CN207584765U - For generating the catalysis combustion plant and 3 stage catalytic combustion plants of energy with high efficiency - Google Patents

Abstract

The utility model relates to a catalytic combustion facility for generating energy with high efficiency and a three-stage catalytic combustion facility. The catalytic combustion facility (CAB) comprises at least the following components: a primary air supply (AIR1) for delivering at least 90% of the air required in the catalytic combustion (CAB) as primary air (AIR1) to said catalytic combustion in the front part (CAS) of the facility (CAB); at least two successive fuel supply sources (FU1, FU2, FU3, FU4) for feeding fuel into said catalytic combustion facility (CAB); and at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4); at least one heat transfer component (HT1, HT2, HT3); combustion generating Exhaust device (EXH) for gas (EXG).

Description

Catalytic combustion facility and 3-stage catalytic combustion for energy generation with high efficiency facility

technical field

The utility model relates to a method for generating energy with high efficiency and very low emissions. The utility model also relates to equipment suitable for the method, as well as the manufacture and use of the equipment.

Background technique

The world is restricting the emissions of nitrogen oxides, carbon monoxide, carbon dioxide and hydrocarbons from energy production to curb the greenhouse effect. In Europe, several directives have been proposed for thermal boilers, process equipment, furnaces etc. for this purpose. These directives include emission standards for greenhouse gases defined directly or indirectly through efficiency. In the United States, the EPA (Environmental Protection Agency) and especially CARB (California Air Resources Board) have enforced strict regulations on nitrogen oxides and hydrocarbons, some in compound-specific forms. CO2 emissions are monitored through the efficiency of boilers and furnaces. China is going through a similar development. In Beijing, for example, the limit value has been set to 30 mg/m ³ for nitrogen oxides from boilers, and 80 mg/m ³ for carbon monoxide gas. These are such stringent criteria that cannot be achieved with current conventional thermal combustion facilities without further processing. The same trend of vigorous retrenchment will continue in other areas of industrialization in China.

The Global Climate Forum is seeking options for a global agreement to stem the rise of greenhouse gases and achieve a steady decline. The most difficult aim is to curb the burning of fossil fuels, especially coal. The carbon dioxide formed in the combustion is accompanied by a large amount of nitrogen oxides. When the temperature rises above 1100 ° C, the accumulation of nitrogen oxides accelerates rapidly. In the case of no loss of efficiency, this is the case in the thermal combustion of gases and liquids. unavoidable. The American Boiler Manufacturers Association (ABMA), operating in the United States, has about 800 member companies. Manufacturers of lower output boilers (<115kW) are not eligible for membership. Based on this, a high approximation is that there are 4000-5000 companies manufacturing this size worldwide, and therefore the number of boilers manufactured is approximately 500.000 pcs/year.

Instead of flue gas aftertreatment, commercial manufacturers of ultra-low NO _x (UltraLow NO _x ) and NO _x (Zero NO _x ) burners use flue gas recirculation, water emulsification, and Gas preheating. Despite being called _NOx -free, no thermal combustion manufacturer has achieved zero _NOx emissions. The lowest reported value is all 6 ppm (about 12 mg/m ³ ) at 3% oxygen level.

The second option is the cleaning of the flue gas. The removal of nitrogen oxides is usually carried out by using selective or non-selective catalytic converters (SCR, NSCR). The highest cleaning rate thus obtained was about 98% at a temperature of about 300°C. However, SCR catalytic converters require a separate reductant, urea or ammonia, which incurs an additional cost of about 4% in fuel costs. _NOx emission levels thus achievable are about 5-20 ppm. In addition, CO emission standards often require separate oxidation catalytic converters.

As a new product, there is already a 3-way catalytic converter in the market, which is common in automobiles and suitable for boilers, but the adjustment of the air/fuel ratio is subject to the strict regulations of the 3-way catalytic converter. This technology even makes it possible to obtain currently quite stringent _NOx and CO limit values.

As a summary of the above, it can be concluded that thermal combustion and the cleaning method of flue gas associated with it cannot produce thermal energy that is practically emission-free ( _NOx , VOC and CO), which can be used with the catalytic combustion equipment of the present invention and clean fuels to produce. Thus, even the only harmful emissions, ie carbon dioxide (CO 2 ), can be utilized eg in the fertilization of plants, as protective gas, industrial raw material, etc.

Plants are about 100 times more sensitive than humans to nitrogen oxides ( _NOx ), sulfur oxides ( _SOx ), hydrogen sulfide (H2S) and ethylene (C2H4) than humans (see table below). In the case of the catalytic oxidation method of the invention, even emission levels required by plants can be achieved. The table that follows shows the acceptable concentrations for humans in the working environment for the most important hazardous gases (male, 8h working day) compared to the acceptable concentrations for plants.

CO2 fertilization is most useful in vegetable cultivation. Finland currently has about 1000 greenhouses in vegetable cultivation, and about 330 of these greenhouses perform fertilization by using a total of about 5 million kg/year of liquid or gaseous carbon dioxide. The price range is wide: in the largest consignment, liquid CO ₂ costs about 0,10 €/kg, while bottled CO ₂ costs about 1,5 €/kg. Compared to the consumption in Finland, it is estimated that the global consumption is more than 200 times the consumption in Finland. In greenhouse use, the market for _CO2 is about 300 million €/year, but the market could be much larger if liquid _CO2 used in small greenhouses were not so expensive.

The fuel must not contain any compounds harmful to catalytic converters, such as organo-noble metals and silicon compounds, nor halogenated hydrocarbons. Likewise, the amount of particles must be limited (recommended less than 1 mg/Nm ³ ).

Utility model content

What is now claimed is a method for generating energy with high efficiency and very low emissions. The utility model also relates to a device suitable for the method and the manufacture and use (purpose) of the device.

According to a first aspect of the present utility model, a catalytic combustion facility for generating energy with high efficiency is characterized in that the catalytic combustion facility comprises at least the following components:

- a primary air supply source for delivering at least 90% of the air required in catalytic combustion as primary air into the front part of said catalytic combustion plant;

- at least two successive fuel supply sources for feeding fuel into said catalytic combustion facility; and at least two successive catalytic combustion stages, in each stage, by delivery to the front part of said catalytic combustion facility The primary air in the 0.015-0.10s time frame only catalytically burns the sequentially supplied fuel step by step, so that the temperature in said catalytic combustion phase is higher than 800°C and lower than 1100°C,

wherein said catalytic combustion is provided such that said catalytic combustion is carried out with excess air measured on the basis of residual oxygen and the fuel/air ratio in said catalytic combustion stage is below the lower explosive limit, and

wherein the catalytic converter used in said catalytic combustion stage is a hybrid catalytic converter comprising noble metal from a metal honeycomb;

- at least one heat transfer element for reducing the temperature of gases produced in at least one successive catalytic combustion stage, and said heat transfer element precedes the next successive catalytic combustion stage;

- Exhaust means for exhausting combustion-generated gases in the tail section of said catalytic combustion plant.

Further, the tail section of the catalytic combustion facility is provided with at least one residual heat transfer component for reducing the temperature of the combustion gas downstream of the catalytic combustion stage.

Further, the heat transfer part and/or the residual heat transfer part has a tubular design.

Further, the amount of residual oxygen is 0.5-10%.

Further, the catalytic combustion facility is provided with at least one static mixer before the catalytic combustion stage.

Further, the catalytic combustion facility is provided with a secondary air supply source, the secondary air supply source is used to deliver air, and the air delivered by the secondary air supply source is not more than required in the catalytic combustion 10% of air.

Further, there is a heat exchanger between the catalytic converters.

Further, a temperature sensor is arranged downstream of the catalytic converter.

Further, said primary air supply source is used to deliver at least 99% of the air required in catalytic combustion as primary air into the front part of said catalytic combustion plant.

Further, in each of said at least two successive catalytic combustion stages, only gradually catalytic The sequentially supplied fuel is combusted such that the temperature in said catalytic combustion stage is higher than 800°C and lower than 1000°C.

Further, the heat transfer part and/or the residual heat transfer part has a finned tube design.

Further, the amount of residual oxygen is 1-3%.

On the other hand, a 3-stage catalytic combustion facility is characterized in that the 3-stage catalytic combustion facility comprises at least the following components:

- a primary fuel supply for supplying at least 90% of the fuel required in catalytic combustion into the front part of said 3-stage catalytic combustion plant;

- 3 successive oxygen supply sources for feeding oxygen into said 3-stage catalytic combustion facility; and 3 successive catalytic-only combustion stages for progressively burning said fuel with delivered oxygen;

- two successive heat transfer elements for reducing the temperature of the gases produced in three successive catalytic combustion stages, and said heat transfer elements precede the next successive catalytic combustion stage;

- an exhaust device for exhausting gases generated by combustion in the tail section of said 3-stage catalytic combustion plant,

Therein, the catalytic converter used in the catalytic combustion stage is a hybrid catalytic converter comprising noble metal from a metal honeycomb.

Further, the tail part of the 3-stage catalytic combustion facility is provided with a residual heat transfer component for reducing the temperature of the gas generated by the combustion after the catalytic combustion stage.

Further, the three-stage catalytic combustion facility also includes a condenser for the gas generated by combustion.

Further, the catalytic converter used in the catalytic combustion stage is provided with a heat exchanger having diagonally corrugated plates stacked in a vertical direction so that crests of the corrugations cross each other in different directions, To create cross-extended flow channels in the shape of a letter X, thereby creating a hybrid honeycomb structure.

Further, the hybrid honeycomb structure of the catalytic converter is welded at its ends to be attached to the casing.

Further, said primary fuel supply source supplies at least 99% of the fuel required in catalytic combustion to the front part of said 3-stage catalytic combustion facility.

On the other hand, the fuel/air ratio in the catalytic combustion stages CA1 , CA2 , CA3 , CA4 is below the LEL (Lower Explosive Limit). First kind of method of the present utility model comprises the following steps at least:

- delivering at least 90%, preferably at least 99%, of the air required in the catalytic combustion (CAB) as primary air (AIR1) into the front part of the catalytic combustion plant (CAB);

- feeding the fuel (FU1, FU2, FU3, FU4) into the catalytic combustion plant (CAB) in at least two successive stages, and in at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4) in In each stage, by primary air (AIR1) delivered to the front part (CAS) of the catalytic combustion facility (CAB), within a time frame (time frame) of 0,015-0,10 s, preferably at 0 In the range of ,02-0,06s, only sequentially supplied fuels (FU1, FU2, FU3, FU4) are catalytically combusted step by step, so that the temperature in the catalytic combustion phases (CA1, CA2, CA3, CA4) is higher than 800°C and Below 1100°C, preferably below 1000°C, where catalytic combustion is performed with excess air measured as residual oxygen and the fuel/air ratio in the catalytic combustion stages (CA1, CA2, CA3, CA4) is at LEL (lower explosion limit);

- reducing the temperature of the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4) in at least one heat transfer stage (HT1, HT2, HT3) which heat transfer stage (HT1, HT2, HT3) before the next catalytic combustion stage (CA1, CA2, CA3, CA4);

- Removal of combustion gases (EXG) from the tail section (CAL) of the combustion facility (CAB).

This approach provides simple technical application and the process becomes efficient and the resulting emissions will be extremely low.

Residual oxygen in this application means the amount (w/w) of oxygen in the gas produced by combustion after catalytic combustion.

According to a second aspect of the invention, the fuel/air ratio in the catalytic combustion stages CA1 , CA2 , CA3 , CA4 is above the UEL (Upper Explosion Limit). Second kind of method of the present utility model comprises the following steps at least:

- delivering at least 90%, preferably at least 99%, of the fuel (FUE) in the catalytic combustion (CAB) to the front part of the catalytic combustion facility (CAB);

- Feed oxidizing gas or liquid (OXY) into the catalytic combustion plant (CAB) in at least two successive stages, and in each stage, within a time frame of 0,015-0,10 s, preferably within 0,02- Within a time frame of 0,06 s, only the feed fuel (FUE) in at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4) is catalytically burnt step by step, so that in the catalytic combustion stages (CA1, CA2, CA3 , CA4) where the temperature is higher than 800°C and lower than 1100°C, preferably lower than 1000°C, and wherein the fuel/air ratio in the catalytic combustion stages (CA1, CA2, CA3, CA4) is within the UEL (Upper Explosion Limit ) above;

- reducing the temperature of the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4) in at least one heat transfer stage (HT1, HT2, HT3) which heat transfer stage (HT1, HT2, HT3) before the next catalytic combustion stage (CA1, CA2, CA3, CA4);

- Removal of combustion gases (EXG) from the tail section (CAL) of the combustion facility (CAB).

At this point the temperature is high enough to burn the fuel efficiently. At the same time the temperature is so low that no _NOx emissions are generated. Temperature also favors assembly (assembly).

According to one aspect of the invention, the invention includes delivering not more than 10%, preferably not more than 1%, of the air required in the catalytic combustion CAB as secondary air AIR2 to the front part CAS of the catalytic combustion facility CAB downstream. According to one aspect of the invention, the invention includes delivering at least 99% of the air required in the catalytic combustion CAB as primary air AIR1 into the front part CAS of the catalytic combustion plant CAB. This provides a further enhancement to combustion and/or its efficiency.

In the combustion according to the invention, including only catalytic combustion, no NOx emissions or very low NOx concentrations will result. There is therefore no need to remove NOx from the exhaust gas. Carbon monoxide (CO) and hydrocarbon (CH) emissions will also be extremely low. This offers both technical and economic advantages with high efficiency and very low emissions compared to prior art processes.

According to one aspect of the invention, the invention comprises feeding the fuels FU1, FU2, FU3, FU4 into the catalytic combustion plant CAB in at least three successive The primary air AIR1 burns the sequentially supplied fuels FU1 , FU2 , FU3 , FU4 step by step in at least three successive catalytic combustion stages CA1 , CA2 , CA3 , CA4 . Accordingly, the invention includes reducing the temperature of the gas EXG generated in at least two successive catalytic combustion stages CA1, CA2, CA3, CA4 in at least two heat transfer stages HT1, HT2, HT3, said heat transfer stage HT1 , HT2, HT3 before the next successive catalytic combustion stages CA1, CA2, CA3, CA4. This provides a further enhancement of combustion and/or its efficiency.

According to one aspect of the invention, the invention comprises feeding the fuels FU1, FU2, FU3, FU4 into the catalytic combustion plant CAB in at least four successive The primary air AIR1 burns sequentially supplied fuels FU1 , FU2 , FU3 , FU4 step by step in at least four successive catalytic combustion stages CA1 , CA2 , CA3 , CA4 . Accordingly, the invention includes reducing the temperature of the gas EXG generated in at least two successive catalytic combustion stages CA1, CA2, CA3, CA4 in at least three heat transfer stages HT1, HT2, HT3, said heat transfer stages HT1, HT2, HT3 precede the next successive catalytic combustion stages CA1, CA2, CA3, CA4. This provides a further enhancement of combustion and/or its efficiency.

According to one aspect of the invention, the invention includes delivering at least 99% of the air required in the catalytic combustion CAB as primary air AIR1 into the front part CAS of the catalytic combustion plant CAB. According to one aspect of the invention, the invention includes delivering not more than 10% of the air required in the catalytic combustion CAB as secondary air AIR2 downstream of the front part CAS of the catalytic combustion plant CAB. This provides a further enhancement of combustion and/or its efficiency.

According to one aspect of the invention, the invention comprises reducing the temperature of the combustion gas EXG in at least one residual heat transfer stage HT4 in the tail section CAL of the combustion plant CAB downstream of the catalytic combustion stages CA1, CA2, CA3, CA4 . According to one aspect of the invention, the invention comprises cooling the combustion gas EXG to a temperature of 150-350° C. in the heat transfer stages HT1 , HT2 , HT3 and/or in the residual heat transfer stage HT4 . According to one aspect of the invention, the invention comprises recovering the heat energy contained in the combustion gas EXG in at least one heat transfer stage HT1, HT2, HT3 and/or in the residual heat transfer stage HT4, and transferring the heat energy to water, air or other liquid or gaseous substances. According to one aspect of the invention, the invention consists in utilizing the thermal energy contained in the gases EXG and/or CO ₂ produced by combustion directly at the point of use, preferably in a greenhouse. This provides a further enhancement of combustion and/or its efficiency.

According to an aspect of the invention, the supplied fuels FU1 , FU2 , FU3 , FU4 are gaseous and/or liquid. According to one aspect of the present invention, the supplied fuels FU1, FU2, FU3, FU4 are selected from the group including natural gas, biogas, liquefied gas, light fuel oil, alcohols, carbon monoxide, and substances generated in wood heat treatment. Other flammable gases and liquids are also possible. This provides a further enhancement of combustion and/or its efficiency. Oxidation is preferably carried out by air in several stages. Oxygen and other oxidizing liquid or gaseous substances can also be used.

According to an aspect of the invention, the temperature in the catalytic combustion stages CA1, CA2, CA3, CA4 is less than 1100°C, preferably less than 1000°C, even more preferably less than 900°C. According to an aspect of the invention, the combustion in the catalytic combustion phases CA1 , CA2 , CA3 , CA4 takes place within a time frame of 0,015-0,10 s. This provides a further enhancement of combustion and/or its efficiency.

According to one aspect of the present invention, the total efficiency of the catalytic combustion is at least 99% when calculated by converting the energy contained in the fuel into heat energy. This provides a further enhancement of combustion and/or its efficiency.

According to an aspect of the present invention, the concentration of nitrogen oxides NO _x in the exhaust gas EG from the catalytic combustion is less than 1 ppm on average. According to an aspect of the invention, the concentration of carbon monoxide CO in the exhaust gas EG from catalytic combustion is on average less than 1 ppm. According to an aspect of the present invention, the concentration of volatile hydrocarbons VOC in the exhaust gas EG from the catalytic combustion is less than 1 ppm on average. This provides a further enhancement of combustion and/or its efficiency.

According to one aspect of the invention, the percentage of the first and/or second fuel supply FU1 relative to the total amount of fuels FU1, FU2, FU3, FU4 supplied to the catalytic combustion facility CAB is based on the calorific value of the fuel It is determined in such a way that the temperature of the first catalytic converter does not rise to more than 1000° C., preferably not to rise to more than 900° C. This provides a further enhancement of combustion and/or its efficiency.

According to an aspect of the invention, the catalytic combustion stages CA1, CA2, CA3, CA4 are carried out by using a hybrid catalytic converter comprising noble metals from metal cells. This provides a further enhancement of combustion and/or its efficiency.

According to an aspect of the invention, the last catalytic converter may be larger than the other catalytic converters in order to ensure clean combustion. Depending on the fuel, the preceding catalytic converter can have a throughput varying in the range 60.000-300.000 1/h. In the last catalytic converter the throughput can preferably be 30.000-200.000 1/h. This provides a further enhancement of combustion and/or its efficiency.

The catalytic combustion equipment according to the first aspect of the utility model can be manufactured through the following steps:

- provide the catalytic combustion plant (CAB) with at least one front section (CAS) comprising at least one primary air supply source (AIR1) for delivering at least 90% of the air required in the catalytic combustion (CAB), Preferably at least 99%;

- downstream of the front section (CAS), at least two successive fuel supply sources (FU1, FU2, FU3, FU4) are provided for the catalytic combustion plant (CAB) for feeding fuel into the catalytic combustion plant (CAB);

- provide the catalytic combustion plant (CAB) with at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4), in each stage, by Primary air (AIR1), within the time frame of 0,015-0,10s, preferably within the time frame of 0,02-0,06s, only progressively catalytically burns the sequentially supplied fuels (FU1, FU2, FU3, FU4) , such that the temperature in the catalytic combustion stages (CA1, CA2, CA3, CA4) is more than 800°C and less than 1100°C, preferably less than 1000°C, wherein the catalytic combustion is carried out with an excess of air measured as residual oxygen, and The fuel/air ratio in the catalytic combustion stages (CA1, CA2, CA3, CA4) is below the LEL (Lower Explosive Limit);

- Provide a catalytic combustion facility (CAB) with at least one heat transfer component (HT1, HT2, HT3) for reducing the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4) temperature, and said heat transfer components (HT1, HT2, HT3) are located before the next successive catalytic combustion stage (CA1, CA2, CA3, CA4);

- Provision of an exhaust plant (EXH) for the catalytic combustion plant (CAB) for combustion gases (EXG) in the tail section (CAL) of the combustion plant (CAB).

The catalytic combustion equipment according to the second aspect of the present invention can be manufactured through the following steps:

- providing at least one front section (CAS) for the catalytic combustion plant (CAB) comprising at least one primary fuel supply source (FUE) for delivering at least 90%, preferably at least 99%;

- provision of at least two successive oxidizing gas or liquid supply sources (OXY) downstream of the front section (CAS) for the catalytic combustion plant (CAB) for feeding fuel into the catalytic combustion plant (CAB);

- Provide a catalytic combustion facility (CAB) with at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4), in each stage, within a time frame of 0,015-0,10 s, preferably within 0,02 - Within a time frame of 0,06s, burn the fuel (FUE) only stepwise catalytically so that the temperature in the catalytic combustion phases (CA1, CA2, CA3, CA4) is more than 800°C and less than 1100°C, preferably less at 1000°C and wherein the fuel/air ratio in the catalytic combustion stages (CA1, CA2, CA3, CA4) is above the UEL (Upper Explosion Limit);

- Provide a catalytic combustion facility (CAB) with at least one heat transfer component (HT1, HT2, HT3) for reducing the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4) temperature, and said heat transfer components (HT1, HT2, HT3) are located before the next successive catalytic combustion stage (CA1, CA2, CA3, CA4);

- Provide an exhaust device (EXH) for the catalytic combustion plant (CAB) in the aft part (CAL) of the combustion plant (CAB) for exhausting the gases (EXG) generated by the combustion,.

According to one aspect of the invention, the catalytic combustion facility CAB is provided in its tail section CAL with at least one residual heat transfer stage HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1, CA2, CA3, CA4 . According to an aspect of the invention, the heat transfer parts HT1 , HT2, HT3 and/or the residual heat transfer stage HT4 have a tubular design. According to an aspect of the invention, the sequential fuel supplies FU1, FU2, FU3, FU4 are suitably gaseous or liquid fuels. According to one aspect of the invention, the catalytic converters used in the catalytic combustion stages CA1 , CA2 , CA3 , CA4 are hybrid catalytic converters comprising noble metals from metal honeycombs. According to one aspect of the present invention, downstream of the front part CAS of the catalytic combustion facility CAB, the catalytic combustion facility CAB is provided with a secondary air supply source AIR2, which can be used to deliver the air required in the catalytic combustion CAB. not more than 10% of the air.

The catalytic combustion facility according to the first aspect of the present utility model comprises:

- a primary air supply source (AIR1) for delivering at least 90%, preferably at least 99%, of the air required in the catalytic combustion (CAB) as primary air (AIR1) to the front part of the catalytic combustion plant (CAB) ( CAS);

- at least two successive fuel supply sources (FU1, FU2, FU3, FU4) for feeding fuel into a catalytic combustion plant (CAB), and at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4) , in each stage, by primary air (AIR1) delivered to the front part (CAS) of the catalytic combustion facility (CAB), within a time frame of 0,015-0,10s, preferably between 0,02-0, Within the time frame of 06s, only sequentially supplied fuels (FU1, FU2, FU3, FU4) are catalytically combusted step by step so that the temperature in the catalytic combustion phases (CA1, CA2, CA3, CA4) is more than 800°C and less than 1100°C, preferably less than 1000°C, where catalytic combustion is performed with excess air measured as residual oxygen (preferably 1-3%) and fuel in catalytic combustion stages (CA1, CA2, CA3, CA4) /air ratio below the LEL (Lower Explosive Limit);

- at least one heat transfer part (HT1, HT2, HT3) for reducing the temperature of the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4), and said heat transfer part ( HT1, HT2, HT3) before the next successive catalytic combustion stage (CA1, CA2, CA3, CA4);

- Exhaust device (EXH) for exhausting combustion gases (EXG) in the aft section (CAL) of the combustion plant (CAB).

The catalytic combustion facility according to the second aspect of the utility model comprises:

- a primary fuel supply (FUE) for delivering at least 90%, preferably at least 99%, of the fuel required in the catalytic combustion (CAB) as primary (AIR1) to the front part of the catalytic combustion facility (CAB) ( CAS);

- at least two successive oxidizing gas or liquid supply sources (OXY) for supplying oxidizing gas or liquid supply into the catalytic combustion plant (CAB), and at least two successive catalytic combustion stages (CA1, CA2, CA3, CA4) , in each phase only sequentially supplied fuels (FU1, FU2, FU3, FU4 ), so that the temperature in the catalytic combustion stages (CA1, CA2, CA3, CA4) is more than 800°C and less than 1100°C, preferably less than 1000°C, and wherein, in the catalytic combustion stages (CA1, CA2, CA3 , CA4) where the fuel/air ratio is above the UEL (Upper Explosive Limit);

- at least one heat transfer part (HT1, HT2, HT3) for reducing the temperature of the gas (EXG) generated in at least one successive catalytic combustion stage (CA1, CA2, CA3, CA4), and said heat transfer part ( HT1, HT2, HT3) before the next successive catalytic combustion stage (CA1, CA2, CA3, CA4);

- Exhaust device (EXH) for exhausting combustion gases (EXG) in the aft section (CAL) of the combustion plant (CAB).

According to an aspect of the invention, the catalytic combustion facility CAB is provided in its tail section CAL with at least one residual heat transfer element HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1, CA2, CA3, CA4.

According to an aspect of the invention, the heat transfer parts HT1 , HT2, HT3 and/or the residual heat transfer part HT4 have a tubular design.

According to one aspect of the invention, the catalytic converters used in the catalytic combustion stages CA1 , CA2 , CA3 , CA4 are hybrid catalytic converters comprising noble metals from metal honeycombs.

According to one aspect of the present invention, downstream of the front part CAS of the catalytic combustion facility CAB, the catalytic combustion facility CAB is provided with a secondary air supply source AIR2, which can be used to deliver the air required in the catalytic combustion CAB. Not more than 10% of air.

According to an aspect of the invention, the sequential fuel supply FU1, FU2, FU3, FU4 is suitable for gaseous or liquid fuels.

In this application, the air required in catalytic combustion CAB refers to the amount of air consumed for complete combustion of the fuel employed. It also includes possible excess air required to ensure complete combustion. This excess air can be delivered as primary air or secondary air.

The sequence of components and stages has been reported with reference to the flow direction of the primary air AIR1.

Averages used are 24-hour averages unless otherwise reported.

The catalytic method of the present invention uses a lean air-fuel mixture that is difficult to burn thermally and can be oxidized in multiple successive stages such that the gas is always cool after a stage. Therefore, the maximum temperature can be adjusted so low that NO _x emissions do not occur. This method enables energy production with high efficiency and practically no nitrogen oxides (NO _x ), VOC and carbon dioxide (CO) emissions. These temperatures are also optimal for oxidizing hydrocarbon and carbon monoxide gases so efficiently that no emissions are produced (<1 ppm). In addition to the low oxidation temperature, the formation of NO _x is excluded by high-speed catalytic oxidation of about 0,02-0,06 seconds, ie about 20 times that in thermal combustion. Another contributing factor is the rapid cooling immediately after oxidation.

Complete combustion of the fuel is enhanced by a mixed-metal honeycomb catalytic converter containing precious metals. The hybrid structure provides a significant enhancement of mass transfer (ie, the diffusion of reactants into the pores of the active coating). Other catalytic converters activated with base metal oxides such as ceramic honeycomb cells are also useful, but these are not as efficient and durable as the catalytic converters described above.

Catalytic combustion is the only method by which oxidation can be performed so as not to produce nitrogen oxides at all, since it can be performed at significantly lower temperatures and substantially higher rates than thermal combustion. During oxidation of high concentrations, the temperature also rises to very high levels in the catalytic converter, even much higher than in thermal combustion, because, as its name implies, the catalytic converter catalyzes or accelerates the reaction and essentially converts The temperature rises. If nearly stoichiometric gas mixtures useful in thermal combustion were catalytically oxidized in a single stage, the temperature would rise to about 2500°C according to modeling. With the device of the invention, by dividing the oxidation into several stages, and by oxidizing lean mixtures which are difficult to burn efficiently thermally, the temperature can be maintained at a temperature of less than 1000°C. An advantage of catalytic combustion is the very high combustion efficiency, even with lean mixtures. In fact, its combustion efficiency is 100%.

The device according to the invention is characterized in that the oxidation is carried out in several stages in such a way that the air/oxygen required for all stages in the combustion is always present in the reaction, while the substance to be oxidized is carried out step by step way to add to airflow. Oxidation is carried out with a catalytic converter in each stage. Dividing the exothermic oxidation reaction into several stages enables the maximum temperature to be reduced to a desired level. The gas is cooled between oxidation stages.

In thermal combustion, there are severe restrictions on igniting the fuel/air mixture. For methane, for example, ignition has a lower limit (LEL) of about 5% and an upper limit (UEL) of about 15%. Combustion in conventional boilers typically occurs with a fuel/air mixture of about 10%, which is close to the stoichiometric ratio.

In catalytic oxidation, the confinement is much looser than in thermal combustion. In the absence of supporting energy, less than 1% of the mixture can be oxidized. Likewise, methane/air mixtures greater than 15% can be partially oxidized as long as oxygen is present. Thus, oxidation or a simultaneous temperature rise can be adjusted with the concentration of combustible gas or oxygen.

If natural gas is oxidized, for example, in three stages, the amount of fuel in each stage will be about 3,3% of the mixture. In this case, the temperature in the catalytic converter will be maintained at less than about 1000°C. Each catalytic oxidation stage is followed by cooling of the gas in a heat exchanger, preferably to about 150-350°C, before the next oxidation stage. During cooling, heat is transferred to water, air or some other medium.

The invention enables partial oxidation not only of lean air/fuel mixtures but also of rich gas mixtures so that only some of the fuel can be oxidized. The purpose may be to oxidize a desired part or desired constituent, eg fully oxidize the hydrogen from the fuel and only partially oxidize the carbon to carbon monoxide gas which can be used as an industrial raw material. Partial oxidation can be performed by incrementally supplementing the fuel stream with oxidant prior to each catalytic converter.

Features of the utility model include:

1. Thin mixture

- Oxidation with several successive catalytic converters in such a way that almost all or all of the quantity of air required in the oxidation travels through all catalytic converters, but the substance to be oxidized is injected individually into each catalytic converter In each catalytic converter, the temperature does not rise above 1000° C. for a long time ( FIGS. 1A to 5 ).

- Catalytic combustion is carried out with an excess of air measured as residual oxygen. According to one aspect of the invention, the amount of residual oxygen in the combustion gas (EXG) from the tail section (CAL) of the combustion plant (CAB) is 0.5-10%, preferably 1-3%.

- There is preferably a heat exchanger between the catalytic converters, in which the gas is cooled to about 150-350° C. by means of a liquid or gaseous medium. Only the species to be oxidized is delivered ahead of each catalytic converter where it is oxidized, thus again increasing the temperature at its highest point to about 1000°C (run Figure 1A-1C)

- Dividing the fuel supply into two to four stages enables particularly lean fuel/air mixtures to be catalytically oxidized. This principle can be used to construct catalytic oxidation plants that will not produce nitrogen oxides (NO _x ) at all and will also have extremely low (<1 ppm) emissions of carbon monoxide (CO) and hydrocarbons (CH). This emission level is achieved notably by means of the X-Flow catalytic converter described in Utility Model No. 10627.

- With the catalytic converter's ability to oxidize lean fuel mixtures, the performance of the boiler can be adjusted with the volume of fuel alone, or together with the volume of air.

-Usable fuels include gaseous or liquid clean fuels, such as natural gas and liquefied gas, low-sulfur light oil, alcohols, biogas and bioliquid, etc. As long as the fuel does not contain nitrogen compounds, no nitrogen oxides are produced.

- The flue gas can be used unrefined for _CO2 fertilization of the greenhouse. Since, in this case, the thermal energy contained in the flue gas is also used, the thermal efficiency of the boiler rises to almost 100%.

- Regenerative heat exchangers enable various gaseous and liquid substances to be heated. In this case, utilities are eg hot water, steam, warm air etc. boilers useful for heating buildings and industrial processes.

- The principles shown in the operation of Figures 1A-1C can also be applied to construct an air heater function with a regenerative heat exchanger.

- The boiler allows the parallel use of various energy sources, such as natural gas, fuel oil, alcohols, etc. The primary and secondary air supplies may also include VOC compounds or other combustion compounds that are oxidized in the catalyst. The concentration of these gases from the supply can be up to 20% of the AEL. A temperature sensor that controls the fuel supply can be controlled to reduce the fuel supply.

- The first and most important application results from catalytic converters activated with noble metals such as platinum (Pt) and palladium (Pd). Base metal oxides such as oxides of lanthanum, cerium, nickel, copper, chromium, tungsten, manganese, iron, cobalt, barium may also be used. Combinations of the above can also be used, but these are not as reactive and durable as noble metals or their mixed oxides.

2. Rich mixture

- The facility can also operate in rich mixtures (>UEL limit) without enough oxygen to combust the entire amount of fuel. In this case, the continuous gas flow will be fuel sequentially replenished with the quantity required for partial oxidation, air, pure oxygen or other oxidizing gas or liquid. Along with the fuel, water can be delivered to cool the reaction or promote selective oxidation, if necessary.

According to an aspect of the invention, at least 90%, preferably more than 99%, of the fuel travels through the entire process, and a controlled amount of air is delivered before each catalytic converter. It is therefore beneficial to pursue partial oxidation in such a way that, for example, only the hydrogen contained in the gas is oxidized by the selective catalytic converter while the oxidation of carbon is limited to carbon monoxide. Hot gases including CO at eg 900° C. can be used eg in the case of hardened steel. The technical application with respect to the method and device can be done as in the application described above, but the delivery of fuel and air is reversed as appropriate.

According to an aspect of the invention, the catalytic combustion plant (CAB) is carried out by using at least one static mixer before the catalytic combustion stages (CA1, CA2, CA3, CA4). This creates a strongly turbulent fluid.

A facility can be made from three identical heating modules and heat transfer modules. The heating modules (preferably 2 to 4) include fuel supply, vertical and horizontal static mixers and catalytic converters. After each heating module there is a heat transfer which can be made of finned tubes connected in series or in parallel. Some modules can also be used for heat recovery of condensers with exhaust gases.

Description of drawings

Several embodiments of the present invention are shown in Fig. 1A to Fig. 7:

FIG. 1A shows a 2-stage catalytic combustion plant comprising primary and secondary air supplies and tube heat exchangers.

Figure 1B shows a 3-stage catalytic combustion plant comprising primary and secondary air supplies and tube heat exchangers.

Figure 1C shows a 4-stage catalytic combustion plant comprising primary and secondary air supplies and tube heat exchangers.

Figure 2 shows a 3-stage catalytic combustion plant comprising primary and secondary air supplies and a continuous heat exchanger in the outer jacket.

Figure 3 shows a 3-stage catalytic combustion plant comprising primary and secondary air supplies and a 3-stage heat exchanger in the outer jacket.

Figure 4 shows a 3-stage catalytic combustion plant whose heat and exhaust gases are utilized in a greenhouse.

FIG. 5 shows a 3-stage catalytic combustion plant including 1-stage fuel supply and 3-stage oxygen supply.

Figure 6 shows an operational diagram of a combustion plant with 3-stage fuel supply.

Figure 7 shows an operational diagram of a combustion plant with 3-stage oxygen supply.

Detailed ways

The catalytic combustion facility shown in Figures 1A-1C and Figures 2-3 includes: a primary air supply source AIR1 for at least 90%, preferably at least 99%, of the air required in the catalytic combustion CAB as primary air AIR1 Delivery into the front part CAS of the catalytic combustion facility CAB; 2-4 sequential fuel supply sources FU1, FU2, FU3, FU4 for fuel delivery into the catalytic combustion facility CAB, and 2-4 sequential catalytic combustion only Stages CA1, CA2, CA3, CA4 for the gradual combustion of sequentially supplied fuels FU1, FU2, FU3, FU4 by primary air AIR1 delivered into the front part CAS of the catalytic combustion plant; including 1-3 heat transfer elements HT1 , HT2, HT3 heat transfer parts HT, used to reduce the temperature of the gas EXG generated in at least one successive catalytic combustion stage CA1, CA2, CA3, and said heat transfer parts HT1, HT2, HT3 in the next successive catalytic combustion Before the phases CA1 , CA2 , CA3 , CA4 ; the exhaust device EXH for the combustion generated gases EXG in the rear part CAL of the combustion plant CAB. The tail section CAL of the catalytic combustion plant CAB is provided with a residual heat transfer element HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1 , CA2 , CA3 , CA4 . The cold water W _cold has been directed through the combustion plant for generating hot water W _heat and/or warm water W _warm .

According to Figures 1A-1C and Figures 2-3, the catalytic combustion facility also includes a secondary air supply source AIR2.

According to Figures 1A-1C, the heat transfer parts HT1, HT2, HT3 and/or the residual heat transfer part HT4 have a tubular design. According to Fig. 2, the heat transfer parts HT1, HT2, HT3 are included in the outer jacket and consist of a continuous structure, whereas the embodiment of Fig. 3 includes separate heat transfer parts HT1, HT2, HT3 in the outer jacket.

Fig. 4 shows a catalytic combustion facility consistent with Fig. 2 to utilize gas EXG and hot water produced by combustion in a greenhouse Green.

Figure 5 depicts a 3-stage catalytic combustion facility comprising: a primary fuel supply source FUE for supplying at least 90%, preferably at least 99%, of the fuel required in the catalytic combustion CAB to the front part CAS of the catalytic combustion facility CAB ; 3 successive oxygen supplies OXY for delivery of oxygen into the catalytic combustion facility, and 3 successive catalytic only combustion stages CA1, CA2, CA3 for progressive combustion of the fuel FUE by the delivered oxygen; with two successive heat The heat transfer part HT of the transfer part HT1, HT2 is used to reduce the temperature of the gas EXG generated in the three successive catalytic combustion stages CA1, CA2, CA3, and said heat transfer part HT1, HT2, HT3 in the next successive catalytic combustion Before the phases CA1 , CA2 , CA3 ; the exhaust device EXH for the gases EXG generated by the combustion in the rear part CAL of the combustion plant CAB. The tail section CAL of the catalytic combustion plant CAB is provided with a residual heat transfer part HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1 , CA2 , CA3 , CA4 . Cold water W cold has been directed through the combustion plant for use in generating hot water W heat. This embodiment also includes a condenser COOL for combustion gas EXG, in which _warm water W is produced and exhaust gas and condensate EXC.

The production diagram in Fig. 6 consists of feeding fuels FU1, FU2, FU3 into the catalytic combustion plant CAB in three successive stages, and by primary air AIR1 delivered to the front part CAS of the catalytic combustion plant sequential combustion of sequentially supplied fuels FU1, FU2, FU3 in successive catalytic-only stages CA1, CA2, CA3; in two heat-transfer stages HT1, HT2, reduction in at least one successive catalytic-combustion stage CA1, CA2, CA3 The temperature of the gas EXG of the heat transfer stage HT1, HT2 before the next successive catalytic combustion stage CA1, CA2, CA3, CA4; removal of the combustion gas EXG from the tail section CAL of the combustion facility CAB. The tail section CAL of the catalytic combustion plant CAB is provided with a residual heat transfer part HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1 , CA2 , CA3 . The cold water W _cold has been led through the combustion plant for generating hot water W _heat and/or warm water W _warm . The catalytic combustion facility also includes a secondary air supply source AIR2.

The production diagram in Figure 7 includes: a primary fuel supply source FUE in the front part CAS of the combustion plant CAB; 3 successive oxygen supply sources OXY for delivering oxygen into the catalytic combustion plant CAB, and 3 successive catalytic combustion Stages CA1, CA2, CA3 for progressive combustion of fuel FUE by sequentially delivered oxygen; heat transfer part HT comprising 2 heat transfer parts HT1, HT2 for reducing The temperature of the gas EXG generated in and said heat transfer parts HT1, HT2 before the next successive catalytic combustion stages CA1, CA2, CA3; the exhaust device EXH for the combustion generated in the tail part CAL of the combustion plant CAB Gas EXG. The tail section CAL of the catalytic combustion plant CAB is provided with a residual heat transfer element HT4 for reducing the temperature of the combustion gas EXG after the catalytic combustion stages CA1 , CA2 , CA3 , CA4. Cold water _Wcold has been directed through the combustion plant for generating _hot water Wheat.

In the equipment of the present invention, the heat exchangers used may include various regenerative heat exchangers or regenerative heat exchangers, which may be made of ordinary boilers or stainless steel grades such as 1.4512 and 1.4509. In catalytic converters, FeCrAl alloyed high temperature steel grades such as 1.4767 are preferred.

A tubular recuperator will form the bulk of the boiler, especially if the substance to be heated is a liquid. Implementation can be based on two different principles. According to the principle of convection, the water passes inside the tube, while the combustion gas passes back and forth several times outside the tube (Fig. 1A-1C). Preference is given to using tubes with small diameters, since the tubes then have a large external surface relative to the cross-sectional area. This is because the heat transfer coefficient from gas to steel, even at its maximum, is only about one-tenth that of that from steel to water.

Heat transfer can be enhanced by arranging tubes in the exchanger to enable a turbulent flow of the combustion gases. Heat transfer can be further enhanced not only with flow guiding walls Mix, but also with separate steel construction partitions that forcefully expand the tubes from the inside in order to create snug metal-to-metal contact surface to engage the pipe. This partition is required to have a sufficient thickness (1,5-2mm) for effective heat transfer from the gas to the steel pipe. Finned tubes become another useful option for enhancing heat transfer from gas to metal.

The flow is preferably divided into two to four sections with gas-tight partitions, in each section the gas passes once back and forth through a series of tubes. Before each section, the gas passes through a catalytic converter.

The facility is activated by heating the catalytic converter with an injector to a temperature of about 450-650°C, after which the flame can be extinguished and the catalytic converter starts to oxidize the gas, while at the same time the supply of air and gas can be raised to a basic level.

Typically, the facility is activated with the same fuel as used in continuous operation of the facility, but with reduced fuel and air flows, and the fuel/air mixture is in the highly flammable range close to the stoichiometric mixture, the fuel/air mixture is used Lit with the standard igniter used in the boiler. Each catalytic converter follows the fuel injection and ignition unit Ign. It is preferred to deliver the fuel into the hot gas stream prior to the catalytic converter to allow time for the liquid fuel to vaporize and mix uniformly before reaching the catalytic converter.

Minor adjustments in boiler performance can be made by reducing fuel supply, while major adjustments can be made by cutting both fuel and air supply.

Downstream of the catalytic converter is a temperature sensor that can be used to monitor the operation of the catalytic converter. If the temperature drops below a set lower limit (eg 700°C), the active mode will be re-established.

The last catalytic converter can have a lower throughput (throughput) than the preceding (leading) catalytic converter, wherein, depending on the fuel, this throughput can preferably vary in the range of 60.000-300.000 1/h. In the last one, in order to achieve zero level discharge, the treatment capacity can preferably be in the range of 40.000-200.000 1/h.

The plant can vary its capacity from low to high, eg 10kW-100MW.

Presented below are two examples of boilers of the described type, for which dimensional and model calculations and sketches 1A-1C and 3 were made.

Embodiment 1 The design scheme based on the structure of the tubular heat exchanger and its main dimensions and technical grade specifications is as follows:

- The fuel may be natural gas or eg (bio)ethanol.

- The capacity of the boiler with natural gas is 50MW, while that with bioethanol is about 29MW. The same facility could be used for both, but the fuel nozzles and the amount of fuel injected in the various stages had to be changed for reaching sufficiently high temperatures (800-950°C) in the first two stages. The amount of natural gas is preferably allocated in order of 36%, 32% and 32%. The distribution of ethanol will preferably be 36%, 32% and 32%. A small excess of air, measured as residual oxygen (preferably 1-3%), ensures complete combustion.

- Catalytic converter types are as follows:

· The first catalytic converter and the second catalytic converter are 4000 x 1200 x 120 mm (W x H x L) and have a volume of 576 dm3, a throughput of 95.500 1/h, a pore density of 100 cpsi and a load of 70 g/ft3 Pd.

• The third catalytic converter is otherwise identical except that it has a length of 150 mm, a volume of 720 dm3 and a capacity of 76.400 1/h.

• Inject the first catalytic converter with 36% of the total amount of fuel, so that the gas temperature rises from +20°C to about 850°C, cooling in the heat exchanger to about 350°C.

• The second and third catalytic converters receive 32% of the fuel so that the temperature rises to about 900°C.

- Calculations have been performed with a heat transfer coefficient of 180 W/m2oK based on making the flow in the heat exchanger turbulent.

- The tubes are DIN 40 x 8000 mm, a total of about 500 rods, material 1.4512.

- External boiler dimensions will be 4500×9000×4000mm (W×L×H).

- The pressure loss is about 5000 Pa.

In this case, the boilers depicted in Figures 1A-1C have utilized conventional tube heat exchangers, where, as presented in Figures 1A-1C, water (fluid) travels in tubes while heated gas travels back and forth Travel through catalytic converters and tubular honeycombs.

A schematic diagram of the dimensions of the second exemplary embodiment is shown in FIG. 3 . The heat capacity of such a boiler with natural gas is about 1 MW, and with ethanol - 0,58 MW.

The boiler is assembled from three elements provided with a hybrid X-flow type catalytic converter and a heat exchanger. As an extension, a similar element can be included, which is a heat exchanger in the absence of a catalytic converter for increased efficiency.

The heat exchanger has diagonally corrugated plates stacked in a vertical direction such that crests of the corrugations intersect each other in different directions to create cross-extending flow channels in the shape of a letter X. The hybrid honeycomb structure thus created is welded at its ends using, for example, resistance welding (capacitor discharge or seam welding) or laser welding for attachment to the casing. The surface of the shell thus constructed has an outer shell made of plates on it, so that a gap of about 25 mm remains between them, in which gap the water to be heated flows. Multiple sheets of steel plates are welded to enhance even water flow and heat transfer.

Each element includes inlet and outlet conduits for the fluid to be heated. The pipes are usually connected in series in such a way that cold water flows from the aft end of the boiler to the front. The pipes can also be connected in parallel, thus providing three separate water heating circuits.

The boiler of Figure 3 can be assembled from elements with flange joints. The outer surface is equipped with thermal insulation. Such a modular structure can also be constructed by having elements mounted on top of each other and connected by flow channels.

The dimensions of the boiler are as follows:

- The dimensions of the first catalytic converter and the second catalytic converter are 200×500×120mm (H×W×L), the volume is 12,0dm ³ , the treatment capacity is 91.700 1/h, the pore density is 100cpsi and the load is 70g/ft3Pd.

- The third catalytic converter is 200 x 500 x 150 mm and has a volume of 15,0 dm3 and a throughput of 73.300 l/h. In other respects, the specifications are the same as those of the first and second monomers.

- The size of the heat exchanger will be 200×500×300mm, the corrugation height will be 10mm, the plate thickness will be 0,6mm and the material will be 1.4509.

- The heat transfer capacity has been calculated with a rate of 130W/m2oK.

- The pressure loss is about 5000 Pa, and the temperature is equal to that in the previous example.

If it is desirable to run the above-mentioned boiler with some other fuel, its distribution of supply for the various stages must be optimized in order to optimize the heat transfer capacity. Natural gas has a calorific value of about 50 MJ/kg, light fuel oil has a calorific value of 42,7 MJ/kg, liquefied gas has a calorific value of 46,4 MJ/kg, carbon monoxide gas has a calorific value of 10 MJ/kg, and ethanol has a calorific value of 29 MJ/kg Calorific value of kg.

Flue gas emissions from boilers can be monitored with _NOx , SOx, VOC and CO sensors, among others.

An option for the solution shown in Figure 3 is to construct a circulation boiler. In this case, too, the gas flows inside the tube while the water travels inside the outer jacket of the tube. Therefore, the catalytic converters are in a vertical row within the tube. (Fig. 2) In order to enhance heat transfer, a static mixer capable of generating severe turbulent flow is provided inside the tube. The blades or helices of the mixer are fastened eg by welding to the outer surface of the tube. This approach has been envisaged for low volumes. For example, a 50kW natural gas boiler would be approximately D300 x 1500mm in size.

The above examples demonstrate the applicability of catalytic combustion to thermal power plants of all sizes and capacities.

As a summary of the above, it can be concluded that it is not possible to generate completely _NOx- free thermal energy with thermal combustion and its associated cleaning methods for flue gases. The high temperature and _relatively long duration of the thermal combustion always produces NO _x , which cannot then be completely removed. This is what hinders the complete thermal oxidation of carbon and hydrogen. Industrial complete oxidation of carbon and hydrogen, without _NOx formation, can only be achieved with the catalytic combustion equipment of the present invention operating at lower temperatures, and by oxidizing clean fuels such as natural gas, biogas, bioethanol, etc. . In this case, the process generates no other harmful emissions than carbon dioxide (CO2), which can be used in services such as fertilization of plants. All flue gases can be directed into the greenhouse where they are distributed by the pipe system to be utilized by the plants (Fig. 4). Thus, the thermal energy contained in the flue gas is also utilized. Since extra moisture is detrimental to growth, the moisture contained in the flue gas can be removed with a condensing heat exchanger before delivering the flue gas into the greenhouse (Figure 5).

Outdoor air has a carbon dioxide content of about 380 ppm. The greatest benefit of CO2 fertilization was achieved in vegetable growing greenhouses, where growth was accelerated by up to more than 40% due to double or triple CO2 concentrations compared to base levels. It is a happy coincidence that the greenhouse demands for heat and carbon dioxide in the Nordic countries can be met simultaneously by oxidation of hydrocarbons, since the production of the necessary heat is accompanied by the production of an almost optimal amount of the often harmful carbon dioxide. CO2 fertilization can provide superior growth in greenhouse capacity, thus reducing energy and capital costs of production.

Finland is characterized by about 1000 companies that commercially grow vegetables in greenhouses. 330 of these companies utilize industrially produced CO2 in liquid or gaseous form. The cheapest liquefied gas costs about 0,10€/kg, while the most expensive bottled gas costs about 2€/kg. The amount of industrially produced CO2 used in Finland is 4 to 5 million kg/year. Worldwide consumption is estimated to be hundreds of times more. The utilization of carbon dioxide generated in energy production is therefore a topic of high importance not only in terms of reducing greenhouse emissions, but also in terms of economics. The most significant environmental impact is achieved when the fuel used is bioethanol, syngas or other biofuels. In this case, energy production has a negative carbon footprint. Going like this can also replace some of the CO2 that is produced industrially and transported to greenhouses.

If the boilers of the present invention were manufactured so as to cover 1% of global boiler production, the result would be about 10 million catalytic converter market.

Claims (18)

1. A kind of 1. catalysis combustion plant (CAB) for being used to generate energy with high efficiency, which is characterized in that the catalysis combustion plant (CAB) including at least with lower component：

   Primary air supply source (AIR1), at least the 90% of burning air needed for (CAB) will to be catalyzed, as primary Air (AIR1) is delivered in the preceding part (CAS) of the catalysis combustion plant (CAB)；

   - at least two successive fuel supply sources (FU1, FU2, FU3, FU4) set for supplying fuel to the catalysis burning It applies in (CAB)；With at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4), in each stage, pass through delivering To the primary air (AIR1) in the preceding part (CAS) of the catalysis combustion plant (CAB), in the time frame of 0.015-0.10s Fuel (FU1, FU2, FU3, FU4) interior, that only gradually catalytically combustion order supplies so that in the catalysis combustion phases Temperature in (CA1, CA2, CA3, CA4) is higher than 800 DEG C and less than 1100 DEG C,

   Wherein, the catalysis burning is provided as：The catalysis burning is carried out using excess air, wherein the excess air base It is measured in remnant oxygen, and the fuel/air rate in the catalysis combustion phases (CA1, CA2, CA3, CA4) explodes Under lower limit (LEL), and

   Wherein, the catalyst for the catalysis combustion phases (CA1, CA2, CA3, CA4) is mixed catalytic converter, institute It states mixed catalytic converter and includes the noble metal from metal beehive；

   At least one heat transfer component (HT1, HT2, HT3), for reducing at least one successive catalysis combustion phases The temperature of the gas (EXG) generated in (CA1, CA2, CA3, CA4), and the heat transfer component (HT1, HT2, HT3) is under Before one successive catalysis combustion phases (CA1, CA2, CA3, CA4)；

   The gas (EXG) that burning for discharge in the tail portion (CAL) of the catalysis combustion plant (CAB) generates Exhaust apparatus (EXH).
2. 2. the catalysis combustion plant according to claim 1 for being used to generate energy with high efficiency, which is characterized in that described to urge The tail portion (CAL) for changing combustion plant (CAB) is provided at least one remaining heat transfer component (HT4), for being urged described Changing the downstream of combustion phases (CA1, CA2, CA3, CA4) reduces the temperature of gas (EXG) of the burning generation.
3. 3. the catalysis combustion plant according to claim 2 for being used to generate energy with high efficiency, which is characterized in that the heat Transferring element (HT1, HT2, HT3) and/or the remaining heat transfer component (HT4) have tube designs.
4. 4. the catalysis combustion plant according to claim 1 or 2 for being used to generate energy with high efficiency, which is characterized in that residual The amount of remaining oxygen is 0.5-10%.
5. 5. the catalysis combustion plant according to claim 1 or 2 for being used to generate energy with high efficiency, which is characterized in that institute It states catalysis combustion plant (CAB) and is provided at least one static state before the catalysis combustion phases (CA1, CA2, CA3, CA4) Mixer.
6. 6. the catalysis combustion plant according to claim 1 or 2 for being used to generate energy with high efficiency, which is characterized in that institute It states catalysis combustion plant (CAB) and is provided with secondary air supply source (AIR2), the secondary air supply source (AIR2) is for passing Air is sent, and the air that the secondary air supply source (AIR2) is delivered is not more than empty needed for catalysis burning (CAB) The 10% of gas.
7. 7. the catalysis combustion plant according to claim 1 or 2 for being used to generate energy with high efficiency, which is characterized in that There are heat exchangers between the catalyst.
8. 8. the catalysis combustion plant according to claim 1 or 2 for being used to generate energy with high efficiency, which is characterized in that The downstream of the catalyst is provided with temperature sensor.
9. 9. the catalysis combustion plant according to claim 1 for being used to generate energy with high efficiency, which is characterized in that described one Secondary air supply source (AIR1) is used as primary air (AIR1) for that will be catalyzed at least the 99% of burning air needed for (CAB) It is delivered in the preceding part (CAS) of the catalysis combustion plant (CAB).
10. 10. the catalysis combustion plant according to claim 1 for being used to generate energy with high efficiency, which is characterized in that in institute It states in each stage at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4), by being delivered to described urge Change the primary air (AIR1) in the preceding part (CAS) of combustion plant (CAB), in the time frame of 0.02-0.06s, only gradually Catalytically combustion order supply fuel (FU1, FU2, FU3, FU4) so that it is described catalysis combustion phases (CA1, CA2, CA3, CA4 the temperature in) is higher than 800 DEG C and less than 1000 DEG C.
11. 11. the catalysis combustion plant according to claim 3 for being used to generate energy with high efficiency, which is characterized in that described Heat transfer component (HT1, HT2, HT3) and/or the remaining heat transfer component (HT4) are designed with finned tube.
12. 12. the catalysis combustion plant according to claim 4 for being used to generate energy with high efficiency, which is characterized in that described The amount of remnant oxygen is 1-3%.
13. 13. a kind of 3 stage catalytic combustion plants (CAB), which is characterized in that the 3 stage catalytic combustion plant (CAB) is including extremely Less with lower component：

    Primary fuel supply source (FUE), for institute will to be supplied at least 90% of fuel needed for catalysis burning (CAB) In the preceding part (CAS) for stating 3 stage catalytic combustion plants (CAB)；

    For 3 successive oxygen supply sources (OXY) that oxygen is supplied in the 3 stage catalytic combustion plant；And it uses It gradually burns 3 of the fuel (FUE) successive only catalysis combustion phases (CA1, CA2, CA3) in the oxygen by delivering；

    - two successive heat transfer components (HT1, HT2), for reducing three successive catalysis combustion phases (CA1, CA2, CA3 the temperature of the gas (EXG) generated in), and the heat transfer component (HT1, HT2, HT3) is in next successive catalysis Before combustion phases (CA1, CA2, CA3)；

    The gas for discharge burning generation in the tail portion (CAL) of the 3 stage catalytic combustion plant (CAB) (EXG) exhaust apparatus (EXH),

    Wherein, the catalyst for the catalysis combustion phases (CA1, CA2, CA3) is mixed catalytic converter, described mixed It closes catalyst and includes the noble metal from metal beehive.
14. 14. 3 stage catalytic combustion plant according to claim 13, which is characterized in that the 3 stage catalytic combustion plant (CAB) tail portion (CAL) setting there are one remaining heat transfer component (HT4), for the catalysis combustion phases (CA1, CA2, CA3, CA4) temperature of gas (EXG) that the burning generates is reduced later.
15. 15. the 3 stage catalytic combustion plants according to claim 13 or 14, which is characterized in that the 3 stage catalytic burning Facility (CAB) further includes the condenser (COOL) of the gas (EXG) for generation of burning.
16. 16. the 3 stage catalytic combustion plants according to claim 13 or 14, which is characterized in that for the catalysis burning The catalyst in stage (CA1, CA2, CA3) is provided with heat exchanger, and the heat exchanger has in the vertical direction The diagonal corrugated plating stacked so that the wave crest of ripple intersects in different directions, is prolonged with establishing in the intersection of the shape of letter X Circulation road is stretched, thus establishes hybrid cellular structure.
17. 17. 3 stage catalytic combustion plant according to claim 16, which is characterized in that the mixing of the catalyst Honeycomb is soldered to be attached with shell in its end.
18. 18. 3 stage catalytic combustion plant according to claim 13, which is characterized in that the primary fuel supply source (FUE) the 3 stage catalytic combustion plant (CAB) will be supplied at least 99% of fuel needed for catalysis burning (CAB) Preceding part (CAS) in.