolts with the nuts and accompanying washers as required. The eighth joining devices 141 can be the same as those described in the present invention for the first attachment devices 14. The upper portion of the fifth water distributor 147, and the rear end of the third outer housing 130, each have preferably one or more bolt holes separated at equal distances, aligned, for the insertion of high strength bolts therein. The lower portion of the fifth water distributor 147 is preferably attached to the forward end of a fourth outer housing 140 using means for securely joining these two areas of the generator 8 together, such as by welding. Essentially, any suitable means or devices known in the art can be used to securely attach the fifth water distributor 147 to the fourth outer housing 140, including the methods and devices described above in the present invention. The water flows under pressure through the sixth inlet of water 149 towards the rear end of the third outer housing 130 to the fifth water distributor 147, filling the fifth water distributor 147 with water. The water is then pressurized to the third combustion area 120 towards the forward end of the third tube assembly 146, which forms the side walls of a portion of the third combustion area 120 from which a product exits. of exhaust gas combustion. The exterior of the third tube assembly 146 is preferably adjacent to the interior of the fourth outer housing 140. The third tube assembly 146 contains one or more hollow tubes which are preferably connected with means for connecting the tubes to each other, for example, by welding. Essentially, any suitable means or devices known in the art can be used to connect the tubes to each other, including the methods and devices described above in the present invention. The hollow tubes are preferably concentric in nature, but may be otherwise if desired. The tubes may be circular, oval, or in any other appropriate form. Alternatively, the outer surface of a piece of pipe can be grooved and slid into the outer outer housing 140, creating a steam passage (a channel wall configuration). The leading end of each of the individual tubes constituting the third tube assembly 146 preferably has a water inlet and the trailing end of each of the individual tubes preferably has a superheated steam product outlet. The third tube assembly 146 is preferably in the form of a conical cone (with the leading end having a diameter smaller than that of the trailing end), but may be in any other appropriate shape. The third tube assembly 146 preferably extends in the opposite direction to the tube 121 (and from the third combustion area 120), as shown in Figure 1, at an angle that preferably varies from about 12 ° to about 18 °. The exterior of the third tube assembly 146 may, optionally but preferably, be covered or wrapped with a high temperature material in the manner described above in the present invention for the first tube assembly 71, for efficient energy management of gas that is produced in the third combustion area 120. The heat from the exhaust product of hot combustion gas that is produced in the third combustion area 120 (resulting from a third combustion process) is transferred from the interior from the third combustion area 120 to the third tube assembly 146. This heat transforms the water that is present in the individual tubes present in the third tube assembly 146 into a superheated steam product or a saturated vapor product dry. The superheated steam product or dry saturated steam product that is produced in the third tube assembly 146 preferably has a pressure and a temperature in the ranges described above in the present invention in connection with the first tube assembly 71.

The water entering the interior of the sixth inlet of water 149 acts as a refrigerant to cool the third tube assembly 146, which is heated from the flue gas exhaust product that is produced in the third combustion area 120 The superheated steam product or dry saturated vapor product that is formed in the individual tubes present in the third tube assembly 146 flows under pressure out of the superheated steam product outlets present in the tubes, and out of the third tube assembly 146, in the opposite direction to the third combustion area 120 towards the lower portion of a third superheated vapor product outlet distributor 143, which preferably has its leading end adjacent the rear end of the third tube assembly 146, and which is preferably located at the rear end of the third combustion area 120 (and generator 8). The front end of the third super heated steam product outlet manifold 143 is also preferably located in close proximity to the lower portion of an exhaust plate 148. The lower portion of the exhaust plate 148 is preferably welded to the rear end of the fourth outer housing 140, functions as an interface to the exhaust product of combustion gas exiting the generator 8, and preferably deflects the exhaust product of combustion gas to a device that can utilize the heat of the product of exhaust of combustion gas, for example, a steam generator for recovery of exhaust heat (shown in Figure 14), or to the atmosphere. The super-heated steam product or dry saturated vapor product flows under pressure from the lower portion towards the upper portion of the third super heated steam product outlet distributor 143, which has its upper end attached to an area located between the lower portion and the upper portion of the exhaust plate 148. This has its lower end joined to the exhaust plate 148 with means for securely joining these two areas of the generator 8 to each other, for example, which may be welding. This has its upper end attached to the exhaust plate 148 with means for securely joining these two areas of the generator 8 together, for example, by welding. Any suitable means or devices can be used to securely link the superheated steam outlet manifold 143 to the third tube assembly 146, and the superheated steam outlet manifold 143 to the exhaust plate 148, which they include the methods and devices described above in the present invention in connection with the union of the fuel inlet manifold 12 with the flow control device, and other similar methods or devices known in the art. The rear end of the third combustion area 120 can be left open, thereby allowing a combustion gas exhaust product that is produced by the generator 8 to be released to the atmosphere. Alternatively, the exhaust plate 148 may be optionally attached to a steam generator by exhaust heat recovery (shown in Figure 14), or similar device, with means for securely joining the plate exhaust 148 to a flange or similar structure present in the steam generator for recovery of exhaust heat, for example, using one or more of the ninth joint devices 150. The ninth joint devices 150 may be the same as the first devices 14, such as high strength bolts with nuts and washers as required. The upper portion of the exhaust plate 148 preferably has one or more bolt holes spaced at equal distances, bored therein, which are aligned with spacing bolt holes and the like in an area of the recovery steam generator. of exhaust heat that can be connected to the exhaust plate 148, which allows the insertion of high strength bolts in it. The superheated steam product or the dry saturated vapor product then passes under pressure from the third superheated steam outlet manifold 143 in the opposite direction to the third combustion area 120 and towards a sixth outlet of super steam product. heated 144, which is preferably located in an upper portion of the third superheated steam outlet manifold 143, between its front end and its rear end. The superheated steam product or dry saturated vapor product then flows out of the sixth outlet of the superheated steam product 144 (and outside the generator 8) to a superheated steam collection device (not shown).

Use of the HCGC in a tri-generation system With reference to Figure 1 and Figure 14, a preferred embodiment of a combustion and power generation system is described, which includes the hydrocarbon combustion gas generator of the present invention. Figure 14 shows the hydrocarbon combustion gas generator subsystem, which is indicated in general terms with the number 1000, in a non-polluting three-generation steam energy generating plant, which is generally indicated with the number 10,000. The tri-generation 10,000 steam power generating plant also comprises a steam generator subsystem for exhaust heat recovery 2000, an oxidant subsystem 3000, a fuel subsystem 4000, a water management subsystem 5000, a subsystem of heat rejection 6000, a generating turbine subsystem 7000, an electric power generating subsystem 8000 and an oxidant manufacturing subsystem 9000. The hydrocarbon combustion gas generator ("generator") 8 produces different types of steam (a super-heated steam product or a dry saturated steam product, medium pressure steam and low pressure steam) that can be used separately in many different existing industrial applications, as well as in new industrial applications, and in the generation of steam electric power, on the site, non-polluting. The oxidant subsystem 3000, the fuel subsystem 4000 and the water management subsystem 5000 provide (feed), and control the flow of, oxidant and fuel reactants, and water, which are used in the generator 8. The oxidant used in the oxidant subsystem 3000 it is obtained by means of an oxidant manufacturing subsystem 9000. The LOX can be used as the oxidant, and it can be produced by an air separation unit through atmospheric air liquefaction and the subsequent separation of the LOX from it by continuous cryogenic distillation. The LOX is removed after the cryogenic distillation system and stored as a cryogenic liquid in a bulk oxidant storage tank 201. The oxidant subsystem 3000 includes a first LOX 270 feed line that feeds the LOX through a first valve 271 to a LOX pump 273, which is driven by a pump transmission unit of LOX 274. The LOX pump 273 delivers LOX at high pressure into a second LOX 276 feed pipe and through a second one. valve 275 which is connected to the second LOX feed pipe 276 with a T (not shown). One side of the T leads to a LOX vaporizer system 277 leading to the generator 8 (towards the first oxidant inlet 42 shown in Fig. 1), and containing, for example, pressure regulators, a venturi control of fluid in cavitation and / or transducers detectors of temperature and pressure. The other side of the T leads to an oxygen flow and pressure management system 278 connected to a third LOX feed line 279 leading to the generator 8 (towards the second oxidant inlet 81 shown in Figure 1). The LOX entering the vaporizer system of LOX 277 is vaporized and this is then conducted from the LOX vaporizer system 277 to the generator 8. (As shown in Figure 1, gaseous oxygen enters the first oxidant inlet 42 to high pressure and flows to the first oxidant distributor 41, where it is injected into the first combustion chamber 70 of the generator 8. The excess oxidant flows at high pressure towards the oxidant transfer tube 49, and then towards the hot oxidant distributor 136, wherein the gaseous oxygen is injected into the third combustion area 120). The LOX that enters the other side of the T flows into the pressure and oxygen flow management system 278 which contains, for example, pressure regulators, a venturi control of fluid in cavitation and / or transducers detectors of temperature and pressure. The LOX remains in a liquid state, and is brought from the pressure and oxygen flow management system 278 to the generator 8. (As shown in Figure 1, the LOX enters the second oxidant input 81 that supplies LOX to the second oxidant distributor 82. The LOX is then injected into the second combustion chamber 100. The excess oxidant flows at high pressure to the oxidant transfer tube 49, and then to the hot oxidant distributor 136, where gaseous oxygen is injected into the third combustion area 120). The fuel used in the fuel subsystem 4000 may be in a liquid, solid or gaseous state, and is obtained from a bulk fuel storage tank 202. The fuel system 4000 includes a first fuel feed line 280 which feeds the fuel through a third valve 281 to a fuel pump 282, which is driven by a fuel pump transmission unit 283. The fuel pump 282 supplies high pressure fuel through a fourth valve 284 The fuel is then conducted to a fuel pressure and flow management system 285 which contains, for example, pressure regulators, a venturi control of cavitating fluid and / or temperature and pressure sensing transducers. Fuel is conducted from the fuel pressure and flow management system 285 through a second fuel supply line 286 to the generator 8. (As shown in Figure 1, the fuel is discharged into the inlet manifold. of fuel 12 of the generator 8). With reference to Figure 1, an ignition device 20 suitable for igniting the oxygen and fuel mixture that is flowing into the first combustion chamber 70 is used. The generator 8 efficiently burns the injected reactants under controlled conditions, what produces a gaseous mixture of high pressure, and high temperature of fuel gases for combustion. This converts the chemical energy present in the fuel into thermal energy (heat) that is transferred to the surrounding tubes containing water, thereby converting the water in the tubes into a vapor product. The generator 8 also produces a hot combustion gas exhaust product, which can be released from the generator 8 through a first flue gas exhaust pipe 125 (Fig. 14) towards a steam generator by heat recovery of exhaust 400 which is present in the exhaust heat recovery subsystem 2000. The combustion gas exhaust product that is produced in the exhaust heat recovery subsystem 2000 leaves the three-generation steam power generating plant 10,000 through a second flue gas exhaust pipe 405. As shown in both Fig. 1 and Fig. 14, the water entering the generator 8 becomes a superheated steam product or a product. of saturated steam as it exits through the superheated steam product outlets present in the generator 8 (shown as 54, 67, 94, 132, 139 and 144 in both Fig. 1 and Fig. 1). 14) to a super-heated steam drum 300. The super-heated steam product or high pressure saturated steam product is then supplied from the central super-heated steam drum 300 to the generating turbine 7000 subsystem (figure 14). The superheated steam product or saturated steam product leaves the generating turbine subsystem 7000 and is supplied to a high pressure generating turbine 310 through a first superheated steam product discharge pipe 301. Thermal control of the combustion processes in the generator 8 can be achieved by controlling the flow rate of the cooling water and the rate of heat supply in connection with each of the water inlets of the combustion chamber (shown as 52, 62, 92, 131, 133 and 149 in FIG. 1) through a second water supply pipe 295 leading to the generator 8 from the water handling subsystem 5000. The replacement feed water is supplied by a water supply pipe. replacement water 425, which provides cooling water to the generator 8 from the heat rejection subsystem 6000. For example, if 45.36 kg of water are present at start-up the generator 8 (when the operation is started), and the generator 8 uses 4,536 kg of water, then the replacement water pipe 425 supplies 4,536 kg of water to the generator 8. The water management subsystem 5000 maintains the proper balance of water in the generator 8 maintaining an appropriate amount of cooling water that is supplied to the generator 8. The use of water in the water management subsystem 5000 is obtained from a bulk water storage tank 203. The subsystem of water handling 5000 includes a first water supply pipe 290 that feeds the water through a fifth valve 291 to a high pressure water pump 292, which is driven by a water pump transmission unit 293. The water pump 292 conducts water at high pressure through a first water pressure and flow management system 294 containing, for example, pressure regulators, a fluid venturi control in cavitation and / or temperature and pressure detector transducers. Water is conducted from the first water pressure and flow management system 294 through a sixth valve 296 to the water inlets (shown as 52, 62, 92, 131, 133 and 149 in Figure 1) of the generator 8, which provides thermal control of combustion processes. At start-up, the generator 8 uses the water flowing to it from the water management subsystem 5000 (for steam water). In this stage of the process, the water is usually at room temperature, and is pumped at an elevated pressure from the high pressure water pump 292 to the water inlets of the generator 8 (shown as 52, 62, 92, 131 , 133 and 149 in Figure 1). However, when the generator 8 is filled with a sufficient amount of water to allow its proper operation, the first water pressure and flow management system 294 closes the sixth valve 296, and diverts the cooling circulation water away from the generator 8. The water that is diverted from the generator 8 flows to the heat rejection subsystem 6000 through a seventh valve 297 to a first water line 298, and then to a first cooling water pump 552, which is driven by a first cooling water pump transmission unit 553. The cooling water is circulated through the first cooling water pump 552 and can be diverted to a holding tank and water cooling tower 550, towards a water condenser 570 and / or to a water cooler 540. Circulating water can be discharged from the first cooling water pump 552 through an eighth valve 554 to a second water pipe 551 leading to the inlet side of the holding tank and water cooling tower 550. In addition, the circulating water can be discharged from the first cooling water pump 552 through a third pipeline of water 555 to a ninth valve 556 and to the cold water inlet side of the water condenser 570. The water condenser 570 also allows the cooling water to be discharged through a fourth water pipe 545 to the water side. water cooler inlet 540. At the start, a sufficient amount of available water is generally present to operate the generator 8. However, to ensure that a sufficient quantity of water is available during start-up, cessation of operations and other operations of the generator 8, the subsystem is used heat rejection 6000. The heat rejection subsystem 6000 acts as a water reservoir, as well as a receiver for the excess water generated by the generator 8 during its operation. In addition to the first cooling water pump 552 and the other components described above, the heat rejection subsystem 6000 contains a second cooling water pump 422, which is driven by a second water pump transmission unit of cooling 421, a second water pressure and flow management system 423 and a third water pressure and flow management system 428. Each of the second and third water pressure and flow management systems 423 and 428 may contain, for example, pressure regulators, cavitation fluid venturi controls and / or temperature and pressure detector transducers. The heat rejection subsystem 6000 provides replenishment water which is preferably preheated for use in the steam generator by recovery of waste heat 400. The waste heat recovery steam generator 400 receives the hot replenishment water from the condenser of water 570 and of the holding tank and water cooling tower 550. The hot replacement water is pumped from the water condenser 570 through a fifth water pipe 571 and then through a tenth valve 572 to the second cooling water pump 422. The hot replacement water is then discharged into the second water pressure and flow management system 423. A twelfth water pipe 557 carries the supplied water from the water holding tank and cooling tower 550 through a fourteenth valve 558 to the second cooling water pump 422. The second pressure and flow management system of water 423 can discharge the hot fill water through a sixth water pipe 426 towards the high pressure inlet (not shown) of the steam generator by recovery of waste heat 400. The hot reset water which does not flow to the steam generator for waste heat recovery 400 from the sixth water pipe 426 is discharged through a seventh water pipe 427 to the third water pressure and flow management system 428. The third pressure and flow management system 428 discharges the hot medium pressure replenishment water to a medium pressure water inlet (not shown) present in the steam generator for recovery of residual heat 400, and discharges the hot low pressure replenishment water through the water. an eighth water pipe 429 to a low pressure water inlet (not shown) present in the steam generator for recovery of residual heat 400. In addition, the water of r The high pressure composition can be discharged through the second water pressure and flow management system 423 through an eleventh valve 424 in the replenishment water pipe 425 which leads to the generator 8 (and enters the second water pipe). water supply 295).

The generating turbine subsystem 7000 converts the output energy produced by the generator 8 into mechanical energy that can excite the electric power generating subsystem 8000. The generating turbine subsystem 7000 contains three electric power generating turbines, a high pressure generating turbine 310, a medium pressure generating turbine 320 and a low pressure generating turbine 330, which are staggered in terms of pressure for optimal efficiency to maximize the use of the energy produced by the generator 8. The generator turbine subsystem 7000 also contains three turbine exhaust steam pipes, a high pressure exhaust steam pipe 311, an average pressure exhaust steam pipeline 321 and a low pressure exhaust steam pipeline 336, as well as a reheated pipeline. Turbine 401. The high pressure exhaust steam pipeline 311 leads from the generating turbine to elevated pressure 310 towards the steam generator by residual heat recovery 400, while the low pressure exhaust vapor pipe 336 leads from the low pressure generating turbine 330 to the steam generator for residual heat recovery 400. The pipeline reheated turbine 401 conducts from the steam generator by waste heat recovery 400 to the medium pressure generating turbine 320. the high pressure generating turbine assembly 310 and the high pressure exhaust steam pipeline 311 is followed by the assembly of the medium pressure generating turbine 320 and the medium pressure exhaust steam pipeline 321. The 7000 generating turbine system is terminated by an assembly of the low pressure generating turbine 330 and the low pressure exhaust steam pipeline 336 , which sends the exhaust steam to the steam generator by recovery of residual heat 400. The superheated steam product or the p Saturated steam product that is produced by the generator 8 is supplied from the generator 8 to the generating turbine subsystem 7000 through the first superheated steam product discharge pipe 301, which leads to the high pressure side (not shown) of the high pressure generating turbine 310. The exhaust steam from the high pressure generating turbine 310 is discharged from the high pressure generating turbine 310 to the high pressure exhaust steam pipe 311. The assembly described in the preceding paragraph is followed by the superheated turbine pipe 401 leaving the steam generator for recovery of waste heat 400 and leading to the medium pressure generating turbine 320. In the turbine reheated pipe 401, the steam temperature of Exhaust is increased to the temperature of the superheated steam process or saturated steam product that comes out through the lids of superheated steam product (shown in figure 1 as 54, 67, 94, 132, 139 and 144) present in the generator 8. This is effected by burning the exhaust steam in a reheated chamber (not shown) of the steam generator for recovery of residual heat 400, and mixing the output from this combustion process with the main stream of superheated steam product flow, thus adding energy, and maintaining a constant inlet temperature of the steam that leads to the medium pressure generating turbine 320 from the superheated turbine pipe 401. The superheated steam product or the saturated steam product is supplied to the medium pressure generating turbine 320 through the superheated turbine pipe 401, wherein the exhaust vapor from the medium pressure generating turbine 320 is discharged to the medium pressure 321. steam exhaust pipe. The exhaust steam flows from the exhaust pipe to the exhaust pipe. erecting steam at medium pressure 321 to the low pressure generating turbine 330, and then out of the low pressure exhaust steam pipeline 336, which sends the exhaust steam to the steam generator for residual heat recovery 400 An electrical power generation subsystem 8000 that is located near the low pressure generating turbine 330 has an electrical power conversion facility 500 that contains one or more electric generators and power conditioners. These electric generators and power conditioners develop the final energy product 501 of this three-generation 10000 steam generating power plant from super-heated or saturated steam products. The waste heat recovery subsystem 2000, which contains the waste heat recovery steam generator 400, is a gas handling system that makes the most efficient use of the exhaust products produced by the generator 8, and by the three different generating turbines 310, 320, and 330. The waste heat recovery steam generator 400 contains a high pressure feed water inlet, a medium pressure feed water inlet, a feed water inlet at medium pressure, a low pressure feedwater inlet, a high-pressure economizer, an economizer at medium pressure, a low-pressure economizer, a high-pressure boiler, a medium-pressure boiler, a low-pressure boiler, a high pressure drum, a medium pressure drum, a low pressure drum, a high pressure superheater outlet, a medium pressure steam outlet, and an outlet low pressure steam, which are not shown, but can be obtained commercially. Steam generators for residual heat recovery can be commercially available from Babcock & Wilcox Company (Barberton, Ohio) and Energy Recovery International (Lincoln, Nebraska). The low pressure steam leaving the low pressure generating turbine 330 is discharged into the low pressure exhaust steam pipe 336, and then to the low pressure feed water inlet (not shown) present in the low pressure generator. steam by recovery of residual heat 400. The low pressure steam can leave the steam generator by recovering residual heat 400 through a twelfth valve 404 and towards a low pressure steam discharge pipe 403. The energy present in this Low pressure steam is suitable for a wide range of industrial applications. A medium pressure steam outlet (not shown) present in the waste heat recovery steam generator 400 is connected to the superheated turbine pipe 401. The superheated turbine pipe 401 supplies medium pressure steam leaving the steam generator by recovery of waste heat 400 towards the medium pressure generating turbine 320. A first three way valve 410 is present in the turbine reheated pipe 401, and can drive the medium pressure steam leaving the steam generator by heat recovery waste 400 to a first medium pressure steam discharge pipe 407, and then to a medium pressure steam and flow management system 402. The medium pressure steam and flow management system 402 contains, for example, flow regulators. pressure, a venturi control of fluid in cavitation and / or transducers detectors of temperature and pressures. The medium pressure steam can be directed from this in the medium pressure steam and flow management system 402 through a thirteenth valve 408 and into a medium pressure steam pipe 409 leading to the water cooler 540. ninth water line 541 conveys water from water cooler 540 to water condenser 570, and a fourth water line 545 carries water from water condenser 570 to water cooler 540. One tenth water pipe 543 carries cold water from the water cooler 540 to a cooling unit (not shown), such as an air conditioner, for use in refrigeration applications, and an eleventh water line 544 carries hot water from the cooling unit back to the 540 water cooler. The cooled air product of the 540 water cooler is suitable for a wide variety of industrial cooling applications, such as air conditioning. A thirteenth water pipe 546 transports water from the water condenser 570 to the holding tank and water cooling tower 550. Alternatively, medium pressure steam can flow from the steam and flow management system to mean pressure 402 to a second medium pressure steam discharge pipe 407A and outside the three generation 30000 steam power plant. The energy present in this medium pressure steam is suitable for a wide range of industrial applications. A superheated steam outlet (not shown) that is present in the waste heat recovery steam generator 400 is connected to a high pressure steam pipe 312 that delivers a superheated steam product or saturated steam product. to the superheated central steam drum 300. A second three-way valve 314 present in the high pressure steam pipe 312 can be used to direct the superheated steam product or saturated steam product to a second line of steam. Super-heated steam discharge 313 and outside the three-generation 10000 steam generation power plant. The energy present in the super-heated steam product or saturated steam product is appropriate for a wide variety of industrial applications, such as as for the generation of electricity, using for example: (a) extraction turbines, which take steam at a high pressure, use some ca nity of steam for electricity generation, and send the remaining steam to other steam processes located downstream of the turbine; (b) back pressure turbines, which take steam at a high pressure, use a certain amount of pressure and pass all the steam to other steam processes at a reduced pressure; and / or (c) condensing turbines, which take steam at a high pressure and, through a series of platforms, take all the available energy in the steam and discharge the steam at a low pressure. Condensing turbines are usually used in thermoelectric plants, where the sole purpose for steam is to produce electricity in general in a steam turbine. However, a certain amount of steam can be used to pre-heat the water in the incoming boiler.

Manufacturing Method The hydrocarbon combustion gas generator, an example of which is shown in Figures 1-3, can be manufactured in the manner described below or using other methods known in the art. The majority of the components of the hydrocarbon combustion gas generator 8 ("generator") can be machined from one or more pieces of material in a manner known to the person skilled in the art. The separate components or component areas of the generator 8 can be joined together by welding, bolting, compression adjustment, or other methods known in the art. O-rings, gaskets, or other sealing materials can be used to prevent leakage of fluid between the components. The dimensions of the "O" ring used in the generator 8 depend on the MAOP used and can be easily determined by the person skilled in the art. For example, in the generator 8 shown in Figure 1, preferably an "O" ring or package is present between the fuel inlet manifold 12 and the fuel meter block 30, between the fuel meter block 30 and the first oxidizer distributor plate 40, between the first superheated steam product outlet distributor 53 and the first water distributor plate 60, between the first water distributor plate 60 and the second oxidant distributor plate 80, between the second water distributor 98 and the second oxidizer distributor plate 80, between the second superheated steam product outlet distributor 93 and the second water distributor plate 110, between the second water distributor plate 110 and the third outer housing 130, and between the third outer housing 130 and the fifth water distributor 147. The description in the present invention about a generator component 8 is applied all the same components that may be present in, or on, the generator 8. For example, a discussion about a first water distributor 5i applies to all the first water distributors 51 that may be present in the generator 8 The second water distributor 98 of the generator 8 can, for example, be manufactured in a manner similar to that of the first water distributor 51. The fuel inlet distributor 12 is preferably designed to operate at a pressure of approximately 84.36 kg. / cm2 gauge to approximately 175.75 kg / cm2 gauge in a conventional manner. The connecting device is preferably present in the fuel inlet manifold 12, and in other portions of the fuel inlet manifold 12, preferably all are machined from a piece of austenitic / ferritic steel. A series of bolt holes spaced at equal distances are preferably drilled in the connection device present in the fuel inlet manifold 12, in which the number, size and spatial distribution of the bolt holes is optimized as is known from the person skilled in the art for a particular fuel pressure. The number, size and spatial orientation of the bolt holes must be arranged to align with the bolt holes present in a similar connection device present in a fuel flow control device. High strength bolts with lock washers or washers and / or nuts, or socket head bolts with lock washers or washers that are preferably made from austenitic / ferritic steel (hereinafter collectively referred to as "fasteners" ) can then be inserted into the bolt holes to connect the fuel inlet manifold 12 with the fuel flow control device. Other components of the generator 8 can be joined in a similar manner as shown in Figures 1-3. The fuel inlets 9 can be drilled and tilted at an angle in the fuel inlet manifold 12, in which the fuel passages lead from the fuel inlets 9 to, and are connected to, the fuel chambers 10, which can also be drilled in the fuel inlet manifold 12. The rear end of the inlet manifold of fuel 12 is preferably attached to the front end of the fuel meter block 30 using fasteners. The area between the rear end of the fuel inlet manifold 12 and the front end of the fuel gauge block 30 is preferably sealed with a high-pressure gasket. Alternatively, an optional "0" ring slot can be machined in the base of the fuel inlet manifold 12, wherein the dimensions of the 0 ring are selected based, in part, on the MAOP. Ring 0 and packing are made from a material for appropriate temperature and high pressure. The fuel meter block 30, the injector wear plate 32 and the first fuel opening tubes 36 are preferably each machined separately from a piece of austenitic / ferritic steel. The first fuel openings 34 are drilled through the wear plate of the injector 32, the fuel meter block 30, the first oxidant inlet 42, the first oxidant distributor plate 40 and the first transfer injector plate 44. (for the subsequent insertion of the first fuel opening pipes 36 therein).

The first fuel opening tubes 36 are inserted into the injector wear plate 32 and through the fuel meter block 30, the first oxidant distributor plate 40 and the first transfer injector plate 44. The wear plate of injector 32 can be pressed into a machined receptacle at the front end of the fuel meter block 30. Second fuel ports 65 can be drilled through the first water distributor plate 60, the second water inlet 62, the fuel wear plate 63, the feed water distributor 64, the second oxidant distributor 82, the second transfer injector plate 84, and the second oxidant distributor plate 80 in the manner described above in connection with the first fuel openings 34 (for the subsequent insertion of the second fuel port tubes 66 therein). As shown in Figure 2, the second fuel port tubes 66 can be inserted through the second fuel ports 65, the first water distributor plate 60, the water supply dispenser 64, the second water distribution plate 60. oxidizer distributor 80, second oxidant distributor 82 and second transfer injector plate 84.

The first oxidizer distributor plate 40 is preferably designed to operate at a pressure ranging from about 84 kg / cm 2 to about 180 kg / cm 2 gauge in a conventional manner, and preferably machined from one piece of austenitic / ferritic steel. The first transfer injector plate 44 is preferably machined from a piece of austenitic / ferritic steel. The design of the first transfer injector plate 44 allows multiple first fuel ports 34 to be present therein, in which multiple first fuel opening tubes 36 can be inserted for different types of fuel. The number of first desired fuel openings 34, which is determined by the ratio 0 / F and the selected fuel, can be drilled in the first transfer injector plate 44. The first transfer injector plate 44 can be inserted into the injector. pressure in a receptacle machined at the rear end of the first oxidant distributor plate 40. The first oxidant distributor 41 can be machined in the first oxidant distributor plate 40. The first oxidant injector orifices 46 can be drilled in the first transfer injector plate 44, the front end of which can be attached to the rear end of the first oxidant distributor plate 40. The second transfer injector plate 84 is also preferably machined from an austenitic steel part / Ferritic The design of the second transfer injector plate 84 allows multiple second fuel ports 65 to be present therein, in which the second multiple fuel orifice tubes 66 can be inserted for different types of fuel. The desired number of second fuel ports 65, which is determined by the ratio 0 / F and selected fuels, can be drilled in the second transfer injector plate 84. The second transfer injector plate 84 can be press-fitted. in a receptacle machined at the rear end of the second oxidant distributor plate 80. The second oxidant distributor 82 can be machined within the second oxidant distributor plate 80. The second oxidant injector orifices 85 can be drilled in the second transfer injector plate 84, the front end of which can be attached to the rear end of the second oxidant distributor plate 80. The ignition device housing 26 of the ignition device 20 is preferably machined from one piece of austenitic / ferritic steel that is compatible with an oxidant. The mixing chamber 28 can be drilled at the rear end of the ignition device 20, and must have the same diameter, or corresponding diameter, as that of the flare tube 29 that is bored in the fuel meter block 30, the first oxidant inlet 42 and the first oxidizer distributor plate 40. The fuel inlet of the ignition device 22 and the oxidant inlet of the ignition device 24 can be drilled and tilted at an angle through the housing of the ignition device 26, which allows the oxidant and fuel used in the ignition device 20 to intersect at the center of the mixing chamber 28. An electronic ignition device interface can be drilled and tilt, using the screw thread, at the front end of the ignition device housing 26 and mixing chamber 28 to join a device high-voltage spark (which can ignite a mixture of oxidant and fuel in the mixing chamber 28) to the ignition device housing 26. The housing of the ignition device 26 can be welded to the fuel meter block 30, and the mixing chamber 28 must be aligned with the flame tube 29. The first combustion chamber 70 is preferably a hollow cylindrical tube having its side walls formed from the first tube assembly 71, which fits inside the first outer housing 50. The first outer housing 50 has one or more first water inlet passages 55 drilled therein, and one or more first exit passages of the same. Superheated steam product 56 bored in it. Each of the individual tubes present within the first tube assembly 71 is preferably bored and sealed to form one or more water inlets and one or more outlets of superheated steam product. The individual tubes, which are preferably made from ferritic / austenitic steel, can then be welded together to preferably form a concentric tubular shell. The exterior of the first tube assembly 71 is preferably wrapped or covered with a material for elevated temperature. The trailing end of the first oxidant distributor plate 40 preferably has a slot 71a machined therein, wherein the leading end of the first tube assembly 71 can be inserted into the first oxidant distributor plate 40. The leading end of the first water distributor plate 60 also preferably has a slot 71b machined therein, wherein the rear end of the first tube assembly 71 can be inserted into the first water distributor plate 60. These areas, in the which the two different components of the generator 8 come into contact, preferably sealed with a package. The first water distributor 51 can be welded to the front end of the first outer housing 50, and can be bolted to the rear end of the first oxidant distributor plate 40. The first superheated steam product outlet distributor 53 it can be welded to the rear end of the first outer housing 50, and can be screwed to the front end of the first water distributor plate 60. The second combustion chamber 100 is preferably a cylindrical hollow tube having the side walls of its end front formed with the second tube assembly 101, which fits inside the second outer housing 90. The second outer housing 90 has one or more second water inlet passages 95 drilled therein, and one or more second exit passages of the same. Super-heated steam product 96 drilled in it. Each of the individual tubes present in the second tube assembly 101 is preferably bored and sealed to form one or more water inlets and one or more outlets of superheated steam product. The individual tubes, which are preferably made from ferritic / austenitic steel, they can also be welded together to form a concentric tubular shell. The exterior of the second tube assembly 101 is preferably wrapped or covered with a material for elevated temperature. The rear end of the second anti-rust distributor plate 80 preferably has a slot 101a machined therein, where the rear end of the second tube assembly 101 can be inserted into the second oxidant distributor plate 80. The front end of the second water distributor plate 110 also preferably has a slot 101b machined therein, wherein the rear end of the second tube assembly 101 can be inserted into the second water distributor plate 110. These areas, in which the two different components of the generator 8 come into contact, preferably they are also sealed with a package. The second water distributor 98 can be welded to the front end of the second outer housing 90, and can be attached with fasteners to the rear end of the second oxidant distributor plate 80. The second superheated steam product outlet distributor 93 it can be welded to the second outer housing 90 between its front end and its rear end, and can be attached with fasteners to the front end of the second water distributor plate 110. The third combustion area 120 is a cylindrical hollow tube that has no wall (or other closure) at its rear end, which allows a combustion gas exhaust product that is produced by the generator 8 to exit the generator 8. A tube 121 that is preferably hollow (but may be solid) , and that preferably forms the side walls of the rear end of the second combustion chamber 100, and the forward end of the third combustion area 120, also d Preferably, it is made from a piece of austenitic / ferritic steel. The forward end of the third combustion area 120 preferably has one or more hot oxidant orifices 122 spaced evenly in one or more rows bored in the tube 121. The hot oxidant orifices 122 must be aligned with the oxidant distributor. hot 136, and must be drilled in one or more rows radially around the circumference of tube 121. The first water distributor 51, the first superheated steam product outlet distributor 53, the second water distributor 98 and the second superheated steam product outlet distributor 93 are each preferably designed to operate at a pressure of up to 320 kg / cm2 absolute and at a temperature of up to 621 ° C, and most preferably at a pressure of 180 ° C. kg / cm2 approximately absolute and at a temperature of approximately 538 ° C. Each of these generator components 8 is preferably machined separately from a piece of austenitic / ferritic steel, and has a connecting device, such as a flange, having one or more bolt holes spaced at the same distance bored. in the same, in its front end or rear end for attachment with fasteners to another component or area of the generator 8. Each of these components has one or more inputs or outputs - for water and / or a super-heated steam product or dry saturated steam product (the first water inlet 52, the first super-heated steam product outlet 54, the third water inlet 92 and the third outlet of superheated steam product 94) drilled therein, or bonded thereto. The first water inlet 52, the first superheated steam product outlet 54, the third water inlet 92 and the third superheated steam product outlet 94 each preferably have a flange-type interface that is welded to the first water distributor 51, the first superheated steam product outlet distributor 53, the second water distributor 98 and the second superheated steam product outlet distributor 93, respectively. The lower portion of the first water distributor 51 and the first superheated steam product outlet distributor 53 each preferably have a machined flange surface that can be welded to the first outer housing 50. The first water distributor 51 of Preferably it has a connecting device, such as a flange, at its leading end having one or more drilled bolt holes, which allow it to be screwed or otherwise secured to the rear end of the first oxidant distributor plate 40. Preferably, the area in which these two components of the generator 8 come into contact are sealed with a package. Alternatively, a slot for ring 0 can be machined in the base of the flange at its rear end. A similar connection device present at the rear end of the first superheated steam product outlet distributor 53 allows it to be screwed to the front end of the first water distributor plate 60. Preferably, the area in which These two components of the generator 8 come into contact and are sealed with a package. Alternatively, a slot for ring 0 can be machined in the base of the flange at its rear end. The lower portions of the second water distributor 98 and the second superheated steam product outlet distributor 93 can be attached to the second outer housing 90 in the same manner as described above in the present invention in connection with the first water distributor 51. and the first superheated steam product outlet distributor 53. The front end of the second water distributor 98 can be attached to the rear end of the second oxidant distributor plate 80, and the rear end of the second outlet distributor of Super-heated steam product 93 can be attached to the front end of the second water distributor plate 110, in the same manner described above in the present invention in connection with the first water distributor 51 and the first outlet distributor of water. super-heated steam product 53. The second water distributor plate 110 is preferably machined from one foot of austenitic / ferritic steel, and preferably has a connecting device, such as a flange, at its rear end for attachment using fasteners to the front end of the third outer housing 130, which preferably has a similar connection device. Preferably, the area in which these two components of the generator 8 come into contact is sealed with a package. Alternatively, a slot for ring O can be machined at the rear end of the second water distributor plate 110. The second water distributor plate 110 preferably has a slot 101b machined at its front end to allow the second Tube assembly 101 is inserted into this slot 101b. This slot 101b allows a superheated steam product, which has a high temperature, and which is under a large amount of pressure, exit the superheated steam product outlet holes that are present in the individual tubes contained in the second tube assembly 101, and flow to the second superheated steam product outlet distributor 93. The front end of the second water distributor plate 110 preferably has one or more bolted and inclined bolt holes, spaced at equal distances corresponding in number, alignment and spatial orientation with the bolt holes drilled in a connecting device, such as a flange, present at the rear end of the second superheated steam product outlet distributor 93. The second water distributor plate 110 can then be joined to the second superheated steam product outlet distributor 93 using fasteners.

The third outer housing 130 is preferably designed to support a pressure of up to about 320 kg / cm2, and a temperature of up to about 621 ° C, with a pressure of about 180 kg / cm2 absolute and a temperature of about 538 being most preferred. ° C. The third outer housing 130 is preferably machined from a piece of austenitic / ferritic steel, and has a plurality of bolt holes spaced at equal distance bored in a connecting device, such as a flange, present at its rear end, which allows its connection using bolts to the fifth water distributor 147. The fourth water inlet 131, the third water distributor 135 and the fourth outlet of the super-heated steam product 132 are preferably each machined in the third outer housing 130. The areas in which the different components of the generator 8 come into contact preferably are sealed with a package. The fifth water inlet 133, the fourth water distributor 137 and the fifth superheated steam product outlet 139 are preferably machined in the third outer housing 130 in a similar manner. The third outer housing 130 preferably has a receptacle machined in an area between its leading end and its trailing end, which extends radially from its internal diameter. The trailing end of the oxidant transfer tube 49, which fits inside this receptacle, can be welded to the third outer housing 130, which allows the hot oxidant to pass from the oxidant transfer tube 49 through the oxidant distributor. hot 136, which also fits inside this receptacle, and is injected through the hot oxidant orifices 122 into the interior of the third combustion area 120. The hot oxidative distributor 136 is positioned between the rear end of the transfer tube oxidant 49 and tube 121. The fifth water distributor 147 is preferably machined from a piece of austenitic / ferritic steel, and preferably has a series of bolt holes spaced at equal distances bored in a connecting device, such as a flange, present in its upper portion, which allows it to join with one or more fasteners to the rear end of the third exterior loosening 130. Preferably, the area in which these two components of the generator 8 come into contact is sealed with a gasket. Alternatively, a ring groove O may be machined at the rear end of the base of a connecting device present at the rear end of the third outer housing 130. The fifth water distributor 147 preferably has a machined cavity in an area between its front end and its rear end which allows it to receive the supply water which flows under pressure through the sixth inlet of water 149. The third tube assembly 146 preferably contains an arrangement of a plurality of concentric hollow tubes, and fits into a fourth outer housing 140. These tubes are preferably welded together in a manner that forms a conical cone, and preferably are made from austenitic / ferritic steel. The front end of the third tube assembly 146 can be welded to the lower portion of the fifth water distributor 147, and the rear end of the third tube assembly 146 can be welded to the front end of the third super product vapor outlet distributor. heated 143. The third superheated steam product outlet distributor 143 is preferably machined from a piece of austenitic / ferritic steel. The front end (and the lower portion) of the third superheated steam product outlet manifold 143 preferably has a machined quality therein, which allows the rear end of the third tube assembly 146, whose tubes form a conical cone, can be welded to it. The sixth output of super-heated steam product 144 can be attached to the third super-heated steam product outlet distributor 143 in the same manner as described above in the present invention for the first output of super-heated steam product 54. Exhaust plate 148 is also preferably made from a ferritic / austenitic steel part, and has a series of bolt holes spaced at equal distances drilled in a connecting device, such as a flange, present in its upper portion , which allows it to be joined using one or more fasteners to a waste heat converter (not shown), such as a steam generator for waste heat recovery (Figure 14), which has a connecting device containing Bolt holes with numbers, size and similar separation. The area in which the third superheated steam product outlet manifold 143 and the exhaust plate 148 come into contact is preferably sealed with a flange gasket (or other gasket), or with an O ring, which prevents the escape of hot combustion gas from escaping from this area of the generator 8. The apparatus and methods described above can be further understood in view of the following non-limiting examples.

EXAMPLE 1 Hydrocarbon combustion gas generator A 10-MW hydrocarbon ("generator") combustion gas generator is constructed having an approximately 97% combustion efficiency from austenitic / ferritic steel generally in the manner shown in the figures. The generator has a total length of about 411 cm and a total outside diameter of about 42.5 cm. This has two combustion chambers and a third, combustion area, each of which has an inner diameter of approximately 33.7 cm and an outer diameter of approximately 37.5 cm. However, the portion of the third combustion area from which a combustion gas exhaust product of the generator exits has different diameters. This part of the third combustion area is cone-shaped, in which the front end of the cone has an inner diameter of approximately 33.7 cm and an outer diameter of approximately 37.5 cm, and the rear end of the cone has an inner diameter of approximately 64 cm and an outer diameter of approximately 67.3 cm.

The first combustion chamber has a length of about 91 cm, and has its side walls formed with a first tube assembly containing fifty-eight tubes that are approximately 91 cm in length. The first tube assembly also covers the inside of a first outer housing. Each of the tubes present in the bundle of individual tubes forming the first tube assembly has an outer diameter of approximately 1.9 cm and an inner diameter of approximately 1.58 cm. The supply water having a temperature of about 120 ° C is supplied to the first tube assembly through a first water inlet at a flow rate of approximately 394.6 m3 / hour. The supply water travels from a water source to the first water inlet, into a first water distributor, and then into the first 58 water inlet passages. The water then travels through each of the 58 individual tubes that are present in the first tube assembly at a flow rate of about 25.25 to 2.29 m3 / hour per tube, where the water becomes a vapor product Super-heated or dry saturated steam product. The steam produced in the tubes travels out of the first 58 superheated steam product outlet passages and into a first superheated steam product outlet distributor. From this point, the steam travels through a first outlet of superheated steam product and out of the generator to a superheated steam product collection device at a temperature of about 538 ° C, and at a pressure of about 141 kg / cm2 gauge. The second combustion chamber has a length of about 91 cm, and has on the side walls at its front end formed with a second tube assembly containing 58 tubes that are approximately 91 cm long. The second tube assembly covers the inside of a second outer housing. Each of the tubes present in the bundle of individual tubes forming the second tube assembly has an outer diameter of approximately 1.9 cm and an inner diameter of approximately 1.58 cm. The supply water having a temperature of about 120 ° C is supplied to the second pipe assembly through a third water inlet at a flow rate of approximately 394.6 m3 / hour. The supply water travels from a water source to the third water inlet, into a second water distributor, and then into the 58 second water inlet passages. The after-water through the 58 individual tubes that are present in the second tube assembly at a flow rate of 2.25 to 2.29 m3 / hour per tube, where it becomes a superheated steam product or dry saturated steam product. The steam produced in the tubes travels out of the 58 seconds superheated steam product outlet passages and into a second superheated steam product outlet distributor. From here, the vapor travels through a third outlet of superheated steam product and out of the generator to a superheated steam product collection device at a temperature of about 538 ° C, and at a pressure of about 141 ° C. kg / cm2 gauge. A single hollow tube forming the side walls of the rear end of the second combustion chamber, and the front end of the third combustion area, has a length of approximately 60.96 cm, an outer diameter of approximately 37.47 cm and an inner diameter of approximately 33.66 cm. The supply water having a temperature of approximately 120 ° C is supplied from a water source through a fourth water inlet to a third water distributor at a flow rate of approximately 2.25 m3 / hour, where it becomes a super-heated steam product or dry saturated steam product. The superheated steam product or dry saturated steam product leaves the generator to a superheated steam collection device through a fourth outlet of superheated steam product at a temperature of approximately 538 ° C and at a pressure of approximately 141 kg / cm2 gauge. The supply water that has a temperature of approximately 120 ° C is also supplied from a water source through a fifth water inlet into a fourth water distributor at a flow rate of approximately 2.25 m3 / hour, in where it becomes a super-heated steam product or dry saturated steam product. The vapor product leaves the generator to a superheated steam collection device through a fifth superheated steam product outlet at a temperature of about 538 ° C, and at a pressure of about 141 kg / cm 2 gauge. A liquid oxygen oxidant (LOX) is pumped from a LOX source into a first oxidant inlet. The LOX then flows into a first oxidant distributor, where it is distributed in a radial manner to provide cooling for a first transfer injector plate, and where it is converted from a liquid to a gas. The resulting gaseous oxygen then passes through a plurality of first oxidant injector orifices at an angle of about 66 ° to the interior of the first combustion chamber zone at a flow rate of about 0.617 kg / s and a pressure of about 42.18 kg / cm2 gauge. At the same time, EF-15 fuel having an energy value of 10944.45 kcal / kg is pumped from a source of this fuel separately in a fuel inlet manifold and in two separate fuel inlets. The fuel that is pumped into the two separate fuel inlets passes into two separate chambers, respectively, that are present in the fuel inlet manifold. The fuel then passes through a plurality of first fuel orifice tubes at an angle of about 90 ° into the first combustion chamber zone initially at a flow rate of about 0.52 kg / s, and at a pressure of approximately 42.18 kg / cm2 gauge, and subsequently (when the supply water reaches the designated operating pressure) at the slowest flow rate of approximately 0.43 kg / s. Oxidant and EF-15 fuel pass into the first combustion chamber zone at a combined oxidant and fuel flow rate of approximately 1.55 kg / s, and at an O / F ratio ranging from about 1.2 to about 1.79, and preferably about 1.19, in a swirling form to allow sufficient homogeneous mixing of the fuel and oxidizer in the gaseous state in the first combustion chamber. (A certain amount of the fuel is transformed into a gaseous state while a certain amount of the fuel remains in a solid state). The swirling action is increased by injection of both the oxidant and the EF-15 fuel into the first angled combustion chamber, and allows a residence time of the fuel EF-15 in the first combustion chamber of about 0.12 to 0.15 seconds (once the mixture of oxidant and fuel EF-15 is ignited by a flare of natural gas or propane gas coming from an ignition device). In the first combustion chamber, the average combustion temperature is from 1371.11 ° C to approximately 1537.78 ° C and the average combustion pressure is approximately 42.18 kg / cm2 gauge. Additional LOX is pumped from a LOX source to a second oxidant inlet. The LOX then flows to a second oxidant distributor, where the LOX is radially distributed to provide cooling for a second transfer injector plate, and for a plurality of second fuel port tubes, thereby converting the liquid oxidant in a gas. The gaseous oxidant passes through a plurality of second oxidant injector orifices at an angle of about 70 ° to the interior of the second combustion chamber zone at a rate of about 1.20 kg / s, and at a pressure of about 35.15 kg. / cm2 manometric. At the same time, the incomplete combustion product that is produced in the first combustion chamber, which includes a certain amount of unburned EF-15 fuel, passes from the first combustion chamber to the second combustion chamber zone through the combustion chamber. a plurality of second fuel orifice tubes at a speed of approximately 0.40 kg / s, and at a pressure of approximately 35.15 kg / cm2 gauge. The relation 0 / F. in the second combustion chamber is from about 3.38 to about 5.03, and preferably about 4.8. In the second combustion chamber, the average combustion temperature is from 2482.22 ° C. approximately up to approximately 3037.78 ° C and the average combustion pressure is 35.15 kg / cm2 gauge. The additional oxidant and the combustion product that is produced in the first combustion chamber (which contains a certain amount of gas and a certain amount of unburnt fuel) enters the second combustion chamber with swirling action to allow sufficient homogeneous mixing of the remaining EF-15 fuel and oxidant gases. The swirling action is increased by injecting the additional oxidant into the second combustion chamber at an angle. The water is pumped from a water source to a second water inlet at a flow rate of approximately 394.7 m3 / h. The water then travels to a supply water distributor, which distributes the water radially for cooling the upper portion of a plurality of second fuel port tubes (to help maintain their structural integrity). The water is converted to super-heated steam or dry saturated steam leaving the generator through a second outlet of superheated steam product. The steam product leaving the generator through the second superheated steam product outlet (and through all other superheated steam product outputs present in this generator) has a temperature of about 538 ° C and it has a pressure of approximately 140.6 kg / cm2 gauge. The excess oxidant entering the interior of the oxidant transfer tube travels through the oxidant transfer tube and passes inside a hot oxidant distributor that is adjacent to the outside of the tube that forms the side walls of the front end of the third combustion area. The hot oxidant distributor distributes the oxidant around the tube, and through a plurality of hot oxidant orifices, wherein the additional oxidant enters a flow rate of 0.36 kg / s into the flue gas product stream, which has a flow rate of approximately 0.08 kg / s of fuel EF-15 without burning. In the third combustion area, the average combustion temperature is from about 2760 ° C to about 3037.78 ° C and the average combustion pressure is about 500 35.15 kg / cm 2 gauge. The relation 0 / F. of the oxidant and fuel EF-15 for the product stream of combustion gas in the third combustion area is from about 3.98 to about 6.3, and preferably about 4.4, thereby achieving about 97% efficiency of fuel combustion EF-15. The swirl action application of the fuel EF-15 which is present in the combustion product passing from the first combustion chamber to the second combustion chamber allows a residence time of the combustible hydrocarbon material in the second combustion chamber and in the third combustion area that makes a total of approximately 0.12 seconds. The exhaust of hot combustion gas that is produced by the generator leaves the generator passing out of the rear end of the third combustion area, which is approximately 60.96 cm long, which has side walls formed by a third tube assembly cone shaped, and extending in the opposite direction of the generator at an angle of approximately 35 °. A fourth outer housing is coated with the third tube assembly. The supply water having a temperature of approximately 121.11 ° C passes from a water source through a sixth water inlet to a fifth a water distributor at a flow rate of approximately 2.25 m3 / h, where it enters to the front end of the third tube assembly at a flow rate from 37,472 to 38,229 liters / minute (9.9 to 10.1 gallons / minute) approximately per tube and converted to superheated steam or dry saturated steam. The steam travels to the rear end of the third tube assembly, passes to the third superheated steam product outlet distributor and then exits out of the generator through a sixth outlet of superheated steam product at a temperature of about 538 ° C and at a pressure of about 140.6 kg / cm2 gauge. The temperature of the combustion gas exhaust product is from approximately 2482.22 ° C to approximately 2760 ° C when it leaves the generator. The hydrocarbon combustion gas generator can produce from approximately 30657.71 kg of a superheated steam product or dry saturated steam product per hour (approximately 16555.56 kg per hour of dry saturated steam and approximately 14102.15 kg per hour of super steam). heated) at the temperatures and pressures described which, in turn, can generate approximately 10 MW of electricity per hour. In addition, the flue gas exhaust product that is produced by this generator, if diverted to a steam generator by heat recovery, such as the steam generator for recovery of residual heat shown in Figure 14, can additionally generate from approximately 10 to approximately 15 MW (megawatts) of electricity per hour. Therefore, this generator can produce a total of approximately 20 to 25 MW of electrical energy per hour. In the configuration described in this example, the generator size is about 20% to 50% approximately smaller than that of conventional steam generators that produce a similar steam performance. Using LOX and EF-15 fuel, the generator described in this example produces an environmentally clean combustion gas exhaust product. The combustion gas exhaust product does not contain (0% by weight) N, NOx, NO, N02, N20, N2, S, SOx, SO, S02, S03, CO, HCl, CH, arsenic, uranium, mercury, lead, thorium, VOCs, dioxin, radium, radon, polonium, bismuth, other carcinogenic and / or mutagenic substances, particulate matter, coal ash or volatile ash. Additionally, it contains a significantly smaller amount of C02 (approximately a C02 reduction of 97%) than would be produced using a conventional plant that uses coal, and that uses the same amount of carbon, and / or that can produce the same amount of electrical energy.

EXAMPLE 2 Analysis of the exhaust of combustion gas that is produced by the combustion of natural gas, methanol, or kerosene with air or LOX The combustion products are determined using the GUIPEP computer thermochemical software based on the use of different fuels in the 10 MW hydrocarbon combustion gas generator described in example 1. The test is based on burning 907.2 kg of each one. of fuels (natural gas, methanol, or kerosene (oil # 1)) using LOX or air as the oxidant, in which each flue gas exhaust product leaves the hydrocarbon combustion gas generator at a pressure of about 70.30 kg / cm2 gauge. The discharge temperature of the exhaust gases varies according to the type of fuel. It should be mentioned that in contrast to the apparatus of the present invention, conventional fuel combustion systems that use air as an oxidant could, in general, explode if LOX is used as an oxidant. The following tables indicate the composition and temperature of the exhaust gas, as well as the weight, moles, and weight percent of each component present in the flue gas exhaust product.

A. Natural gas and LOX (Exhaust temperature of 1106.66 ° C) A. Natural gas and LOX (cont.) N0X (0 kg) is not found in the flue gas exhaust product.

B. Natural gas and air - (exhaust temperature of 1090. 56 ° C) B. Natural gas and air - (cont.) It is determined that the exhaust product includes 647.68 kg of NOx. Tables A and B show that when the same amount of natural gas is burned in the apparatus using air, instead of LOX, as the oxidant, the procedure results in a significant increase in the environmental pollutant by NOx titration.

C. Methanol and LOX - (exhaust temperature of 1162. 78 ° C) C. Methanol and LOX - (cont.) NOx (0 kg) is not found in the flue gas exhaust product D. Methanol and air - (exhaust temperature of 1063. 33 ° C) D. Methanol and air - (cont.) It is determined that the exhaust product includes 591.39 kg of NOx. Tables C and D show that when the same amount of methanol is burned in the apparatus using air, instead of LOX, as the oxidant, the procedure results in a significant increase in the environmental contaminant by NOx titration.

E. Kerosene and LOX - (exhaust temperature of 1307. 22 ° C) E. Kerosene and LOX - (cont.) NOx (0 kg) is not found in the flue gas exhaust product.

F. Kerosene and air - (exhaust temperature of 1059. 44 ° C) F. Kerosene and air - (cont.

It is determined that the escape product includes 669. 37 kg of NOx. Tables E and F show that when the same amount of kerosene is burned in the apparatus using air, instead of LOX, as the oxidant, the procedure results in a significant increase in the environmental pollutant by NOx titration.

EXAMPLE 3 Comparison of flue gas exhaust products using different fuels designed The combustion products are determined using the GUIPEP computer thermochemical software based on the use of different fuels in the 10 MW hydrocarbon combustion gas generator described in example 1. The test is based on burning 907.2 kg of each one. of the fuels using LOX as the oxidant, in which each flue gas exhaust product leaves the hydrocarbon combustion gas generator at a pressure of approximately 42.18 kg / cm2 gauge. The following tables indicate the composition and temperature of the exhaust gas, as well as the weight, moles, and weight percent of each component present in the flue gas exhaust product.

A. Fuel EF-1 (exhaust temperature of 1530.56 ° C) A. Fuel EF-1 (cont.) It is determined that the exhaust product includes 0.8399 kg of NOx (0.093% by weight).

B. Fuel EF-2 (exhaust temperature of 1645. 56 ° C) B. Fuel EF-2 (cont) It is determined that the exhaust product includes 1176 kg of NOx (0.130% by weight).

C. Fuel EF-3 (exhaust temperature of 1645. 56 ° C) C. Fuel EF-3 (cont.) It is determined that the escape product includes 2. 969 kg of NOx (0.327% by weight).

D. Fuel EF-4 (exhaust temperature of 1588. 33 ° C) D. Fuel EF-4 (cont.) It is determined that the exhaust product includes 1,616 kg of NOx (0.178% by weight).

E. Fuel EF-5 (exhaust temperature of 1591. 11 ° C) E. Fuel EF-5 (cont.) It is determined that the exhaust product includes 5,675 kg of NOx (0.624% by weight).

F. Fuel EF-6 (exhaust temperature of 1596. eleven) It is determined that the exhaust product includes 681 kg of NOx (0.516% by weight).

G. Fuel EF-7 (exhaust temperature of 1553. 89 ° C; It is determined that the exhaust product includes 3,487 kg of NOx (0.384% by weight).

H, Fuel EF-8 (exhaust temperature of 1584. 44 ° C) It is determined that the exhaust product includes 1830 kg of NOx (0.201% by weight).

I. Fuel EF-9 (exhaust temperature of 1580 ° C) I. Fuel EF-9 (cont.) It is determined that the escape product includes 2. 216 kg of NOx (0.244% by weight).

J. Fuel EF-10 (exhaust temperature 1626. 67 ° C) J. Fuel EF-10 (cont.) It is determined that the exhaust product includes 3,986 kg of NOx (0.439% by weight).

K. Fuel EF-11 (exhaust temperature of 1718. 89 ° c; K. Fuel EF-11 (cont.

It is determined that the exhaust product includes 3,464 kg of NOx (0.382% by weight).

L. Fuel EF-12 (exhaust temperature of 1477. 22 ° C) L. Fuel EF-12 (cont.) It is determined that the escape product includes 3. 432 kg of NOx (0.378% by weight).

M. Fuel EF-13 (exhaust temperature of 1554. 44 ° C) M. Fuel EF-13 (cont.) It is determined that the exhaust product includes 3,205 kg of NOx (0.353% by weight).

N. Fuel EF-14 (exhaust temperature of 1549. 44 ° C) N. Fuel EF-14 (cont.) It is determined that the exhaust product includes 4,081 kg of NOx (0.449% by weight).

O. Fuel EF-15 (exhaust temperature 1649. 44 ° C) N0X (0 kg) is not found in the flue gas exhaust product.

P. Fuel EF-16 (exhaust temperature of 1650 ° C) NOx (0 kg) is not found in the flue gas exhaust product. In general, this example shows that when air is burned with a fuel, high levels of atmospheric environmental pollutants, such as N0X, S0X, CO and particulate matter, generally occur, and that it would be desirable to use a purer oxygen source. These emissions are in, and in some cases are higher than, the critical threshold levels allowed by the federal and / or state governments, and need to be reduced in order to conserve clean air.

EXAMPLE 4 Comparison of the emission rates of CQ2, N0X and SQ2 per megawatt of electricity produced using different fuels In the United States of America, average emission rates from conventional coal-fired power plants for each megawatt of electricity produced are: However, depending on the quality of the coal, uncontrolled S02 emissions can vary from 3,178 to 27.24 kg per MW / h of electricity produced, and uncontrolled NOx emissions can vary from 4.54 to more than 9.08 kg per megawatt / hour of electricity produced. Current waste combustion practices in many power plants result in the release of toxic chemicals into the environment, normally present in waste for combustion, such as volatile ash. In the United States of America, average emission rates from power plants that use natural gas for each megawatt of electricity produced are: The amount of C02, NOx and S02 present in the exhaust product of flue gas per megawatt / hour (MWh) of electricity that occurs when the designed fuels described below are separately burned in the hydrocarbon combustion gas generator 10 MW described in Example 1 (using LOX as the oxidant, and each flue gas exhaust product leaves the hydrocarbon combustion gas generator at a pressure of 42.18 kg / cm2 gauge and at a temperature of 1481.11 ° C) they are determined using the GUIPEP computer program. The results, together with the amount of fuel used per megawatt / hour of electricity produced, are indicated in the following table. In each case, and in the tables above for coal and natural gas, one megawatt hour of electricity is produced using 859824 kcalories (3,412,000 BTUs) of fuel.

The table above shows that the number of exhaust components of the combustion gas C02, NOx, and S02 produced by megawatts of electricity produced using these fuels is significantly lower than the average emissions of these components per megawatt of electricity produced in the United States of America using conventional coal or natural gas combustion processes.

EXAMPLE 5 Generation of 25 megawatts of electricity using different fuels Combustible oils are usually a mixture of hydrocarbons obtained from the refining of crude oil. ASTM D 396 provides specifications for fuel oil properties that divide fuel oils into several grades: grade # 2 fuel oil is a heavy distillate that is used primarily with pressure atomized (gun) burners that sprinkle petroleum inside a combustion chamber; # 4 grade fuel oil is an intermediate fuel intended for burners that atomize oils of higher viscosity than those that domestic burners can handle; and grade 6 fuel oil (Bunker C) is a high viscosity fuel oil used primarily in commercial and industrial heating. The following table shows a comparison between several variables in the production of 25 megawatts of electricity per kilogram of fuel per hour [8,397.52 kcal / s (119,967,930 BTU / hr), 79450 kg (175,000 Ibs) of superheated steam product per hour , 25,000 kW per hour and 218,400,000 kW per year] using the hydrocarbon combustion gas generator described in example 1 using six different types of fuels, including bituminous coal, fuel grades # 2, # 4 and # 6, and LOX as the oxidant (determined using the GUIPEP computer software). The costs associated with the EF-8 fuel include the receipt of tolling fees. The amount of LOX used varies, depending on the type of fuel used, with different resulting 0 / F ratios. The operating cost per 25,000 kw hour for all fuels is $ 270.39. The values in parentheses are negative.

The above table shows that, when the EF-8 fuel is used to produce the same amount of electrical energy as the other five fuels indicated (all in the apparatus described in example 1), using the same oxidant, the fuel cost is reduced significantly (a reduction that varies from approximately 89.5% to approximately 94.5%), which results in a significantly reduced total cost per kw / hour (a reduction ranging from approximately 43% to approximately 73%).

EXAMPLE 6 Hydrocarbon combustion gas generator "GG-1X" A 1 MW hydrocarbon combustion gas generator named "GG-1X" is built. This is equal to the same generator, but at half the scale / size, of Example 1. The GG-1X generator can process approximately 454 kg / hour of waste fuel (ie, fuel that is produced from waste materials). waste).

EXAMPLE 7 Injectors of the first combustion chamber of GG1-X and short-duration intense fire test of combustion stability A first test (LF-JP5-LOX-001-first test) is performed with the GG-1X hydrocarbon combustion gas generator to observe the combustion stability in the first combustion chamber using a low 0 / F ratio. It is used as the fuel kerosene (Kl) ("JP5", a high-grade kerosene known in the art containing anti-freeze and antifungal additives), and LOX is used as the oxidant. Deionized water is used to cool the first combustion chamber. Nitrogen gas is used to purge the fuel and oxidant systems. The building materials of the combustor are the following: the fuel inlet manifold, the fuel meter block, and the first combustion chamber are made of carbon steel. The first oxidant distributor plate is made of stainless steel. The first oxidizer injector orifices and the first fuel injector holes are made of bronze. The planned duration of the test is 5.0 seconds maximum and the actual duration is 5.6 seconds. The oxidant: fuel ratio (0 / F) is 2.75. The operating pressure in the first combustion chamber is 21.09 kg / cm2 gauge. The reactants are supplied to the reactor as shown in detail in the following table: There is no calcination of the combustion chamber (that is, the integrity of the first combustion chamber is fully maintained). This test is successful because the performances of the first combustion chamber and the injector are satisfactory. The pressures measured at various times and locations during the test are indicated in the following table.

In this test some instability of combustion is observed. A post-test inspection indicates that a LOX check valve has become stuck. The valve is replaced with a new one, and the test is repeated as indicated in detail in example 8.

EXAMPLE 8 Injectors of the first combustion chamber of GG1-X and short-duration intense fire test of combustion stability (second test) A second test (LF-JP5-LOX-002-second test) is carried out with the GG-1X using the same parameters as those described in example 7. The test lasts for 5.6 seconds and no calcination of the chamber occurs of combustion. No instability of the combustion is observed. A post-test inspection indicates that the performances of the first combustion chamber and the injector are satisfactory. Therefore, it is considered that the test is successful. The pressures measured at various times and locations during the test are indicated in the following table The publications cited in the present invention and the materials for which they are cited are incorporated specifically for reference. Modifications and variations of the methods and devices described in the present invention will be apparent to the person skilled in the art from the above detailed description. It is intended that said modifications and variations fall within the scope of the appended claims.

Claims (36)

NOVELTY OF THE INVENTION Having described the present invention, it is considered as a novelty and therefore the content of the following is claimed as property: CLAIMS

1. An apparatus for use as a hydrocarbon combustion gas generator comprising: a first combustion chamber in which a first combustion of fuel and oxidant can be effected to produce an incomplete combustion product, the first combustion chamber has a end of entry and one end of exit; control and dosing means for dosing separately a fuel and an oxidant within the first combustion chamber to achieve incomplete combustion of the fuel in the first chamber; a second combustion chamber in which a second combustion of fuel and additional oxidant can be effected to produce a second combustion product, the second combustion chamber has an inlet end and an exit end in which the inlet end of the combustion chamber the second combustion chamber is in fluid communication with the outlet end of the first combustion chamber; control and dosing means for dosing additional oxidant into the second combustion chamber for additionally burning fuel in the second chamber; means for dosing into the second combustion chamber the incomplete combustion product that is produced in the first combustion chamber; and heat exchanger means for cooling the first and second combustion chambers and optionally converting the cooling water to steam, characterized in that the cooling water and steam are kept separate from the combustion gases produced by the first and second combustion gases. second combustions.

2. The apparatus according to claim 1, characterized in that the second combustion is a complete combustion.

3. The apparatus according to claim 1, further comprising: a third chamber or combustion space in which a third combustion of the fuel and additional oxidant can be effected to produce a third combustion product; control and dosing means for dosing additional oxidant within the third chamber or combustion area to burn additionally fuel in the third chamber or area; and additional heat exchanger means for cooling the third chamber or combustion area and for optionally converting the cooling water to steam, in which the cooling water and the steam are kept separate from the combustion gases produced by the third combustion.

4. The apparatus according to claim 3, which also comprises means for metering into the third combustion chamber the incomplete combustion product that is produced in the second combustion chamber

5. The apparatus according to any of the claims 1 to 4, characterized in that the unmeasured air is not allowed to mix with the fuel or the oxidant in the combustion chambers.

6. The apparatus according to any of claims 1 to 5, characterized in that the means for dosing into the second combustion chamber the incomplete combustion product produced in the first combustion chamber comprises a plurality of tubular openings.

7. - The apparatus according to any of claims 1 to 5, characterized in that the control and dosing means for separately metering a fuel and an oxidant into the first combustion chamber the fuel and the oxidant comprise a plurality of holes near the entrance end of the first combustion chamber.

8. The apparatus according to claim 7, characterized in that the fuel, the oxidant, or both are metered into each of the chambers or combustion areas in an inclined manner, which results in at least one point of collision between the fuel and the oxidant.

9. The apparatus according to any of claims 1 to 8, characterized in that the heat exchanger means comprises a plurality of tubes forming one or more tube assemblies, having at least one cooling water inlet and at least one steam outlet.

10. The apparatus according to claim 9, characterized in that the tube assemblies form walls that define one or more of the combun chambers or areas.

11. The apparatus according to any of claims 1 to 10, characterized in that the control and dosing means for separately dosing a fuel are adapted to dose two or more types of fuel separately within the first combun chamber.

12. The apparatus according to any of claims 1 to 11, which also comprises an electronic ignition system or other means for igniting the fuel in the first combun chamber.

13. The apparatus according to any of claims 1 to 12, which also comprises a source of oxidant.

14. The apparatus according to claim 13, characterized in that the oxidant is a liquid oxidant.

15. The apparatus according to claim 13 or 14, characterized in that the oxidant is selected from LOX, O, 03, H202 or HAN.

16. The apparatus according to any of claims 1 to 15, which also comprises a source of one or more fuels.

17. The apparatus according to claim 16, characterized in that at least one fuel is in the form of solid particles.

18. The apparatus according to claim 17, characterized in that the solid fuel comprises pla, rubber, or other waste materials.

19. The apparatus according to claim 17, characterized in that the solid fuel has a particle size ranging from about 31 to about 2,300 microns.

20. The apparatus according to any of claims 16 to 19, characterized in that at least one additional fuel is a liquid or gaseous fuel.

21. The apparatus according to any of claims 16 to 20, characterized in that the fuel comprises EF-1, EF-2, EF-3, EF-4, EF-5, EF-6, EF-7, EF -8, EF-9, EF-10, EF-11, EF-12, EF-13, EF-14, EF-15, EF-16, EF-17 or EF-18.

22. The apparatus according to any of claims 1 to 21, characterized in that the apparatus burns from about 97% to about 100% of the fuel metered in the first combun chamber.

23. A system for generating electricity comprising: the apparatus according to any of claims 1 to 22, which generates steam; and an electric power generating device driven by said steam.

24. - The system according to claim 23, characterized in that the electric power generator comprises a steam-driven turbine.

25. The system according to claim 23 or 24, which can produce from 1 to approximately 600 megawatts of electric power per day.

26. The system according to any of claims 23 to 25, which is a cogeneration system, a tri-generation system, or a quad-generation system.

27. A combustion process comprising: supplying at least one fuel to the apparatus according to any of claims 1 to 25; supplying at least one oxidant to said apparatus; and burning said fuel and said oxidant in said apparatus.

28. The process according to claim 27, characterized in that the first combustion occurs at a temperature ranging from

648. 88 ° C approximately to 3204.44 ° C approximately, to a pressure that varies from approximately 35.15 kg / cm2 to approximately 105.45 kg / cm2 gauge and during a period that varies from approximately 0.025 to approximately 10 seconds.

29. The process according to claim 28, characterized in that the second combustion occurs at a temperature ranging from approximately 1648.88 ° C to approximately 3204.44 ° C, at a pressure ranging from approximately 21.09 kg / cm2 to 105.45 kg. / cm2 approximately and for a period that varies from approximately 0.025 to approximately 10 seconds.

30. The process according to any of claims 27 to 29, characterized in that the oxidant comprises LOX.

31. The process according to any of claims 27 to 29, characterized in that the fuel comprises a material that is not waste.

32. The process according to claim 31, characterized in that the non-waste material comprises wood, coal, hydrogen, methane, ethane, butane, propane, natural gas, gasoline, diesel fuel, kerosene, fuel oil, methanol, alcohol, a product that contains plastic, mixed plastic or plastic resin, or a combination thereof.

33.- The process according to any of claims 27 to 32, characterized in that the exhaust product of combustion gas does not contain, or contains insignificant amounts of, mercury, SO, S02, S03, NO, N02, N20, CO. , CH4, HCl or dioxin.

34. A method for the disposal of hazardous or waste materials, comprising: supplying a fuel to the apparatus according to any of claims 1 to 25, characterized in that the fuel comprises at least one hazardous or waste material; supplying at least one oxidant to said apparatus; and burning said fuel and said oxidant in said apparatus.

35. The method according to claim 34, characterized in that the hazardous material comprises infectious medical waste, biological or chemical weapons, components thereof, or a container for them.

36. The method according to claim 34, characterized in that the waste material comprises used tires, plastic-based packaging materials, or components thereof.